CN113289452A - Flue gas carbon dioxide recovery process - Google Patents
Flue gas carbon dioxide recovery process Download PDFInfo
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- CN113289452A CN113289452A CN202110719538.8A CN202110719538A CN113289452A CN 113289452 A CN113289452 A CN 113289452A CN 202110719538 A CN202110719538 A CN 202110719538A CN 113289452 A CN113289452 A CN 113289452A
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- flue gas
- carbon dioxide
- adsorption tower
- adsorption
- recovery process
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 140
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 239000003546 flue gas Substances 0.000 title claims abstract description 84
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 70
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 70
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 238000001179 sorption measurement Methods 0.000 claims abstract description 121
- 238000003795 desorption Methods 0.000 claims abstract description 30
- 150000001412 amines Chemical class 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims abstract description 22
- 239000007787 solid Substances 0.000 claims abstract description 22
- 239000000428 dust Substances 0.000 claims abstract description 10
- 238000003860 storage Methods 0.000 claims abstract description 8
- 238000001816 cooling Methods 0.000 claims description 15
- 239000003463 adsorbent Substances 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 7
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000004568 cement Substances 0.000 claims description 4
- 125000000524 functional group Chemical group 0.000 claims description 3
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 3
- 238000012824 chemical production Methods 0.000 claims description 2
- 229920006037 cross link polymer Polymers 0.000 claims description 2
- 239000002861 polymer material Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 29
- 239000000779 smoke Substances 0.000 description 4
- 238000000605 extraction Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- -1 power plants Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Images
Classifications
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/20—Organic adsorbents
- B01D2253/202—Polymeric adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
-
- 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]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a flue gas carbon dioxide recovery process, wherein flue gas flows through a dust removal device, is introduced into an adsorption tower loaded with a solid amine adsorption material from the bottom, is then discharged from the top of the adsorption tower, when the concentration of carbon dioxide in the flue gas discharged from the top of the adsorption tower is greater than a preset value, the introduction of the flue gas into the adsorption tower is stopped, a gas outlet at the top of the adsorption tower is closed, a heat source is introduced into the adsorption tower from the bottom, after a preset desorption time, the introduction of the heat source into the adsorption tower is stopped, and then the carbon dioxide desorbed from the adsorption tower is extracted from the gas outlet and stored in a carbon dioxide storage tank. The flue gas carbon dioxide recovery process provided by the invention has the advantages of low energy consumption and small occupied area, and is beneficial to reducing the enterprise cost.
Description
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to a flue gas carbon dioxide recovery process.
Background
China is a large carbon dioxide emission country, about 60-70% of China is from industrial combustion, including industrial emissions such as cement, power plants, steel smelting and the like, flue gas refers to gaseous substances which are generated when fossil fuels such as coal and the like are combusted and pollute the environment, the main components of the flue gas include carbon dioxide, nitrogen, water vapor, sulfides and the like, and the carbon dioxide occupies most of the flue gas.
In order to reduce the carbon emission per unit GDP, carbon dioxide needs to be captured from flue gas, and at present, enterprises generally capture the carbon dioxide in the flue gas by using liquid organic amine, but the process has the following disadvantages: the organic amine has high viscosity and needs to be diluted by water for use, the mass fraction of the solute is generally 15-20%, and a large amount of heat is absorbed by the solvent in the regeneration process, so that the regeneration energy consumption is greatly increased; the auxiliary equipment is more, and the occupied area is large. Therefore, how to provide a flue gas carbon dioxide recovery process with low energy consumption and small occupied area becomes a technical problem to be solved urgently by the technical personnel in the field.
Disclosure of Invention
In view of the above, the invention provides a flue gas carbon dioxide recovery process, which has the advantages of low energy consumption and small occupied area and is beneficial to reducing the enterprise cost.
In order to achieve the purpose, the invention provides the following technical scheme:
a flue gas carbon dioxide recovery process comprises the steps that flue gas flows through a dust removal device, then enters an adsorption tower loaded with a solid amine adsorption material from the bottom, then is discharged from the top of the adsorption tower, when the concentration of carbon dioxide in the flue gas discharged from the top of the adsorption tower is larger than a preset value, the flue gas is stopped from entering the adsorption tower, a gas outlet in the top of the adsorption tower is closed, a heat source is introduced into the adsorption tower from the bottom, after preset desorption time, the heat source is stopped from entering the adsorption tower, and then carbon dioxide desorbed from the adsorption tower is extracted from the gas outlet and stored in a carbon dioxide storage tank.
Alternatively, in the above flue gas carbon dioxide recovery process, the flue gas is generated from any one of industrial production activities of fossil energy combustion, cement production, chemical production, and refining production.
Optionally, in the flue gas carbon dioxide recovery process described above, the heat source is steam or hot air.
Optionally, in the flue gas carbon dioxide recovery process, air is introduced from the bottom of the adsorption tower while carbon dioxide desorbed from the inside of the adsorption tower is drawn out from the air outlet.
Optionally, in the flue gas carbon dioxide recovery process described above, the air is dedusted by a dedusting apparatus prior to being passed to the adsorption tower.
Alternatively, in the flue gas carbon dioxide recovery process described above, the solid amine adsorbent material is a class of macroporous, spherical divinylbenzene-based, cross-linked polymeric materials having primary amino functional groups.
Optionally, in the flue gas carbon dioxide recovery process, before the flue gas is reintroduced into the adsorption tower, condensed water produced during desorption is evacuated through a cooling valve located at the bottom of the adsorption tower.
Optionally, in the flue gas carbon dioxide recovery process, before the flue gas is introduced into the adsorption tower, air is introduced into the adsorption tower through the cooling valve and an adsorption fan connected to the gas outlet to cool the solid amine adsorption material.
Optionally, in the flue gas carbon dioxide recovery process described above, the flue gas is introduced from an enterprise's flue gas system, and flue gas discharged from the top of the adsorption tower is transported back to the flue gas system.
According to the technical scheme, in the flue gas carbon dioxide recovery process provided by the invention, the carbon dioxide is captured from the flue gas by using the solid amine adsorption material, then the carbon dioxide in the solid amine adsorption material is desorbed by using the heat source, and finally the gas carbon dioxide is stored in the storage tank. The solid amine adsorption material does not have the dilution requirement of liquid organic amine, so the energy consumption is greatly saved, the heat required by the regeneration of the solid amine adsorption material is lower, in addition, the solid adsorption material is loaded on the adsorption tower, so the arrangement of the adsorption tower is more flexible, the number of auxiliary equipment is less, the occupied area is favorably reduced, the adsorption tower can be separately dispersed and used, and the combined design can be carried out according to the requirement so as to achieve the large-scale and high-efficiency adsorption. In conclusion, the flue gas carbon dioxide recovery process provided by the invention has the advantages of low energy consumption and small occupied area, and is beneficial to reducing the enterprise cost.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic diagram of a flue gas carbon dioxide recovery process provided by an embodiment of the present invention.
Labeled as:
1. a dust removal device; 2. an adsorption inlet valve; 3. an adsorption tower; 4. an adsorption outlet valve; 5. an adsorption fan; 6. a heat source inlet valve; 7. a desorption outlet valve; 8. a desorption fan; 9. a dust removal device; 10. cooling the valve; 11. a thermometer.
Detailed Description
For the purpose of facilitating understanding, the present invention will be further described with reference to the accompanying drawings.
Referring to fig. 1, the flue gas carbon dioxide recovery process provided by the present invention is generally performed according to a production schedule cycle, and in each cycle, the flue gas carbon dioxide recovery process includes three stages, the first stage is an adsorption process, the second stage is a desorption process, and the third stage is a carbon dioxide collection process, which are described below.
An adsorption process: flue gas → dust collector 1 → adsorption inlet valve 2 → adsorption tower 3 → adsorption outlet valve 4 → adsorption fan 5 → flue gas exhaust system.
The inside of the adsorption tower 3 is loaded with solid amine adsorption material, flue gas flows through the dust removal device 1, then enters the adsorption tower 3 from the bottom, and is discharged from the top of the adsorption tower 3, in the process, the adsorption inlet valve 2 and the adsorption outlet valve 4 are opened, and the heat source inlet valve 6, the desorption outlet valve 7 and the cooling valve 10 are closed. It should be noted that the flue gas discharged from the top of the adsorption tower 3 can be either fed back to the flue gas discharge system as in the present embodiment, or discharged to other subsequent gas treatment equipment, or even to the atmosphere if the emission standards have been met. The hollow arrows in figure 1 indicate the gas flow direction in the fume extraction system, and as can be seen from figure 1, the flue gas extraction location of the fume extraction system is generally upstream of the flue gas return location. It should be noted that fig. 1 shows the smoke exhaust system using a diagram of the shape of the chimney, only for the sake of understanding, and does not mean that the gas taking point and the gas returning point of the flue gas are arranged on the smoke exhaust chimney, and in fact, the gas taking point and the gas returning point of the flue gas are usually arranged on the smoke duct before the chimney.
The term "flue gas" herein includes, but is not limited to, gases in the following cases: a. carbon dioxide-containing gas produced by fossil energy combustion or industrial combustion; b. gases containing carbon dioxide generated in industrial production processes such as cement production, steel smelting and the like; c. carbon dioxide-containing by-product gas generated in the process flow in the petroleum refining process; d. because of the process production requirements, a decarbonized gas is required.
The solid amine adsorption material can save energy consumption without dilution, can keep stronger adsorption capacity after being recycled for many times, and has obvious advantages compared with the traditional solid adsorption materials such as carbon-based adsorbents, activated alumina, zeolites and the like. In this example, the solid amine adsorbent material is a macroporous spherical divinylbenzene-based crosslinked polymer material with primary amino functional groups.
With the increase of the adsorption time, the carbon dioxide adsorbed by the solid amine adsorbing material gradually increases and gradually tends to be saturated in adsorption, the concentration of the carbon dioxide in the flue gas discharged from the top of the adsorption tower 3 gradually increases, when the concentration of the carbon dioxide is higher than a certain value (namely a set value), the adsorption fan 5 is turned off, the adsorption inlet valve 2 and the adsorption outlet valve 4 are closed, and then the next process, namely a desorption process, is carried out.
The set value of the carbon dioxide concentration may be set as needed, and for example, the concentration of carbon dioxide in the flue gas before entering the adsorption tower 3 may be set as the set value, which means that the desorption process is performed after the solid amine adsorbent is saturated in adsorption, or 95% of the concentration of carbon dioxide in the flue gas before entering the adsorption tower 3 may be set as the set value, which means that the desorption process is performed when the solid amine adsorbent is about to be saturated in adsorption.
A desorption process: heat source → heat source inlet valve 6 → adsorption tower 3.
When the concentration of carbon dioxide in the flue gas discharged from the top of the adsorption tower 3 is greater than a preset value, the introduction of the flue gas into the adsorption tower 3 is stopped, the gas outlet at the top of the adsorption tower 3 is closed, a heat source (including but not limited to steam, hot air and waste heat of enterprises) is introduced into the adsorption tower 3 from the bottom, and the heat source supplies heat to the solid amine adsorption material to heat the solid amine adsorption material, so that the carbon dioxide adsorbed on the solid amine adsorption material is desorbed. In this process, the heat source inlet valve 6 is opened, and the adsorption inlet valve 2, the adsorption outlet valve 4, the desorption outlet valve 7, and the cooling valve 10 are closed. The temperature inside the adsorption tower 3 is monitored in real time through a thermometer 11, and the heat source inlet valve 6 is closed when the temperature reaches a certain degree. Of course, a desorption time may be set, and when the opening time of the heat source inlet valve 6 reaches the desorption time, the heat source inlet valve 6 is closed, the introduction of the heat source into the adsorption tower is stopped, and then the next process, that is, the carbon dioxide collecting process is performed.
And (3) carbon dioxide collection process: adsorption tower 3 → desorption outlet valve 7 → desorption fan 8 → storage tank.
The carbon dioxide desorbed from the adsorption tower 3 is pumped out from the gas outlet at the top and then stored in the carbon dioxide storage tank, in the process, the desorption outlet valve 7 is opened, and the adsorption inlet valve 2, the adsorption outlet valve 4, the heat source inlet valve 6 and the cooling valve 10 are closed. It should be noted that, when the carbon dioxide is extracted from the air outlet of the adsorption tower 3, the cooling valve 10 may also be opened to introduce air, that is, the carbon dioxide collecting process is changed to: air → dust collector 9 → cooling valve 10 → adsorption tower 3 → desorption outlet valve 7 → desorption fan 8 → storage tank. The purpose of letting in air is to reduce the time that the evacuation carbon dioxide took, improves work efficiency, moreover, in order to ensure that the concentration of the carbon dioxide in the storage tank accords with target range value, the flow of air should not be too big, and cooling valve 10 need only slightly open. In addition, before the flue gas is re-introduced into the adsorption tower 3, the condensed water generated in the desorption process can be emptied through a cooling valve 10 located at the bottom of the adsorption tower 3. Solid-state amine adsorption material provides the heat by the heat source and carries out the desorption, and solid-state amine adsorption material's temperature is higher after the desorption, lets in the flue gas again to adsorption tower 3 before adsorbing, can drop the temperature to solid-state amine adsorption material through leading air in to adsorption tower 3 earlier through cooling valve 10 and adsorption fan 5, and the process of cooling is: air → dust removing device 9 → cooling valve 10 → adsorption tower 3 → adsorption outlet valve 4 → adsorption fan 5 → smoke evacuation system.
The flue gas carbon dioxide recovery process of the present invention performs well in the flue gas treatment of a power plant, effectively reducing the operating cost of the power plant, and the specific application thereof is described below. The flue gas source is the clean flue gas of the power plant after desulfurization, dust removal and denitration, various parameters of the flue gas are shown in table 1, technological parameters of the adsorption process are shown in table 2, and technological parameters of the desorption process are shown in table 3.
TABLE 1 flue gas parameters
TABLE 2 Process parameters for the adsorption Process
| Item | Numerical value | Unit of |
| Flue gas cooled temperature | ≤40 | ℃ |
| Adsorption air quantity | 60000 | m3/h |
| Loading of adsorbent | 100 | m3 |
| Flow rate of adsorption | 600 | BV/h |
| Average cycle adsorption time | 0.5 | h |
| Average periodic adsorption capacity | 4000 | kg |
TABLE 3 Process parameters for the desorption procedure
| Item | Numerical value | Unit of |
| Desorption heat source | 120 (power plant exhaust steam) | ℃ |
| Mean period desorption time | 0.5 | h |
| Mean concentration of desorption | >90 | ％ |
| Average periodic desorption amount | 3880 | kg |
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to the embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. A flue gas carbon dioxide recovery process is characterized in that flue gas flows through a dust removal device, then is introduced into an adsorption tower loaded with a solid amine adsorption material from the bottom, then is discharged from the top of the adsorption tower, when the concentration of carbon dioxide in the flue gas discharged from the top of the adsorption tower is larger than a preset value, the introduction of the flue gas into the adsorption tower is stopped, a gas outlet in the top of the adsorption tower is closed, a heat source is introduced into the adsorption tower from the bottom, after a preset desorption time, the introduction of the heat source into the adsorption tower is stopped, and then the carbon dioxide desorbed from the adsorption tower is extracted from the gas outlet and stored in a carbon dioxide storage tank.
2. The flue gas carbon dioxide recovery process of claim 1, wherein the flue gas is generated from any one of a fossil energy combustion, cement production, chemical production, and refinery production.
3. The flue gas carbon dioxide recovery process of claim 1, wherein the heat source is steam or hot air.
4. The flue gas carbon dioxide recovery process of claim 1, wherein air is introduced from the bottom of the adsorption tower while carbon dioxide desorbed from the inside of the adsorption tower is drawn out from the gas outlet.
5. The flue gas carbon dioxide recovery process of claim 4, wherein the air is dedusted by a dedusting apparatus prior to being passed to the adsorption tower.
6. The flue gas carbon dioxide recovery process of any one of claims 1 to 5, wherein the solid amine adsorption material is a macroporous, spherical divinylbenzene-based crosslinked polymer material having primary amino functional groups.
7. The flue gas carbon dioxide recovery process of claim 6, wherein condensed water produced during desorption is evacuated through a cooling valve located at the bottom of the adsorption column prior to reintroducing the flue gas to the adsorption column.
8. The flue gas carbon dioxide recovery process of claim 7, wherein the solid amine adsorbent material is cooled by introducing air into the adsorption tower through the cooling valve and an adsorption fan coupled to the air outlet prior to introducing the flue gas into the adsorption tower.
9. The flue gas carbon dioxide recovery process of claim 6, wherein the flue gas is introduced from a plant's flue gas system and flue gas exhausted from the top of the adsorption tower is transported back to the flue gas system.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114225629A (en) * | 2021-12-21 | 2022-03-25 | 天津工业大学 | A solid-state amine absorption system for CO2 abatement in confined rooms |
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