CN214809744U - System for directly mineralizing flue gas carbon dioxide based on three-phase fluidized bed - Google Patents
System for directly mineralizing flue gas carbon dioxide based on three-phase fluidized bed Download PDFInfo
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- CN214809744U CN214809744U CN202121253082.2U CN202121253082U CN214809744U CN 214809744 U CN214809744 U CN 214809744U CN 202121253082 U CN202121253082 U CN 202121253082U CN 214809744 U CN214809744 U CN 214809744U
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model relates to a based on three-phase fluidized bed direct mineralization flue gas carbon dioxide system adopts gas-liquid-solid three-phase fluidized bed, owing to adopt the fine powder granule to contact with the fluid under the suspension state, liquid-solid interfacial area is big, is favorable to going on of heterogeneous reaction, has improved the utilization ratio of catalyst, and the reaction is gone on with higher speed, and the ammonium carbonate that the decarbonization generated contacts with excessive gypsum and is all converted into calcium carbonate rapidly, has realized single tower carbon dioxide desorption and gypsum mineralization process; the fluidized bed layer design is very favorable for the separation of gypsum particles and calcium carbonate particles, and the utilization rate of gypsum and the purity of calcium carbonate are obviously improved.
Description
Technical Field
The utility model belongs to the atmospheric pollutants field of purifying relates to a based on three-phase fluidized bed direct mineralization flue gas carbon dioxide system.
Background
Greenhouse gases have serious influence on global climate, the requirement of carbon dioxide emission reduction is remarkably increased, carbon emission of coal-fired power plants accounts for the maximum total emission of China at present, and the decarburization capability becomes an important research direction of coal-fired units in future.
At present, the smoke decarbonization of a coal burner unit mainly adopts a carbon capture, utilization and storage (CCUS) technology. The organic amine is used as an absorbent and reacts with carbon dioxide in the smoke to generate water-soluble salt, then the absorption liquid is heated to release and capture the carbon dioxide, and the absorption liquid is regenerated.
At present, because the desulfurized gypsum has low quality and large yield and is difficult to be recycled, the desulfurized gypsum is generally stacked and buried, occupies land and pollutes the environment, and is an industrial solid waste to be treated urgently. The technology for directly mineralizing gypsum and co-producing ammonium sulfate and calcium carbonate by using flue gas and carbon dioxide is always a research hotspot, but the prior art does not relate to the development of carbon capture and utilization technology of a coupling wet desulphurization system, and does not relate to the research of the process technology of calcium circulation of the desulphurization system.
SUMMERY OF THE UTILITY MODEL
The utility model provides a direct mineralize flue gas carbon dioxide system based on three-phase fluidized bed to the carbon entrapment that exists not involving coupling wet flue gas desulfurization system among the prior art, utilize the development of process technology, do not relate to the problem of the process technology research of desulfurization system calcium circulation, the utility model provides a.
The utility model discloses a realize through following technical scheme:
a system for directly mineralizing flue gas carbon dioxide based on a three-phase fluidized bed is characterized by comprising a three-phase fluidized bed absorption tower, an ammonium sulfate crystallization generation device and a calcium carbonate generation device;
the calcium carbonate generating device comprises a calcium carbonate cyclone, a gypsum slurry tank and an ammonia conveying pipe;
the three-phase fluidized bed absorption tower is sequentially provided with an ammonium sulfate concentration spraying area, a three-phase fluidized reaction area and a demisting area from bottom to top;
a slurry pool is arranged at the bottom of the ammonium sulfate concentration spraying area, and a concentration spraying layer is arranged at the top of the ammonium sulfate concentration spraying area; the slurry pool is connected with an ammonium sulfate crystallization generation device;
the bottom of the three-phase fluidization reaction zone is sequentially provided with a gas distribution plate, an ammonia supplementing pipe grid and a gypsum slurry pipe grid from bottom to top, an outlet of the ammonia supplementing pipe grid is vertically downward, an input end of the ammonia supplementing pipe grid is connected to an ammonia conveying pipe, an outlet of the gypsum slurry pipe grid is vertically upward, and an input end of the gypsum slurry pipe grid is connected to an output end of the bottom of a gypsum slurry tank; and the side wall of the upper part of the three-phase fluidization reaction zone is provided with a calcium carbonate discharge outlet and is connected with a side cutting inlet of a calcium carbonate cyclone;
the demisting zone is sequentially provided with a demister and a process water spraying layer from bottom to top.
Further, the slurry pool is positioned below the inlet of the desulfurized flue gas.
Further, the ammonium sulfate crystallization generating device comprises an ammonium sulfate discharge pump, an ammonium sulfate swirler and a centrifuge;
the side cut inlet of the ammonium sulfate cyclone is connected with the ammonium sulfate crystallization outlet of the slurry pool through an ammonium sulfate discharge pump, and the outlet at the bottom of the ammonium sulfate cyclone is connected with the input end of the centrifuge;
the liquid phase outlet of the centrifuge is combined with the top outlet of the ammonium sulfate swirler and is connected to the ammonium sulfate slurry reflux port of the slurry pool through a reflux pump.
Further, the top outlet of the calcium carbonate cyclone is sequentially connected with the evaporation ammonia remover and the vacuum belt conveyor, and the bottom outlet is connected with the top input end of the gypsum slurry tank.
Further, an ammonia outlet of the ammonia remover is connected with an ammonia conveying pipe, and a solid phase outlet is connected with a vacuum belt conveyor.
Further, the input end of the ammonia conveying pipe is connected with an ammonia tank.
And further, a filtrate outlet of the vacuum belt conveyor is connected into a slurry pool through a filtrate pump.
Further, the side wall of the gypsum slurry tank is connected with a desulfurized gypsum slurry pipe for supplementing gypsum slurry.
Compared with the prior art, the utility model discloses following profitable technological effect has:
the utility model relates to a based on three-phase fluidized bed direct mineralization flue gas carbon dioxide system adopts gas-liquid-solid three-phase fluidized bed, owing to adopt the fine powder granule to contact with the fluid under the suspension state, liquid-solid interfacial area is big, is favorable to going on of heterogeneous reaction, has improved the utilization ratio of catalyst, and the reaction is gone on with higher speed, and the ammonium carbonate that the decarbonization generated contacts with excessive gypsum and is all converted into calcium carbonate rapidly, has realized single tower carbon dioxide desorption and gypsum mineralization process; the fluidized bed layer design is very favorable for the separation of gypsum particles and calcium carbonate particles, and the utilization rate of gypsum and the purity of calcium carbonate are obviously improved.
Further, the utility model provides an ammonium sulfate crystal generates device connects gradually calcium carbonate swirler and evaporation ammonia removal ware, and calcium carbonate swirler is high-speed rotatory, continues to participate in the reaction with gypsum thick liquid water conservancy diversion to the crystallizer tank, practices thrift the cost, and the high-usage is rateed, and calcium carbonate water conservancy diversion to evaporation ammonia removal ware to obtain solid calcium carbonate and filtrating, wherein filtrating water conservancy diversion to the thick liquid pond cyclic utilization of lower part cooling zone.
Further, ammonium sulfate crystal generating device passes through ammonium sulfate swirler and centrifuge to the ammonium sulfate thick liquid in the lower part cooling zone thick liquid pond to cooperation desulfurization flue gas waste heat can realize the evaporative crystal of ammonium sulfate, and the ammonium sulfate mainly acts on fertilizer, is applicable to various soil and crops, still can be used to the aspect such as weaving, leather, medicine simultaneously, and this system reasonable in design can reduction in production cost.
Drawings
Fig. 1 is a schematic structural flow diagram of a system for directly mineralizing flue gas and carbon dioxide based on a three-phase fluidized bed in the embodiment of the present invention.
In the figure: the device comprises a three-phase fluidized bed absorption tower 30, an ammonium sulfate crystallization generation device 31, a calcium carbonate generation device 33, an ammonium sulfate concentration spraying zone 301, a three-phase fluidized reaction zone 302, a demisting zone 303, a process water spraying layer 1, a demister 2, a three-phase fluidized bed absorption tower 3, a gypsum slurry pipe grid 4, an ammonia supplementing pipe grid 5, a gas distribution plate 6, a concentration spraying layer 7, an absorption liquid discharge pump 8, an ammonia evaporator 9, a calcium carbonate swirler 10, a vacuum belt conveyor 11, a gypsum slurry tank 12, a desulfurized gypsum slurry pipe 13, an ammonia supplementing pump 14, an ammonia tank 15, a gypsum supplementing pump 16, a filtrate pump 17, an ammonium sulfate swirler 18, a reflux pump 19, a centrifuge 20, an ammonium sulfate discharge pump 21 and a concentration circulating pump 22.
Detailed Description
The present invention will now be described in further detail with reference to specific examples, which are intended to be illustrative, but not limiting, of the invention.
The utility model relates to a direct mineralization flue gas carbon dioxide system based on a three-phase fluidized bed, which comprises a three-phase fluidized bed absorption tower 30, an ammonium sulfate crystallization generating device 31 and a calcium carbonate generating device 33;
the calcium carbonate generating device 33 comprises a calcium carbonate cyclone 10, a gypsum slurry tank 12 and an ammonia conveying pipe;
the three-phase fluidized bed absorption tower 30 is sequentially provided with an ammonium sulfate concentration spraying area 301, a three-phase fluidized reaction area 302 and a demisting area 303 from bottom to top along the height direction, the bottom of the ammonium sulfate concentration spraying area 301 is provided with a slurry tank, and the top of the ammonium sulfate concentration spraying area 301 is provided with a concentration spraying layer 7; specifically, the thick liquid pond is located desulfurization flue gas entry below, and the thick liquid pond lateral wall from supreme ammonium sulfate crystallization export, ammonium sulfate thick liquid backward flow mouth, ammonium sulfate circulation entry and the ammonium sulfate of having set gradually down sprays the loop exit, and the ammonium sulfate export connects back to ammonium sulfate thick liquid backward flow mouth through ammonium sulfate crystallization generation device 31, and ammonium sulfate circulation entry is used for connecting back calcium carbonate generation device 33 filtrating, and the ammonium sulfate sprays the concentrated input that sprays layer 7 of loop exit connection.
Specifically, the ammonium sulfate crystallization generator 31 includes an ammonium sulfate discharge pump 21, an ammonium sulfate cyclone 18, and a centrifuge 20; the side cut inlet of the ammonium sulfate cyclone 18 is connected with the ammonium sulfate crystallization outlet of the slurry pool through an ammonium sulfate discharge pump 21, the top outlet is connected with the ammonium sulfate slurry return port of the slurry pool of the three-phase fluidized bed absorption tower 30, and the bottom outlet is connected with the input end of the centrifuge 20; the liquid phase outlet of the centrifuge 20 is merged with the top outlet of the ammonium sulfate cyclone 18 and is connected with the ammonium sulfate slurry return port of the slurry pool of the three-phase fluidized bed absorption tower 30 through a return pump 19. Form the circulation process to ammonium sulfate in the concentrated spraying district bottom thick liquid pond of ammonium sulfate, simultaneously, because the temperature of desulfurization flue gas is higher, utilize the waste heat, can realize the evaporative crystallization to ammonium sulfate, ammonium sulfate mainly acts on fertilizer, is applicable to various soil and crops, still can be used to the aspect such as weaving, leather, medicine simultaneously, this system reasonable in design can reduction in production cost.
The bottom of the three-phase fluidization reaction zone 302 is provided with a gas distribution plate 6, an ammonia supplementing pipe grid 5 and a gypsum slurry pipe grid 4 from bottom to top in sequence along the height direction, the outlet of the ammonia supplementing pipe grid 5 is vertically downward, the outlet of the gypsum slurry pipe grid 4 is vertically upward, because the calcium carbonate particles have a density less than the gypsum particles, the gypsum slurry particles will collect on the distribution plate 6 at the bottom of the three-phase fluidization reaction zone 302, and cover the bottom distribution plate 6, so as to be capable of fully reacting with the exothermic desulfurization flue gas entering the three-phase fluidization reaction zone 302, the upper layer of the three-phase fluidization reaction zone 302 can enrich the generated calcium carbonate particles, so that reactants can be contacted with fluid in a suspension state, the flow-solid phase interface area is large, the heterogeneous reaction is facilitated, the utilization rate of the catalyst can be improved, the reaction is accelerated, and the single-tower carbon dioxide removal and gypsum mineralization process can be realized; the fluidized bed layer design is very favorable for the separation of gypsum particles and calcium carbonate particles, and the utilization rate of gypsum and the purity of calcium carbonate are obviously improved.
The input end of the ammonia supplementing pipe grid 5 is connected with an ammonia conveying pipe, and the input end of the gypsum slurry pipe grid 4 is connected with the bottom output end of the gypsum slurry tank 12; and the side wall of the upper part of the three-phase fluidization reaction zone 302 is provided with a calcium carbonate discharge port and is connected with a side cut inlet of the calcium carbonate cyclone 10.
Specifically, the calcium carbonate generating device 33 comprises a calcium carbonate cyclone 10 and a gypsum slurry tank 12; the calcium carbonate discharge port of the three-phase fluidization reaction zone 302 is provided with an absorption liquid discharge pump 8 and is connected with a side cut inlet of a calcium carbonate swirler 10, a solid phase outlet of the calcium carbonate swirler 10 is sequentially connected with an evaporation ammonia remover 9 and a vacuum belt conveyor 11, and a liquid phase outlet is connected with the top input end of a gypsum slurry tank 12; the output end of the bottom of the gypsum slurry tank 12 is connected with the input end of the gypsum slurry pipe grid 4 through a gypsum replenishing pump 16; wherein, the calcium carbonate solid that vacuum belt feeder 11 filters out returns desulfurization system as the desulfurization raw materials, forms cyclic utilization system. Meanwhile, a desulfurized gypsum slurry pipe 13 is connected to the side wall of the gypsum slurry tank 12 for supplementing gypsum slurry.
An absorption liquid discharge pump 8 pumps out absorption liquid from the upper part of a fluidized bed layer, the absorption liquid enters a calcium carbonate cyclone 10 for layering, slurry at the bottom of the calcium carbonate cyclone 10 contains unreacted gypsum particles, the slurry enters a gypsum slurry tank 12 through a liquid phase outlet and returns to the fluidized bed layer for continuous reaction, slurry at the upper part separated by the calcium carbonate cyclone 10 enters an ammonia evaporator 9 for removing ammonia, specifically, the ammonia removed by the evaporator 9 is input into the input end of an ammonia supplementing pipe grid 5 through an ammonia input pipe for recycling ammonia gas, meanwhile, the ammonia input pipe is also connected with an ammonia tank 15, and an ammonia outlet of the ammonia tank 15 is provided with an ammonia supplementing pump 14 for adjusting the pH value in a three-phase fluidized reaction zone 302; a solid phase outlet of the evaporator 9 is connected with a vacuum belt conveyor 11, solid filtered by the vacuum belt conveyor 11 is calcium carbonate solid, and filtrate enters a slurry pool of an ammonium sulfate concentration spraying area 301 through a filtrate pump 17; the cost can be saved, and the utilization rate is improved.
The demisting zone 303 is provided with a demister 2 and a process water spraying layer 1 from bottom to top along the height direction in sequence, so that a very small number of escaping harmful substances can be filtered.
The utility model relates to a direct mineralization flue gas carbon dioxide system based on three-phase fluidized bed is when using, and flue gas after the desulfurization gets into ammonium sulfate spray zone 301 by three-phase fluidized bed absorption tower 30 lower part desulfurization flue gas entry, with the ammonium sulfate solution countercurrent contact that the circulation sprayed, utilizes the waste heat of desulfurization flue gas, realizes constantly evaporative concentration to ammonium sulfate solution, simultaneously, the flue gas is cooled down to 20 ℃ -30 ℃,
the heat release desulfurization flue gas passes through the gas distribution plate 6 and enters a three-phase fluidization reaction zone 302, the zone is in a gas-liquid-solid three-phase fluidization state, the gas component participating in chemical reaction in the heat release desulfurization flue gas is carbon dioxide in the flue gas, the liquid phase component is ammonia water supplemented through an ammonia supplementing pipe grid 5, and the solid phase component is gypsum particles supplemented through a gypsum slurry pipe grid 4; specifically, when the heat-releasing desulfurization flue gas passes through the gas distribution plate 6, the gas flow speed is high, bubbles are formed, the bubbles and gypsum slurry are strongly mixed, the gas-liquid-solid reaction can be accelerated by the fluidization rolling, and the chemical reaction is CO2Ammonia and gypsum to produce ammonium sulfate and calcium carbonate, the reaction equation is as follows:
CO2+2NH3+CaSO4·2H2O→(NH4)2SO4+CaCO3↓+2H2O
because the density of the calcium carbonate particles is less than that of the gypsum particles, the bottom of the gas-liquid-solid three-phase fluidized bed layer is enriched in the density of the gypsum particles, and the upper layer is enriched in the generated calcium carbonate particles; carbon dioxide in the flue gas is removed in the three-phase fluidized reaction zone 302 to form clean flue gas, and the clean discharge is realized after the clean flue gas passes through the demister 2 and the process water spray layer 1.
The absorption liquid discharge pump 8 pumps calcium carbonate particles out of the upper part of the fluidized bed layer, the calcium carbonate particles enter a calcium carbonate cyclone 10 for layering, slurry at the bottom of the calcium carbonate cyclone 10 contains unreacted gypsum particles, the slurry enters a gypsum slurry tank 12 and returns to the fluidized bed layer for continuous reaction, slurry at the upper part separated by the calcium carbonate cyclone 10 enters an ammonia evaporator 9 for removing ammonia, the slurry enters a vacuum belt conveyor 11 for filtration to obtain calcium carbonate solid, and the filtrate enters a slurry tank of an ammonium sulfate concentration spraying area 301 through a filtrate pump 17.
In the ammonium sulfate crystallization generator 31, a solid-containing slurry pool at the bottom of the three-phase fluidized bed absorption tower 30 is pumped into the ammonium sulfate cyclone 18 for layering through an ammonium sulfate discharge pump 21, slurry at the bottom of the ammonium sulfate cyclone 18 enters a centrifuge 20 for separating solid ammonium sulfate, and filtrate of the centrifuge 20 and slurry of the ammonium sulfate cyclone 18 are pumped back to the slurry pool at the bottom of the tower through a reflux pump 19 for recycling.
Specifically, the pH of the slurry in the three-phase fluidized reaction zone 302 in the three-phase fluidized-bed absorption tower 30 is controlled by the ammonia supply pump 14, and the pH is controlled within the range of 8-10.
Specifically, the heat source in the ammonia evaporator 9 is one of hot flue gas or hot steam, wherein the temperature of the ammonia removing slurry in the ammonia evaporator 9 is controlled between 50 ℃ and 70 ℃ due to the instability of calcium sulfate.
Specifically, when the solid content in the ammonium sulfate slurry in the ammonium sulfate concentration spraying region 301 is greater than 10%, the ammonium sulfate discharge pump 21 is started to pump the ammonium sulfate solution into the ammonium sulfate crystallization generation device 31, so as to realize separation and crystallization of the ammonium sulfate solution.
Claims (8)
1. A system for directly mineralizing flue gas carbon dioxide based on a three-phase fluidized bed is characterized by comprising a three-phase fluidized bed absorption tower (30), an ammonium sulfate crystallization generation device (31) and a calcium carbonate generation device (33);
the calcium carbonate generating device (33) comprises a calcium carbonate cyclone (10), a gypsum slurry tank (12) and an ammonia conveying pipe;
the three-phase fluidized bed absorption tower (30) is sequentially provided with an ammonium sulfate concentration spraying zone (301), a three-phase fluidized reaction zone (302) and a demisting zone (303) from bottom to top;
a slurry pool is arranged at the bottom of the ammonium sulfate concentration spraying area (301), and a concentration spraying layer (7) is arranged at the top; the slurry pool is connected with an ammonium sulfate crystallization generating device (31);
the bottom of the three-phase fluidization reaction zone (302) is sequentially provided with a gas distribution plate (6), an ammonia supplementing pipe grid (5) and a gypsum slurry pipe grid (4) from bottom to top, an outlet of the ammonia supplementing pipe grid (5) is vertically downward, an input end of the ammonia supplementing pipe grid is connected to an ammonia conveying pipe, an outlet of the gypsum slurry pipe grid (4) is vertically upward, and an input end of the gypsum slurry pipe grid is connected with an output end at the bottom of a gypsum slurry tank (12); and the side wall of the upper part of the three-phase fluidization reaction zone (302) is provided with a calcium carbonate outlet and is connected to a side cut-in port of the calcium carbonate cyclone (10);
the demisting zone (303) is sequentially provided with a demister (2) and a process water spraying layer (1) from bottom to top.
2. The three-phase fluidized bed based direct mineralization flue gas carbon dioxide system of claim 1, wherein the slurry tank is located below a desulfurized flue gas inlet.
3. The three-phase fluidized bed-based direct mineralization flue gas carbon dioxide system of claim 1, wherein the ammonium sulfate crystallization generation device (31) comprises an ammonium sulfate discharge pump (21), an ammonium sulfate cyclone (18) and a centrifuge (20);
the side cut inlet of the ammonium sulfate cyclone (18) is connected with the ammonium sulfate crystallization outlet of the slurry pool through an ammonium sulfate discharge pump (21), and the bottom outlet is connected with the input end of a centrifuge (20);
the liquid phase outlet of the centrifuge (20) is combined with the top outlet of the ammonium sulfate cyclone (18) and is connected to the ammonium sulfate slurry return port of the slurry pool through a return pump (19).
4. The system for directly mineralizing flue gas and carbon dioxide based on the three-phase fluidized bed as recited in claim 1, wherein the outlet at the top of the calcium carbonate cyclone (10) is connected with the evaporation ammonia remover (9) and the vacuum belt conveyor (11) in sequence, and the outlet at the bottom is connected with the input at the top of the gypsum slurry tank (12).
5. The system for directly mineralizing flue gas and carbon dioxide based on the three-phase fluidized bed according to claim 4, wherein an ammonia outlet of the ammonia remover (9) is connected to an ammonia conveying pipe, and a solid phase outlet is connected to a vacuum belt conveyor (11).
6. The system for directly mineralizing flue gas and carbon dioxide based on the three-phase fluidized bed as recited in claim 1 or 5, wherein the input end of the ammonia conveying pipe is connected with an ammonia tank (15).
7. The system for directly mineralizing flue gas and carbon dioxide based on the three-phase fluidized bed according to claim 4, wherein a filtrate outlet of the vacuum belt conveyor (11) is connected to a slurry pool through a filtrate pump (17).
8. The system for directly mineralizing flue gas carbon dioxide based on the three-phase fluidized bed as recited in claim 1, wherein a desulfurized gypsum slurry pipe (13) is connected to the side wall of the gypsum slurry tank (12) for supplementing gypsum slurry.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121253082.2U CN214809744U (en) | 2021-06-04 | 2021-06-04 | System for directly mineralizing flue gas carbon dioxide based on three-phase fluidized bed |
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| CN202121253082.2U CN214809744U (en) | 2021-06-04 | 2021-06-04 | System for directly mineralizing flue gas carbon dioxide based on three-phase fluidized bed |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114452790A (en) * | 2022-01-28 | 2022-05-10 | 嘉兴市碳捕手科技有限责任公司 | Method for absorbing and mineralizing carbon dioxide in waste gas |
| CN116116185A (en) * | 2023-01-31 | 2023-05-16 | 西安热工研究院有限公司 | System and method for directly mineralizing flue gas carbon dioxide by using desulfurization gypsum |
-
2021
- 2021-06-04 CN CN202121253082.2U patent/CN214809744U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114452790A (en) * | 2022-01-28 | 2022-05-10 | 嘉兴市碳捕手科技有限责任公司 | Method for absorbing and mineralizing carbon dioxide in waste gas |
| CN116116185A (en) * | 2023-01-31 | 2023-05-16 | 西安热工研究院有限公司 | System and method for directly mineralizing flue gas carbon dioxide by using desulfurization gypsum |
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