CN114788997A - Flue gas CO by chemical absorption method 2 Trapping system - Google Patents
Flue gas CO by chemical absorption method 2 Trapping system Download PDFInfo
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 69
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 239000003546 flue gas Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000000126 substance Substances 0.000 title claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 154
- 239000012528 membrane Substances 0.000 claims abstract description 118
- 238000000909 electrodialysis Methods 0.000 claims abstract description 89
- 239000003513 alkali Substances 0.000 claims abstract description 87
- 239000002253 acid Substances 0.000 claims abstract description 81
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 74
- 238000003795 desorption Methods 0.000 claims abstract description 59
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 37
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 37
- 238000011084 recovery Methods 0.000 claims abstract description 9
- 239000002585 base Substances 0.000 claims description 16
- 238000005341 cation exchange Methods 0.000 claims description 12
- 239000003011 anion exchange membrane Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 239000003518 caustics Substances 0.000 claims description 8
- 230000008569 process Effects 0.000 abstract description 20
- 230000008929 regeneration Effects 0.000 abstract description 19
- 238000011069 regeneration method Methods 0.000 abstract description 19
- 238000005265 energy consumption Methods 0.000 abstract description 12
- 230000002745 absorbent Effects 0.000 abstract description 9
- 239000002250 absorbent Substances 0.000 abstract description 9
- 238000005262 decarbonization Methods 0.000 abstract description 7
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 46
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid group Chemical group S(O)(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 14
- 239000007789 gas Substances 0.000 description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 9
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 9
- 235000011114 ammonium hydroxide Nutrition 0.000 description 9
- 238000010586 diagram Methods 0.000 description 7
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- -1 alcohol amine Chemical class 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 4
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 3
- 150000001450 anions Chemical class 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 230000005012 migration Effects 0.000 description 3
- 238000013508 migration Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 239000012527 feed solution Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- MKKVKFWHNPAATH-UHFFFAOYSA-N [C].N Chemical compound [C].N MKKVKFWHNPAATH-UHFFFAOYSA-N 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
- B01D53/965—Regeneration, reactivation or recycling of reactants including an electrochemical process step
-
- 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
- B01D53/1418—Recovery of products
-
- 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
-
- 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
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/73—After-treatment of removed components
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/46—Apparatus therefor
- B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
-
- 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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Abstract
The application discloses a chemical absorption method for flue gas CO 2 The trapping system comprises an absorption tower, a desorption reactor and a bipolar membrane electrodialysis device. The flue gas enters an absorption tower and reacts with alkali liquor to generate a decarbonized product, so that the absorption of carbon dioxide is realized. Strong acid solution is filled in the desorption reactor, the decarbonized product enters the desorption reactor to react with the strong acid to generate carbon dioxide and feed liquid, and the carbon dioxide enters a carbon dioxide recovery system; the feed liquid enters a bipolar membrane electrodialysis device to generate acid liquorAnd alkali liquor to complete the regeneration of the absorbent. The decarbonization product reacts with the strong acid in the desorption reactor to remove carbonate of the decarbonization product, the feed liquid is regenerated in the bipolar membrane electrodialysis equipment to generate the strong acid and alkali liquor, and no bubbles are generated in the regeneration process of the absorbent, so that the conductivity of the bipolar membrane electrodialysis equipment is guaranteed, the efficiency of the bipolar membrane electrodialysis equipment is obviously improved, and the energy consumption of a system is reduced.
Description
Technical Field
The application relates to the technical field of environmental protection equipment, in particular to a chemical absorption method for flue gas CO 2 A capture system.
Background
At present, industrial flue gas CO 2 The capture mainly adopts a chemical absorption capture process, namely, carbon dioxide in the flue gas is absorbed by adopting chemical reaction, and then CO is decomposed from decarbonization products by heating 2 And to CO 2 The absorbent is collected and regenerated at the same time, so that the absorbent can be recycled. Common absorbents include alkaline substances such as alcohol amine solution (such as MEA), ammonia water, potassium carbonate, sodium carbonate, etc. But existing CO 2 The absorption and trapping process generally has the problems of complex system, high energy consumption, poor economy, easy volatilization and escape of the absorbent, easy decomposition, easy corrosion of equipment and the like.
In recent years, researchers have proposed that the regeneration of the decarbonized product is realized by using the principle that bipolar membrane electrodialysis is utilized to convert a salt solution into acid and alkali. Flue gas CO (carbon monoxide) adopting bipolar membrane electrodialysis as chemical absorption method 2 Compared with thermal regeneration, the regeneration process of the capture system can be operated at normal temperature and normal pressure, can avoid the problems of product crystallization, carbon dioxide yield reduction and the like caused by reaction among regeneration gases, and is undoubtedly a choice with good development potential. However, the bipolar membrane electrodialysis regeneration process has the problem of high energy consumption, so that the bipolar membrane electrodialysis regeneration process is difficult to popularize.
Therefore, how to reduce the energy consumption of the regeneration process in the carbon dioxide capture process is a technical problem which needs to be solved urgently by the technical personnel in the field.
Disclosure of Invention
The application aims to provide a chemical absorption method for flue gas CO 2 The capture system is provided with a desorption reactor, the decarbonized product reacts with strong acid in the desorption reactor to generate carbon dioxide and feed liquid with strong acid salt, and the feed liquid is decomposed in the bipolar membrane electrodialysis equipment, so that the decarbonized product is prevented from being decomposed in the bipolar membrane electrodialysis equipmentThe gas bubbles are directly decomposed to generate the gas bubbles, so that the resistance increase caused by the gas bubbles is avoided, the regeneration efficiency of the absorbent is improved, and the energy consumption of a system is reduced.
In order to achieve the purpose, the application provides a flue gas CO chemical absorption method 2 A capture system, comprising:
the absorption tower is used as a reaction site for absorbing carbon dioxide by using alkali liquor;
a desorption reactor connected to the bottom of the absorption tower to accommodate the decarbonized product generated in the absorption tower and the acid solution reacted with the decarbonized product and serve as a reaction site for the desorption of the decarbonized product, the top of the desorption reactor being connected to a carbon dioxide recovery system;
and the bipolar membrane electrodialysis equipment is connected with the desorption reactor and is used for decomposing the feed liquid generated by the desorption reactor, and a solution pump for conveying the feed liquid is arranged between the bipolar membrane electrodialysis equipment and the desorption reactor.
In some embodiments, the bipolar membrane electrodialysis apparatus includes a three-compartment bipolar membrane electrodialysis device, the middle of the three-compartment bipolar membrane electrodialysis device is a first feed liquid chamber, two sides of the first feed liquid chamber are a first acid chamber and a first alkali chamber respectively, one side of the first alkali chamber, which is away from the first feed liquid chamber, is a first cathode chamber, one side of the first acid chamber, which is away from the first feed liquid chamber, is a first anode chamber, an anion exchange membrane is arranged between the first feed liquid chamber and the first acid chamber, a cation exchange membrane is arranged between the first feed liquid chamber and the first alkali chamber, a bipolar membrane is arranged between the first cathode chamber and the first alkali chamber, a bipolar membrane is also arranged between the first anode chamber and the first acid chamber, and the solution pump is communicated with the first feed liquid chamber.
In some embodiments, the bipolar membrane electrodialysis apparatus comprises a two-chamber bipolar membrane electrodialysis device, a second feed liquid chamber and a second alkali chamber are arranged in the middle of the two-chamber bipolar membrane electrodialysis device, a second anode chamber is arranged on one side, away from the second alkali chamber, of the second feed liquid chamber, a second cathode chamber is arranged on one side, away from the second feed liquid chamber, of the second alkali chamber, a cation exchange membrane is arranged between the second feed liquid chamber and the second alkali chamber, a bipolar membrane is arranged between the second cathode chamber and the second alkali chamber, a bipolar membrane is also arranged between the second anode chamber and the second feed liquid chamber, and the solution pump is communicated with the second feed liquid chamber.
In some embodiments, the bipolar membrane electrodialysis apparatus further comprises a first feed liquid pump connected to an inlet of the first feed liquid chamber, a first acid liquid pump connected to an inlet of the first acid chamber, a first lye pump connected to an inlet of the first lye chamber, and a first electrode liquid pump connected to both the first anode chamber and an inlet of the first cathode chamber, an outlet of the first acid chamber is connected to an inlet of the first acid liquid pump, an outlet of the first lye chamber is connected to an inlet of the first lye pump, an outlet of the feed liquid chamber is connected to an inlet of the first feed liquid pump, and outlets of the first cathode chamber and the first anode chamber are connected to an inlet of the first electrode liquid pump.
In some embodiments, the bipolar membrane electrodialysis apparatus further comprises a second feed liquid pump connected to an inlet of the second feed liquid chamber, a second caustic liquid pump connected to an inlet of the second caustic chamber, and a second anolyte pump connected to inlets of both the second anode chamber and the second cathode chamber, outlets of the second anode chamber and the second cathode chamber being connected to inlets of the second anolyte pump, an outlet of the second feed liquid chamber being connected to an inlet of the second feed liquid pump, and an outlet of the second caustic chamber being connected to an inlet of the second caustic liquid pump.
In some embodiments, the outlet of the first acid chamber is further connected to a desorption reactor and the outlet of the first base chamber is further connected to an absorption column.
In some embodiments, the outlet of the second feed chamber is further connected to a desorption reactor and the outlet of the second caustic chamber is further connected to an absorption column.
In some embodiments, the device further comprises a mixer, the mixer comprises a fresh alkali liquor inlet and a regenerated alkali liquor inlet, an outlet of the mixer is connected with the absorption tower, and the regenerated alkali liquor inlet is connected with an outlet of the alkali chamber of the bipolar membrane electrodialysis device.
In some embodiments, the carbon dioxide recovery system includes a gas-liquid separator coupled to the desorption reactor, a compressor positioned between the desorption reactor and the gas-liquid separator, and a cooler positioned between the compressor and the gas-liquid separator.
In some embodiments, the gas phase outlet at the top of the desorption reactor is further provided with a demister, the outlet of which is connected to the inlet of the compressor.
In the prior art, the decarbonized product is directly decomposed in the bipolar membrane electrodialysis device to generate bubbles, and the bubbles are attached to the surface of an electrode membrane and dispersed in a solution, so that the resistance of the bipolar membrane electrodialysis device is increased, and the energy consumption of a system is further increased.
The chemical absorption flue gas CO provided by the application 2 The trapping system comprises an absorption tower, a desorption reactor and a bipolar membrane electrodialysis device. The flue gas enters an absorption tower to react with the alkali liquor sprayed into the tower to generate a decarbonized product, so that the absorption of carbon dioxide is realized. Strong acid solution is filled in the desorption reactor, and the decarbonized product enters the desorption reactor to react with strong acid to generate feed liquid containing strong acid salt and CO 2 ，CO 2 Overflow from the desorption reactor and enter the carbon dioxide recovery system. The bipolar membrane electrodialysis equipment is connected with the desorption reactor, the solution pump conveys the feed liquid into the bipolar membrane electrodialysis equipment, and the feed liquid is decomposed under the action of current to generate acid liquid and alkali liquid, so that the regeneration of the absorbent is realized.
The strong acid and the decarbonization product react in a desorption reactor to remove carbonate of the decarbonization product, and feed liquid generated after the removal of the carbonate is conveyed to bipolar membrane electrodialysis equipment to be regenerated to generate the strong acid and alkali liquor. Because the feed liquid is dissociated and regenerated in the bipolar membrane electrodialysis equipment, no air bubble is generated in the process, the conductivity of the bipolar membrane electrodialysis equipment is guaranteed, the increase of the system resistance in the regeneration process is avoided, the dissociation efficiency in the bipolar membrane electrodialysis equipment is improved, and the energy consumption of the system is reduced.
In addition, feed liquid, acid liquor and the like in the bipolar membrane electrodialysis device flow in a circulating mode, and the regeneration rate of the feed liquid can be improved after multiple cycles, so that the utilization rate of materials is improved, and waste liquid discharge is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings used in the embodiments or the prior art descriptions will be briefly described below, it is obvious that the drawings in the following description are only the embodiments of the present application, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a chemical absorption flue gas CO provided by the present application 2 A process flow schematic of the capture system;
FIG. 2 is a chemical absorption flue gas CO 2 The structure schematic diagram of the bipolar membrane electrodialysis device in one embodiment of the trapping system;
FIG. 3 is a chemical absorption flue gas CO 2 A schematic structure diagram of a bipolar membrane electrodialysis device in another specific embodiment of the trapping system;
fig. 4 is a schematic diagram of ion migration after two groups of three-chamber bipolar membrane electrodialysis devices are superposed.
Wherein the reference numerals in fig. 1 to 4 are:
the system comprises an absorption tower 1, an alkali liquor cooler 2, a mixer 3, a desorption reactor 4, a defogging device 5, a bipolar membrane electrodialysis device 6, a solution pump 7, a compressor 8, a cooler 9, a gas-liquid separator 10, a first anode chamber 611, a first acid chamber 612, a first feed liquor chamber 613, a first alkali chamber 614, a first cathode chamber 615, a first electrode liquor storage tank 621, a first acid liquor storage tank 622, a first feed liquor storage tank 623, a first alkali liquor storage tank 624, a first electrode liquor pump 631, a first acid liquor pump 632, a first feed liquor pump 633, a first alkali liquor pump 634, a second anode chamber 641, a second feed liquor chamber 642, a second alkali chamber 643, a second cathode chamber 644, a second feed liquor storage tank 651, a second electrode liquor storage tank 652, a second alkali liquor storage tank 653, a second feed liquor pump, a second electrode liquor pump 662 and a second alkali liquor pump 663.
In the figure, H + Represents a hydrogen ion, OH - Represents a hydroxide ion and MOH represents a useful compound for absorbing CO 2 Alkali solution of, M + Denotes the cation corresponding to the alkali solution, HX denotes the cation which can react with carbonate to desorb CO 2 Acid solution of (2), X - Represents an anion corresponding to an acid solution.
Detailed Description
The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only a part 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.
In order to better understand the technical scheme of the present application, the following detailed description is provided for the person skilled in the art with reference to the accompanying drawings and the detailed description.
Referring to fig. 1 to 4, fig. 1 shows a chemical absorption flue gas CO provided in the present application 2 A process flow schematic of the capture system; FIG. 2 is a chemical absorption flue gas CO 2 The structure schematic diagram of the bipolar membrane electrodialysis device in one embodiment of the trapping system; FIG. 3 is a chemical absorption flue gas CO 2 A schematic structure diagram of a bipolar membrane electrodialysis device in another specific embodiment of the trapping system; fig. 4 is a schematic diagram of ion migration after two groups of three-chamber bipolar membrane electrodialysis devices are overlaid.
The chemical absorption flue gas CO provided by the application 2 The trapping system, a process flow of which is shown in fig. 1, comprises an absorption tower 1, a desorption reactor 4 and a bipolar membrane electrodialysis device 6. The lower part of the absorption tower 1 is provided with an air inlet, and the top is provided with an air outlet. The upper part of the absorption tower 1 is provided with a spray pipe which is connected with an alkali liquor conveying pipeline, and the bottom of the absorption tower 1 is provided with a liquid outlet. Alkali liquor is conveyed into the absorption tower 1 through an alkali liquor conveying pipe and is sprayed to the bottom of the absorption tower 1, flue gas enters from the air inlet, and the alkali liquor and the flue gas flow in a reverse direction. The alkali liquor can be used as an absorbent to absorb carbon dioxide in the flue gas in the falling process, and the flue gas after carbon removal is discharged out of the absorption tower 1 through an exhaust port.
The desorption reactor 4 is connected with the liquid outlet of the absorption tower 1, and the decarbonization product generated by the reaction of the alkali liquor and the carbon dioxide is conveyed into the desorption reactor 4. The desorption reactor 4 is filled with acid liquor, and the acidity of the acid liquor is stronger than that of carbonic acid. So that the decarbonization product reacts with the acid solution to generate carbonic acid. The top of the desorption reactor 4 is connected with a carbon dioxide recovery system, and high-concentration carbon dioxide generated after the carbonic acid is decomposed enters the carbon dioxide recovery system, so that the carbon dioxide is recycled.
The bipolar membrane electrodialysis device 6 is connected with the bottom of the desorption reactor 4 through a feed liquid output pipeline, a solution pump 7 is arranged in the feed liquid output pipeline, and the feed liquid is conveyed to the bipolar membrane electrodialysis device 6 through the solution pump 7. As shown in fig. 4, the bipolar membrane electrodialysis apparatus 6 includes a bipolar membrane electrodialysis device in which a cation exchange membrane, an anion exchange membrane, and a bipolar membrane are provided. Two ends of the bipolar membrane electrodialysis device are provided with bipolar membranes, and the bipolar membranes, the cathode plate and the anode plate respectively form a cathode chamber and an anode chamber. Electrode solution is filled in the cathode chamber and the anode chamber, and voltage is applied. Ions in the feed liquid flow under the action of voltage, and meanwhile, a cation exchange membrane in the bipolar membrane electrodialysis device only allows cations to pass through, and an anion exchange membrane only allows anions to pass through, so that the feed liquid is decomposed to form alkali liquor and acid liquor, and the regeneration of the feed liquid is realized. The alkali liquor can be ammonia water, the ammonia water has the advantages of low price, no degradation and the like, and the acid liquor can be sulfuric acid. Of course, other solutions may be used as the alkali solution or the acid solution according to the needs of the user, for example, the alkali solution may be sodium alkali, potassium alkali, MEA (Monoethanolamine), etc., which is not limited herein, and the present application is described by taking ammonia as the alkali solution and sulfuric acid as the acid solution as examples.
Alternative, chemical absorption flue gas CO 2 The trapping system further comprises a mixer 3. As shown in figure 1, the mixer 3 comprises a new alkali liquor inlet and a regenerated alkali liquor inlet, the new alkali liquor inlet is connected with an alkali liquor conveying pipeline, the regenerated alkali liquor inlet is connected with an alkali chamber outlet of the bipolar membrane electrodialysis device 6, and an outlet of the mixer 3 is connected with the absorption tower 1. The fresh alkali liquor and the regenerated alkali liquor are mixed in the mixer 3 and then are conveyed to the absorption tower 1. In addition, an alkali liquor cooler 2 is arranged between the mixer 3 and the absorption tower 1 to cool the mixed alkali liquor.
Optionally, the carbon dioxide recovery system includes a gas-liquid separator 10 and a compressor 8, an inlet of the compressor 8 is connected to a gas-phase outlet at the top of the desorption reactor 4, an outlet of the compressor 8 is connected to the gas-liquid separator 10, and the gas-liquid separator 10 separates carbon dioxide from condensed droplets. A cooler 9 is provided between the gas-liquid separator 10 and the compressor 8, and the cooler 9 cools the gas phase to further condense the water vapor. In addition, a gas-phase outlet at the top of the desorption reactor 4 is also provided with a demisting device 5, an outlet of the demisting device 5 is connected with an inlet of the compressor 8, the demisting device 5 can remove liquid drops in the gas phase, the influence of the liquid drops on the compressor 8 is reduced, and the load of the gas-liquid separator 10 is reduced.
In this example, flue gas CO was chemically absorbed 2 A desorption reactor 4 is provided in the capture system, and the desorption reactor 4 reacts with the decarbonized product with a strong acid to produce carbonic acid. Carbon dioxide is desorbed after the carbonic acid is decomposed, and the high-concentration carbon dioxide is recycled by a carbon dioxide recycling system. The feed liquid generated after desorption is regenerated in the bipolar membrane electrodialysis equipment 6, so that bubbles generated in the regeneration process are avoided, the increase of the system resistance is reduced, and the purpose of reducing the energy consumption of the system is achieved.
In one embodiment of the present application, the bipolar membrane electrodialysis device 6 comprises a three-compartment bipolar membrane electrodialysis apparatus. As shown in fig. 2, the middle of the three-compartment bipolar membrane electrodialysis device is a first feed compartment 613, two sides of the first feed compartment 613 are a first acid compartment 612 and a first base compartment 614, respectively, an anion exchange membrane is disposed between the first feed compartment 613 and the first acid compartment 612, and a cation exchange membrane is disposed between the first feed compartment 613 and the first base compartment 614. The side of the first base chamber 614 far away from the first feeding chamber 613 is a first cathode chamber 615, the side of the first acid chamber 612 far away from the first feeding chamber 613 is a first anode chamber 611, a bipolar membrane is arranged between the first cathode chamber 615 and the first base chamber 614, and a bipolar membrane is also arranged between the first anode chamber 611 and the first acid chamber 612. The sulfate ions in the first feed chamber 613 pass through the anion exchange membrane to enter the first acid chamber 612, and the ammonium ions pass through the cation exchange membrane to enter the first base chamber 614, so that sulfuric acid is generated in the first acid chamber 612 and ammonia water is generated in the first base chamber 614.
Optionally, the bipolar membrane electrodialysis device 6 further includes a first feed liquid pump 633 connected to an inlet of the first feed liquid chamber 613, an inlet of the first feed liquid pump 633 is connected to an outlet of the first feed liquid chamber 613, and the first feed liquid pump 633 can drive feed liquid to circularly flow, so as to improve the utilization rate of the feed liquid. An outlet of the solution pump 7 is connected to an inlet of the first feed chamber 613, and feeds the first feed chamber 613. A conductivity test instrument may be disposed in the first feed chamber 613 for detecting the conductivity of the treated feed solution, wherein a conductivity of the feed solution below a threshold value indicates that a substantial portion of the anions and cations have been transferred to the first acid chamber 612 and the first base chamber 614, respectively. A first feed liquid storage tank 623 for storing feed liquid is provided between the first feed liquid pump 633 and the first feed liquid chamber 613.
The bipolar membrane electrodialysis device 6 further comprises a first acid pump 632 connected to an inlet of the first acid compartment 612, an inlet of the first acid pump 632 being connected to an outlet of the first acid compartment 612, an outlet of the first acid compartment 612 being further connected to the desorption reactor 4. The first acid pump 632 drives the acid solution to flow circularly, and a pH sensor may be disposed in the first acid chamber 612, so that the acid solution is delivered to the desorption reactor 4 for utilization when the acid solution reaches a first preset pH value. A first acid storage tank 622 is disposed between the first acid pump 632 and the first acid chamber 612 for storing acid.
The bipolar membrane electrodialysis device 6 further comprises a first lye pump 634 connected to an inlet of the first lye chamber 614, an inlet of the first lye pump 634 being connected to an outlet of the first lye chamber 614, an outlet of the first lye chamber 614 being further connected to the absorption column 1. The first lye pump 634 drives the lye to circularly flow, a pH sensor can be arranged in the first lye chamber 614, and when the lye reaches a second preset pH value, the lye is conveyed to the absorption tower 1 for utilization. A first lye storage tank 624 is further disposed between the first lye pump 634 and the first lye chamber 614 for storing lye.
Optionally, the bipolar membrane electrodialysis apparatus 6 further includes a first electrode liquid pump 631 connected to inlets of the first anode chamber 611 and the first cathode chamber 615, outlets of the first cathode chamber 615 and the first anode chamber 611 are connected to an inlet of the first electrode liquid pump 631, and a first electrode liquid storage tank 621 is disposed between the first electrode liquid pump 631 and the three-chamber bipolar membrane device, and is configured to store electrode liquid.
In addition, when the treatment capacity is large, a user can parallelly and superpose a plurality of three-chamber bipolar membrane electrodialysis devices for use. In fig. 4, two three-compartment bipolar membrane electrodialysis devices are stacked as an example, and a schematic diagram of ion migration after stacking is shown. A user can also set a plurality of three-chamber bipolar membrane electrodialysis devices according to needs. In the bipolar membrane electrodialysis device 6, reference may be made to an embodiment of a three-chamber bipolar membrane electrodialysis device, which is not described herein again.
In an application scenario of the embodiment, the alkali solution is an ammonia solution with a temperature of 10-20 ℃ and a concentration of 3-10 wt.%. The ammonia water solution enters from a nozzle at the upper part of the absorption tower 1, and the flue gas is saturated flue gas with the temperature of about 50 ℃ after denitration, desulfurization, dust removal and temperature reduction, wherein the carbon dioxide accounts for about 12.46 percent. Flue gas enters from the lower part of the absorption tower 1, and the ammonia water solution and the flue gas are in countercurrent contact and react in the absorption tower 1 to absorb carbon dioxide in the flue gas. The liquid drops of the washed decarbonized flue gas are removed by a high-efficiency demisting device at the upper end of the absorption tower 1, and the decarbonized flue gas is washed by water to remove ammonia and then enters a chimney to be discharged. The decarbonized product is discharged from the bottom of the absorption tower 1 and enters a desorption reactor 4.
After entering the desorption reactor 4, the decarbonized product reacts with the sulfuric acid solution in the desorption reactor 4 to generate a large amount of carbon dioxide gas. The gas enters a carbon dioxide recovery system after carried liquid drops are removed by a demisting device 5 at the gas outlet of the desorption reactor 4. After compression, condensation and gas-liquid separation, most of water vapor in the gas is removed, and the high-purity carbon dioxide gas enters a subsequent storage or transportation unit.
Feed liquid generated after the reaction of the decarbonized product and the sulfuric acid enters a first feed liquid chamber 613 of the three-chamber bipolar membrane electrodialysis device from a liquid outlet at the lower part of the desorption reactor 4, dilute sulfuric acid with the initial concentration of 0.1mol/L is filled in a first acid chamber 612, and aqueous ammonia with the initial concentration of 0.1mol/L is filled in a first alkali chamber 614. The first anode chamber 611 and the first cathode chamber 615 were filled with an initial 0.5mol/L sodium sulfate solution. 15mA/cm is applied between the cathode and the anode 2 The feed liquid is regenerated into acid liquid and alkali liquid under the action of electric field drive and ion exchange membrane selective permeability, and the acid liquid and the alkali liquid are recycled. Under the working condition, the decomposition efficiency of the bipolar membrane electrodialysis can reach more than 90 percent, the decomposition energy consumption is 0.80MJ/kg, the reaction in the carbon dioxide desorption reactor 4 is strong acid-weak acid, and the carbon dioxide can be completely desorbed, and the calculation shows that in the system, when the ammonia and the carbon dioxide are completely reacted at the ratio of 1:1, the theoretical minimum carbon dioxide regeneration energy consumption is only 1.124MJ/kgCO 2 . However, the ammonia-carbon ratio is larger than 1 in the actual condition, and the simulation junction of AspenplusThe result shows that the carbon dioxide desorption energy consumption of the system is 1.865MJ/kgCO 2 Is far lower than that of the alcohol amine decarburization process (4-5 MJ/kgCO) 2 ) And ammonia process flue gas CO 2 Trapping process (2.5-3.5 MJ/kgCO) 2 ) The carbon dioxide desorption energy consumption has obvious energy-saving effect.
In this embodiment, the bipolar membrane electrodialysis apparatus 6 comprises a three-compartment bipolar membrane electrodialysis device, which is separated by a cation exchange membrane and an anion exchange membrane to form a first acid compartment 612, a first feed compartment 613 and a first base compartment 614. In the regeneration process, the feed liquid, the acid liquid and the alkali liquid circularly flow, and when the acid liquid and the alkali liquid reach the standard, the feed liquid, the acid liquid and the alkali liquid are respectively conveyed to the desorption reactor 4 and the absorption tower 1. The three-chamber bipolar membrane electrodialysis device can reduce the mixing of feed liquid, acid liquid and alkali liquid and ensure the purity of the material.
In another embodiment of the present application, the bipolar membrane electrodialysis device 6 comprises a two-compartment bipolar membrane electrodialysis apparatus. As shown in fig. 3, the middle part of the two-compartment bipolar membrane electrodialysis device is provided with a cation exchange membrane, and the cation exchange membrane separates the two-compartment bipolar membrane electrodialysis device to form a second feed compartment 642 and a second base compartment 643. The side of the second feed chamber 642 away from the second alkali chamber 643 is a second anode chamber 641, and the side of the second alkali chamber 643 away from the second feed chamber 642 is a second cathode chamber 644. A bipolar membrane is disposed between second cathode chamber 644 and second base chamber 643, and between second anode chamber 641 and second feed chamber 642. The solution pump 7 communicates with the second feed chamber 642, and delivers feed liquid into the second feed chamber 642. Under the action of the electric field, ammonium ions in the feed liquid pass through the cation exchange membrane and enter the second alkali chamber 643, an ammonia water solution is formed in the second alkali chamber 643, and sulfate ions are left in the second feed liquid chamber 642 to form a sulfuric acid solution. Of course, a user may also set an anion exchange membrane in the middle of the two-compartment bipolar membrane electrodialysis device according to needs, and the anion exchange membrane separates the two-compartment bipolar membrane electrodialysis device into a feed compartment and an acid compartment, which is not limited herein.
The bipolar membrane electrodialysis device 6 further comprises a second feed liquid pump 661, a second alkaline liquid pump 663 and a second electrode liquid pump 662. The outlet of the second feed liquid pump 661 is connected to the inlet of the second feed liquid chamber 642, the inlet of the second feed liquid pump 661 is connected to the outlet of the second feed liquid chamber 642, and the second feed liquid pump 661 can drive the feed liquid to flow circularly. A second feed liquid storage tank 651 is disposed between the second feed liquid pump 661 and the second feed liquid chamber 642 for storing the feed liquid. The outlet of the second feed liquid chamber 642 is also connected to the desorption reactor 4, and a pH sensor may be disposed in the second feed liquid chamber 642 to deliver the feed liquid to the desorption reactor 4 for utilization when the feed liquid reaches a first predetermined pH value.
An outlet of the second alkali liquid pump 663 is connected to an inlet of the second alkali chamber 643, an inlet of the second alkali liquid pump 663 is connected to an outlet of the second alkali chamber 643, and an outlet of the second alkali chamber 643 is further connected to the absorption tower 1. The second alkali liquid pump 663 drives the alkali liquid to circularly flow, and a pH sensor can be arranged in the second alkali chamber 643 to convey the alkali liquid to the absorption tower 1 for utilization when the alkali liquid reaches a second preset pH value. A second lye storage tank 653 is also arranged between the second lye pump 663 and the second lye chamber 643 for storing lye.
The inlets of the anode chamber and the cathode chamber are connected to the outlet of the second electrode liquid pump 662, and the outlets of the second anode chamber 641 and the second cathode chamber 644 are connected to the inlet of the second electrode liquid pump 662. A second electrode solution storage tank 652 is arranged between the second electrode solution pump 662 and the two-chamber bipolar membrane electrodialysis device and used for storing electrode solution. The second electrode liquid pump 662 can drive the electrode liquid to circularly flow. The electrode solution may be 0.5mol/L sodium sulfate solution, and certainly, the user may also select other solutions as the electrode solution according to the need, which is not limited herein.
In this embodiment, the bipolar membrane electrodialysis apparatus 6 realizes regeneration of acid solution and alkali solution by using a two-chamber bipolar membrane electrodialysis device. The regeneration process can also ensure the purity of the acid liquor and the alkali liquor, and simultaneously can simplify the structure of the bipolar membrane electrodialysis equipment 6 and reduce the equipment cost.
It should be noted that in this specification, relational terms such as first and second, and the like are used solely to distinguish one entity from another entity without necessarily requiring or implying any actual such relationship or order between such entities.
Chemical absorption cigarette provided by the applicationGas CO 2 The trapping system is described in detail. The principles and embodiments of the present application are explained herein using specific examples, which are provided only to help understand the method and the core idea of the present application. It should be noted that, for those skilled in the art, it is possible to make several improvements and modifications to the present application without departing from the principle of the present application, and such improvements and modifications also fall within the scope of the claims of the present application.
Claims (10)
1. Flue gas CO by chemical absorption method 2 An entrapment system, comprising:
the absorption tower (1) is used as a reaction place for absorbing carbon dioxide by alkali liquor;
a desorption reactor (4) connected to the bottom of the absorption tower (1) for accommodating the decarbonized product generated in the absorption tower (1) and the acid solution reacted with the decarbonized product and serving as a reaction site for decarbonizing the decarbonized product, wherein the top of the desorption reactor (4) is connected to a carbon dioxide recovery system;
the bipolar membrane electrodialysis device (6) is connected with the desorption reactor (4) and used for decomposing feed liquid generated by the desorption reactor (4), and a solution pump (7) used for conveying the feed liquid is arranged between the bipolar membrane electrodialysis device (6) and the desorption reactor (4).
2. The chemical absorption flue gas CO of claim 1 2 The trapping system is characterized in that the bipolar membrane electrodialysis device (6) comprises a three-chamber bipolar membrane electrodialysis device, the middle of the three-chamber bipolar membrane electrodialysis device is a first feed chamber (613), two sides of the first feed chamber (613) are a first acid chamber (612) and a first base chamber (614), the side, away from the first feed chamber (613), of the first base chamber (614) is a first cathode chamber (615), the side, away from the first feed chamber (613), of the first acid chamber (612) is a first anode chamber (611), an anion exchange membrane chamber is arranged between the first feed chamber (613) and the first acid chamber (612), and a cation exchange membrane is arranged between the first feed chamber (613) and the first base chamber (614)A membrane, a bipolar membrane being provided between the first cathode compartment (615) and the first base compartment (614), a bipolar membrane also being provided between the first anode compartment (611) and the first acid compartment (612), the solution pump (7) being in communication with the first feed compartment (613) in the bipolar membrane electrodialysis device (6).
3. The chemical absorption flue gas CO of claim 1 2 A trapping system, characterized in that the bipolar membrane electrodialysis apparatus (6) comprises a two-compartment bipolar membrane electrodialysis device, the middle part of the two-chamber bipolar membrane electrodialysis device is provided with a second feed chamber (642) and a second alkali chamber (643), the side of the second feed chamber (642) far away from the second alkali chamber (643) is a second anode chamber (641), the side of the second alkali chamber (643) far away from the second feed chamber (642) is a second cathode chamber (644), a cation exchange membrane is arranged between the second feed liquid chamber (642) and the second alkali chamber (643), a bipolar membrane is arranged between the second cathode chamber (644) and the second alkali chamber (643), a bipolar membrane is also arranged between the second anode chamber (641) and the second feed liquid chamber (642), the solution pump (7) is communicated with the second feed liquid chamber (642) in the bipolar membrane electrodialysis device (6).
4. The chemical absorption flue gas CO of claim 2 2 A capture system, characterized in that the bipolar membrane electrodialysis device (6) further comprises a first feed liquid pump (633) connected to an inlet of the first feed chamber (613), a first acid liquid pump (632) connected to an inlet of the first acid chamber (612), a first lye pump (634) connected to an inlet of the first lye chamber (614), and a first electrode liquid pump (631) connected to inlets of both the first anode chamber (611) and the first cathode chamber (615), the outlet of the first acid chamber (612) is connected to the inlet of the first acid pump (632), the outlet of the first caustic chamber (614) is connected to the inlet of the first caustic pump (634), the outlet of the first feed liquid chamber (613) is connected with the inlet of the first feed liquid pump (633), the outlets of the first cathode chamber (615) and the first anode chamber (611) are connected with the inlet of the first electrode liquid pump (631).
5. The chemical absorption flue gas CO of claim 3 2 A trapping system, characterized in that the bipolar membrane electrodialysis device (6) further comprises a second feed liquid pump (661) connected to the inlet of the second feed liquid chamber (642), a second alkaline liquid pump (663) connected to the inlet of the second alkaline chamber (643), and a second electrode liquid pump (662) connected to both the second anode chamber (641) and the inlet of the second cathode chamber (644), the outlets of the second anode chamber (641) and the second cathode chamber (644) being connected to the inlet of the second electrode liquid pump (662), the outlet of the second feed liquid chamber (642) being connected to the inlet of the second feed liquid pump (661), the outlet of the second alkaline chamber (643) being connected to the inlet of the second alkaline liquid pump (663).
6. The chemical absorption flue gas CO of claim 4 2 A capture system, characterized in that the outlet of the first acid chamber (612) is further connected to the desorption reactor (4) and the outlet of the first base chamber (614) is further connected to the absorption column (1).
7. The chemical absorption flue gas CO of claim 5 2 A capture system, characterized in that the outlet of the second liquor chamber (642) is further connected to the desorption reactor (4) and the outlet of the second caustic chamber (643) is further connected to the absorption column (1).
8. The chemical absorption flue gas CO of any one of claims 6 or 7 2 The trapping system is characterized by further comprising a mixer (3), wherein the mixer (3) comprises a fresh alkali liquor inlet and a regenerated alkali liquor inlet, the outlet of the mixer (3) is connected with the absorption tower (1), and the regenerated alkali liquor inlet is connected with the outlet of the alkali chamber of the bipolar membrane electrodialysis device (6).
9. The chemical absorption flue gas CO according to any one of claims 1 to 7 2 -capture system, characterized in that it comprises a desorption reactor (4)A gas-liquid separator (10) connected to the desorption reactor (4), a compressor (8) located between the desorption reactor and the gas-liquid separator (10), and a cooler (9) located between the compressor (8) and the gas-liquid separator (10).
10. The chemical absorption flue gas CO of claim 9 2 The trapping system is characterized in that a gas-phase outlet at the top of the desorption reactor (4) is also provided with a demisting device (5), and an outlet of the demisting device (5) is connected with an inlet of the compressor (8).
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Application publication date: 20220726 |