CN112870919A - Flue gas CO2Hypergravity regeneration energy-saving process for trapping system - Google Patents
Flue gas CO2Hypergravity regeneration energy-saving process for trapping system Download PDFInfo
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- CN112870919A CN112870919A CN202110004167.5A CN202110004167A CN112870919A CN 112870919 A CN112870919 A CN 112870919A CN 202110004167 A CN202110004167 A CN 202110004167A CN 112870919 A CN112870919 A CN 112870919A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
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- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
The application discloses flue gas CO2The capture system hypergravity regeneration energy-saving process comprises the following steps S1-S7. Provides a chemical absorption method for flue gas CO2The capture system adopts a coupled regeneration process of the hypergravity reactor, the solution boiler and the boiling liquid separator to replace the original regeneration process of the desorption tower and the boiler, so that the size of equipment is greatly reduced, and the capture system has the advantages of miniaturization, flexibility, high efficiency, small investment, skid-mounted equipment, modularization and the like, saves the investment cost and has obvious reduction of regeneration energy consumption; the chemical absorption method of the invention is used for flue gas CO2The coupled regeneration process of the 'super-gravity reactor, the solution boiler and the boiling liquid separator' of the trapping system reduces the medicament loss and the degradation and deterioration of the medicament, improves the recycling times of the chemical absorbent, meets the characteristics of low consumption, low emission and high efficiency of recycling economy, and achieves the purposes of recycling and reducing environmental pollution.
Description
Technical Field
The application relates to the technical field of flue gas capture systems, in particular to flue gas CO2The capture system hypergravity regeneration energy-saving process.
Background
In recent years, the atmospheric environment continues to deteriorate due to the combustion of fossil fuels, and the "greenhouse effect" caused thereby is becoming more and more serious to threaten human survival. CO22Not only are major contributors to greenhouse gases, their hazards last longer. To alleviate the effect of "greenhouse effect", the first solution to CO should be2The emission reduction and the recycling are realized.
Carbon Capture and sequestration&Storage, CCS) is a reduction in CO emitted into the atmosphere without reducing current fossil fuel usage2The most direct and effective way of gas quantity, and meanwhile, the CCS technology is one of the most important emission reduction technologies which are actively used for coping with climate change and ensuring the leading position of world clean energy in China, Britain, America, Japan and other countries at present. The method for separating carbon dioxide from flue gas by the CCS technology mainly comprises the following steps: membrane separation, physical adsorption, cryogenic distillation, absorption separation, and the like. CO capture by chemical absorption2The method is widely used due to the high absorption rate, high absorption efficiency, simple process and mature technology, and a plurality of demonstration evaluation projects are built at home and abroad.
However, current chemical absorption methods capture CO2The main disadvantage of the technology is the high energy consumption of the regeneration system, in order to reduce CO2Regeneration energy consumption and CO reduction2Trapping cost, and domestic and foreign scholars are continuously optimizing and developing the existing process to develop new CO2A trapping and regenerating process, so we propose a flue gas CO2The supergravity regeneration energy-saving process of trapping system is characterized by that it improves existent organic amine chemical absorption process, and adopts supergravity machine to replace conventional desorption tower to heat and regenerate absorption liquid so as to implement miniaturization of desorption system,Flexible, skid-mounted and modular.
Disclosure of Invention
The embodiment of the application provides flue gas CO2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
s1, after the flue gas from the coal-fired power plant is subjected to desulfurization, denitrification and dedusting by a deep purification tower, controlling the gas temperature to be 30-50 ℃;
s2, pressurizing the flue gas by a draught fan, then entering an absorption tower from bottom to top, entering a barren liquor absorbent into the absorption tower from top to bottom, and carrying out countercurrent contact on the barren liquor absorbent and the absorption tower to finish CO2The absorption process of (2);
s3, absorbing CO2Discharging the rich solution of the gas from the bottom of the absorption tower, feeding the cold rich solution pressurized by a rich solution pump into a lean rich solution heat exchanger for heat exchange, and spraying the cold rich solution into a supergravity reactor after heat exchange;
s4, making CO2Desorbing from the absorbent rapidly, feeding the desorbed regeneration gas into a gas-liquid separator through a regeneration gas outlet for separation to obtain product gas, pressurizing the desorbed barren solution by a barren solution outlet of the supergravity reactor through a barren solution pump, feeding the barren solution into a barren and rich solution heat exchanger for heat exchange and cooling, feeding the barren solution into a barren solution cooler for cooling, feeding the cooled barren solution into an absorption tower, and starting a new absorption process;
s5, when the step S4 is performed, part of the barren solution flows into the siphon solution boiler from the super-gravity reactor to the electric regulating valve on the pipeline branch of the barren solution pump to be heated;
s6, heated solution and CO desorbed in heating process2The gas-liquid two-phase mixture enters a boiling liquid separator from a boiling liquid outlet under the siphoning action of a solution boiling device for gas-liquid separation, and the separated desorption gas enters a super-gravity reactor from a gas outlet at the top of the boiling liquid separator;
s7, install the electrical control valve on the hypergravity reactor lean solution pump pipeline branch pipeline, the electrical control valve interlocks with the liquid level check out test set who installs on the boiling liquid separator, when the boiling liquid separator liquid level was too high, the electrical control valve aperture reduced, when the boiling liquid separator liquid level was too low, the electrical control valve aperture increased.
The embodiment of the application adopts the following technical scheme that in the step S1, after the flue gas is subjected to desulfurization, denitrification and dedusting by the deep purification tower, the gas temperature is controlled to be 40 ℃, and the deep purification tower is provided with the purification tower pump.
The technical scheme is adopted in the embodiment of the application, and a tail gas discharge port is arranged at the top of the absorption tower; the gas-liquid separator is provided with a product gas outlet and a first drain outlet; a rich liquid inlet and a regenerated gas outlet are formed in the supergravity reactor; the solution boiler is provided with a boiling liquid inlet and a second sewage outlet.
In the embodiment of the application, the following technical scheme is adopted, in step S3, the temperature of the cold rich liquid after being pressurized by the rich liquid pump is 50-55 ℃, and the temperature of the rich liquid after entering the lean rich liquid heat exchanger for heat exchange is 90-95 ℃.
In the embodiment of the application, the following technical scheme is adopted, and in step S3, after the cold rich liquid enters the lean rich liquid heat exchanger, the unique flow behavior of the multiphase flow system under the condition of supergravity is utilized to strengthen the relative speed and mutual contact between the phases and before the phases, so that the efficient mass and heat transfer process and the efficient chemical reaction process are realized.
In the embodiment of the application, the following technical scheme is adopted, in step S3, the temperature of the liquid after the desorbed barren solution enters the barren and rich solution heat exchanger for heat exchange and cooling is 55-65 ℃, and the temperature of the liquid after the liquid enters the barren solution cooler for cooling is 40-45 ℃.
In the embodiment of the application, the following technical scheme is adopted, and in step S5, the temperature of the lean solution is 100-110 ℃ after the lean solution flows into the siphon-type solution boiler to be heated.
The embodiment of the present application adopts the following technical solution, in step S5, the heating form of the solution boiler is set to be electric heating or steam heating.
In the embodiment of the present application, the following technical solution is adopted, and in step S6, the solution separated by the boiling liquid separator enters the solution boiler through the solution outlet at the bottom of the boiling liquid separator to continue circulating.
The embodiment of the present application adopts the following technical scheme that in step S7, the electric control valve is usedIs reduced and increased, thereby realizing the stable circulation of the boiling separation system, and the recycling of the absorbent lean and rich liquid enables CO2The absorption and desorption processes are continuously carried out.
The embodiment of the application adopts at least one technical scheme which can achieve the following beneficial effects:
1. the invention provides a chemical absorption method for flue gas CO2The capture system adopts a coupled regeneration process of the hypergravity reactor, the solution boiler and the boiling liquid separator to replace the original regeneration process of the desorption tower and the boiler, so that the size of equipment is greatly reduced, and the capture system has the advantages of miniaturization, flexibility, high efficiency, small investment, skid-mounted equipment, modularization and the like, saves the investment cost and has obvious reduction of regeneration energy consumption;
2. the chemical absorption method of the invention is used for flue gas CO2The coupled regeneration process of the 'super-gravity reactor, the solution boiler and the boiling liquid separator' of the trapping system reduces the medicament loss and the degradation and deterioration of the medicament, improves the recycling times of the chemical absorbent, meets the characteristics of low consumption, low emission and high efficiency of recycling economy, and achieves the purposes of recycling and reducing environmental pollution.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
FIG. 1 shows flue gas CO of the present invention2The structure schematic diagram of the capture system hypergravity regeneration energy-saving process;
FIG. 2 shows the flue gas CO of the invention2A process flow chart of the hypergravity regeneration energy-saving process of the trapping system.
In the figure: 1. a deep purification tower; 2. a purge column pump; 3. an absorption tower; 4. an induced draft fan; 5. a tail gas discharge port; 6. a rich liquor pump; 7. a lean liquid cooler; 8. a lean-rich liquid heat exchanger; 9. a barren liquor pump; 10. a hypergravity reactor; 11. a solution boiler; 12. a boiling liquid separator; 13. a gas-liquid separator; 14. a product gas outlet; 15. a first drain port; 16. a rich liquid inlet; 17. a regeneration gas outlet; 18. a barren liquor outlet; 19. a boiling liquid outlet; 20. a boiling liquid inlet; 21. a liquid level detection device; 22. an electric control valve; 23. A second sewage draining outlet; 24. a gas outlet; 25. and (6) solution outlet.
Detailed Description
In order to make the objects, technical solutions and advantages of the present application more apparent, the technical solutions of the present application will be described in detail and completely with reference to the following specific embodiments of the present application and the accompanying drawings. It should be apparent that the described embodiments are only some of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
The technical solutions provided by the embodiments of the present application are described in detail below with reference to the accompanying drawings.
Examples
Flue gas CO2The hypergravity regeneration energy-saving process of the trapping system comprises the following steps:
s1, after the flue gas from the coal-fired power plant is subjected to desulfurization, denitrification and dust removal by the deep purification tower 1, controlling the gas temperature to be 30-50 ℃;
s2, pressurizing the flue gas by a draught fan 4, then entering an absorption tower 3 from bottom to top, entering a barren liquor absorbent into the absorption tower 3 from top to bottom, and carrying out countercurrent contact on the barren liquor absorbent and the absorption tower 3 to finish CO2The absorption process of (2);
s3, absorbing CO2The rich solution of the gas is discharged from the bottom of the absorption tower, the cold rich solution pressurized by the rich solution pump 6 enters the lean rich solution heat exchanger 8 for heat exchange, and the cold rich solution is sprayed into the supergravity reactor 10 after heat exchange;
s4, making CO2Desorbing from the absorbent rapidly, feeding the desorbed regeneration gas into a gas-liquid separator 13 via a regeneration gas outlet 17 for separation to obtain product gas, pressurizing the desorbed barren solution from a barren solution outlet 18 of a supergravity reactor 10 via a barren solution pump 9, feeding the barren solution into a barren and rich solution heat exchanger 8 for heat exchange and cooling, feeding the barren solution into a barren solution cooler 7 for cooling, feeding the cooled barren solution into an absorption tower 3, and starting a new absorption process；
S5, step S4, part of the barren solution flows into the siphon solution boiler 11 from the high gravity reactor 10 to the electric regulating valve 22 on the pipeline branch of the barren solution pump 9 for heating;
s6, heated solution and CO desorbed in heating process2The gas-liquid two-phase mixture enters the boiling liquid separator 12 from the boiling liquid outlet 19 for gas-liquid separation under the siphoning action of the solution boiler 11, and the separated desorption gas enters the super-gravity reactor 10 from the gas outlet 24 at the top of the boiling liquid separator 12;
s7, installing an electric control valve 22 on a pipeline branch line of a lean solution pump 9 of the supergravity reactor 10, interlocking the electric control valve 22 with a liquid level detection device 21 installed on a boiling liquid separator 12, reducing the opening degree of the electric control valve 22 when the liquid level of the boiling liquid separator 12 is too high, and increasing the opening degree of the electric control valve 22 when the liquid level of the boiling liquid separator 12 is too low.
In step S1, after the flue gas is desulfurized, denitrated and dedusted by the deep purification tower 1, the gas temperature is controlled to be 40 ℃, and the deep purification tower 1 is provided with the purification tower pump 2. The top of the absorption tower 3 is provided with a tail gas discharge port 5; the gas-liquid separator 13 is provided with a product gas outlet 14 and a first sewage discharge port 15; the supergravity reactor 10 is provided with a rich liquid inlet 16 and a regenerated gas outlet 17; the solution boiler 11 is provided with a boiling liquid inlet 20 and a second sewage outlet 23.
In step S3, the temperature of the cold rich liquid pressurized by the rich liquid pump 6 is 50 to 55 ℃, and the temperature of the rich liquid entering the lean rich liquid heat exchanger 8 for heat exchange is 90 to 95 ℃. In step S3, after the cold rich liquid enters the lean rich liquid heat exchanger 8, the unique flow behavior of the multiphase flow system under the condition of supergravity is utilized to enhance the relative speed and mutual contact between the phases, thereby realizing the efficient mass and heat transfer process and the efficient chemical reaction process.
In step S3, the temperature of the lean solution after the desorbed lean solution enters the lean-rich solution heat exchanger 8 for heat exchange and cooling is 55 to 65 ℃, and the temperature of the solution after the lean solution enters the lean solution cooler 7 for cooling is 40 to 45 ℃.
In step S5, the lean solution flows into the siphon-type solution boiler 11 to be heatedThe post-temperature is between 100 and 110 ℃. The solution boiler 11 is heated in the form of electric heating or steam heating. In step S6, the solution separated by the boiling liquid separator 12 is introduced into the solution boiler 11 through the solution outlet 25 at the bottom of the boiling liquid separator 12 to be continuously circulated. In step S7, the opening degree of the electric control valve 22 is decreased and increased to realize a stable circulation of the 12-boil-off separation system, and the circulation of the absorbent rich-lean solution causes CO to circulate2The absorption and desorption processes are continuously carried out.
In conclusion, the invention integrates the supergravity reactor 10, the solution boiler 11, the gas-liquid separator 13 and the interlocking automatic control unit system, and can effectively reduce the flue gas CO by the chemical absorption method2The invention provides a chemical absorption method for flue gas CO, and relates to the regeneration energy consumption of a trapping system2The capture system adopts a coupled regeneration process of the hypergravity reactor, the solution boiler and the boiling liquid separator to replace the original regeneration process of the desorption tower and the boiler, so that the size of equipment is greatly reduced, and the capture system has the advantages of miniaturization, flexibility, high efficiency, small investment, skid-mounted equipment, modularization and the like, saves the investment cost and has obvious reduction of regeneration energy consumption; chemical absorption method for flue gas CO2The coupled regeneration process of the capture system of the hypergravity reactor, the solution boiler and the boiling liquid separator reduces the medicament loss and the degradation and deterioration of the medicament, improves the recycling times of the chemical absorbent, meets the characteristics of low consumption, low discharge and high efficiency of recycling economy, and achieves the aims of recycling and reducing environmental pollution
It should also be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises the element.
The above description is only an example of the present application and is not intended to limit the present application. Various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the scope of the claims of the present application.
Claims (10)
1. Flue gas CO2The hypergravity regeneration energy-saving process of the trapping system is characterized by comprising the following steps:
s1, after the flue gas from the coal-fired power plant is subjected to desulfurization, denitrification and dust removal by the deep purification tower (1), controlling the gas temperature to be 30-50 ℃;
s2, pressurizing the flue gas by a draught fan (4), then entering the absorption tower (3) from bottom to top, entering the barren liquor absorbent into the absorption tower (3) from top to bottom, and making the barren liquor absorbent and the absorption tower in countercurrent contact to finish CO2The absorption process of (2);
s3, absorbing CO2The rich solution of the gas is discharged from the bottom of the absorption tower, the cold rich solution pressurized by the rich solution pump (6) enters a lean rich solution heat exchanger (8) for heat exchange, and the cold rich solution is sprayed into a supergravity reactor (10) after heat exchange;
s4, making CO2Desorbing from an absorbent rapidly, feeding desorbed regeneration gas into a gas-liquid separator (13) through a regeneration gas outlet (17) for separation to obtain product gas, pressurizing the desorbed barren solution by a barren solution outlet (18) of a supergravity reactor (10) through a barren solution pump (9), feeding the barren solution into a barren and rich solution heat exchanger (8) for heat exchange and cooling, then feeding the barren solution into a barren solution cooler (7) for cooling, feeding the cooled barren solution into an absorption tower (3), and starting a new absorption process;
s5, when the step S4 is performed, part of the barren solution flows into the siphon solution boiler (11) from the hypergravity reactor (10) to the electric regulating valve (22) on the pipeline branch of the barren solution pump (9) to be heated;
s6, heated solution and CO desorbed in heating process2The gas-liquid two-phase mixture enters the boiling liquid separator (12) from the boiling liquid outlet (19) for gas-liquid separation under the siphoning action of the solution boiler (11), and the desorbed gas after separation enters the gas outlet (24) at the top of the boiling liquid separator (12)A hypergravity reactor (10);
s7, an electric regulating valve (22) is installed on a pipeline branch pipeline of a lean solution pump (9) of the supergravity reactor (10), the electric regulating valve (22) is interlocked with a liquid level detection device (21) installed on a boiling liquid separator (12), when the liquid level of the boiling liquid separator (12) is too high, the opening degree of the electric regulating valve (22) is reduced, and when the liquid level of the boiling liquid separator (12) is too low, the opening degree of the electric regulating valve (22) is increased.
2. The flue gas CO of claim 12The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in the step S1, after the flue gas is subjected to desulfurization, denitrification and dedusting by the deep purification tower (1), the gas temperature is controlled to be 40 ℃, and the deep purification tower (1) is provided with a purification tower pump (2).
3. The flue gas CO of claim 22The super-gravity regeneration energy-saving process of the trapping system is characterized in that: a tail gas discharge port (5) is formed in the top of the absorption tower (3); the gas-liquid separator (13) is provided with a product gas outlet (14) and a first drain outlet (15); a rich liquid inlet (16) and a regenerated gas outlet (17) are arranged on the supergravity reactor (10); the solution boiler (11) is provided with a boiling liquid inlet (20) and a second sewage draining outlet (23).
4. The flue gas CO of claim 32The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in step S3, the temperature of the cold rich liquid pressurized by the rich liquid pump (6) is 50-55 ℃, and the temperature of the rich liquid entering the lean rich liquid heat exchanger (8) for heat exchange is 90-95 ℃.
5. The hypergravity regeneration energy-saving process of the flue gas CO2 capture system according to claim 4, characterized in that: in step S3, after the cold rich liquid enters the lean rich liquid heat exchanger (8), the unique flow behavior of the multiphase flow system under the condition of supergravity is utilized to strengthen the relative speed and mutual contact between the phases, thereby realizing the efficient mass and heat transfer process and the efficient chemical reaction process.
6. The flue gas CO of claim 52The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in step S3, the temperature of the lean solution after the desorbed lean solution enters the lean-rich solution heat exchanger (8) for heat exchange and cooling is 55-65 ℃, and the temperature of the solution after the lean solution enters the lean solution cooler (7) for cooling is 40-45 ℃.
7. The flue gas CO of claim 62The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in step S5, the lean solution is heated in the siphon-type solution boiler (11) at 100 to 110 ℃.
8. The flue gas CO of claim 72The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in step S5, the heating form of the solution boiler (11) is set to be electric heating or steam heating.
9. The flue gas CO of claim 82The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in step S6, the solution separated by the boiling liquid separator (12) enters the solution boiler (11) through the solution outlet (25) at the bottom of the boiling liquid separator (12) and continues to circulate.
10. The flue gas CO of claim 92The super-gravity regeneration energy-saving process of the trapping system is characterized in that: in step S7, the opening degree of the electric control valve (22) is reduced and increased to realize a stable circulation of the 12 boiling separation system, and the circulation of the absorbent lean and rich liquid enables the CO to be recycled2The absorption and desorption processes are continuously carried out.
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Cited By (5)
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| CN114028903A (en) * | 2021-10-22 | 2022-02-11 | 国能国华(北京)电力研究院有限公司 | System for catching carbon dioxide in flue gas |
| CN114191942A (en) * | 2021-09-28 | 2022-03-18 | 广东捷玛节能科技股份有限公司 | Flue gas CO2Hypergravity regeneration energy-saving process for trapping system |
| CN114414301A (en) * | 2021-11-26 | 2022-04-29 | 国家能源集团新能源技术研究院有限公司 | Tower liquid sampling device and packed tower |
| CN115040991A (en) * | 2022-07-06 | 2022-09-13 | 浙江浩普环保工程有限公司 | Carbon dioxide capture system |
| CN116585868A (en) * | 2023-03-13 | 2023-08-15 | 中国矿业大学 | Integrated process for capturing carbon dioxide and preparing urea |
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