CN117138553A - Isothermal carbon dioxide absorption and trapping technology - Google Patents
Isothermal carbon dioxide absorption and trapping technology Download PDFInfo
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- CN117138553A CN117138553A CN202210569993.9A CN202210569993A CN117138553A CN 117138553 A CN117138553 A CN 117138553A CN 202210569993 A CN202210569993 A CN 202210569993A CN 117138553 A CN117138553 A CN 117138553A
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 62
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 25
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 22
- 238000005516 engineering process Methods 0.000 title claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 74
- 238000011069 regeneration method Methods 0.000 claims abstract description 40
- 230000008929 regeneration Effects 0.000 claims abstract description 39
- 230000002745 absorbent Effects 0.000 claims abstract description 16
- 239000002250 absorbent Substances 0.000 claims abstract description 16
- 238000005191 phase separation Methods 0.000 claims abstract description 8
- 239000002904 solvent Substances 0.000 claims abstract description 6
- 230000008859 change Effects 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 238000010992 reflux Methods 0.000 claims description 17
- 239000003960 organic solvent Substances 0.000 claims description 10
- 150000001412 amines Chemical class 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 239000002608 ionic liquid Substances 0.000 claims description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 150000002170 ethers Chemical class 0.000 claims description 3
- 230000006872 improvement Effects 0.000 claims description 3
- 150000001409 amidines Chemical class 0.000 claims description 2
- 150000001413 amino acids Chemical class 0.000 claims description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 2
- 238000005485 electric heating Methods 0.000 claims description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims 1
- 230000007704 transition Effects 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 13
- 238000005265 energy consumption Methods 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 230000008569 process Effects 0.000 abstract description 7
- -1 alcohol amine Chemical class 0.000 abstract description 2
- 230000007547 defect Effects 0.000 abstract description 2
- 239000003054 catalyst Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 14
- 239000012071 phase Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- BFSVOASYOCHEOV-UHFFFAOYSA-N 2-diethylaminoethanol Chemical compound CCN(CC)CCO BFSVOASYOCHEOV-UHFFFAOYSA-N 0.000 description 1
- 101001039157 Homo sapiens Leucine-rich repeat-containing protein 25 Proteins 0.000 description 1
- 102100040695 Leucine-rich repeat-containing protein 25 Human genes 0.000 description 1
- 150000001298 alcohols Chemical group 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 150000003141 primary amines Chemical group 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 150000003335 secondary amines Chemical class 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 150000003512 tertiary amines Chemical class 0.000 description 1
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
- B01D53/34—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
- 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
- B01D53/343—Heat recovery
-
- 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
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/70—Organic acids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/80—Organic bases or salts
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Aiming at the defect of high energy consumption in the process of capturing carbon dioxide by using the existing alcohol amine solution, the invention provides a carbon dioxide isothermal absorption capturing technology, and the heat of reaction is recovered by combining a phase-change absorbent and a heat pump technology, so that the regeneration energy consumption is reduced. Wherein the technical route includes phase change absorbent, absorption tower, decanter, regeneration tower, heat pump system and other auxiliary equipment. The invention has the advantages that: 1. the absorbent in the absorption tower can be used for mixing CO with 2 Partially or totally recovering the reaction heat of the catalyst for a regeneration process; 2. the phase-change solvent is utilized for phase separation after absorption, so that the quantity of rich liquid entering a regeneration tower can be effectively reduced, the sensible heat of the rich liquid for heating is reduced, and the regeneration energy consumption can be effectively reduced.
Description
Technical Field
The invention relates to the technical field of carbon dioxide trapping, in particular to a carbon dioxide isothermal absorption trapping technology.
Background
CO 2 TrappingThe chemisorption method in the field of utilization and sequestration (CCUS) is CO 2 The most promising route for trapping is trapped. However, the chemical absorption method using alcohol amine solution as absorbent has the bottleneck of high energy consumption (3.5-4.0 GJ/t CO) 2 ）。
To reduce CO 2 Energy consumption for trapping researchers have conducted extensive studies on screening of absorbents and heat recovery during trapping, wherein the screened low-reaction heat phase-change absorbents include MEA, DEA/mixed alcohol/H 2 O、DEEA/MAPA+H 2 Solvents such as O. The heat recovery mode comprises a lean-rich liquid heat exchanger, an absorption tower intercooler, a heat pump process recovery regeneration tower top waste heat and other methods.
When the phase-change absorbent is used in the traditional absorption process, the trapping energy consumption is not reduced to 2.2 GJ/t CO 2 The following is given. Several of the heat recovery methods are to recycle the waste heat leaving the whole trapping system, but the regenerated energy consumption after energy optimization is difficult to break through 2.4 GJ/t CO 2 . In the regeneration process, the heat demand ratio of the reaction is close to 60%, the reaction heat released in the absorption tower can not be utilized by the flow improvement of the basic heat exchange method, and in order to further reduce the energy consumption, the energy released in the absorption reaction is required to be recovered and supplied to the regeneration section, so that the heat source demands such as steam and the like in the regeneration flow are reduced.
Disclosure of Invention
The invention aims to solve the technical problem of overcoming and optimizing the defect of high energy consumption of a carbon dioxide capturing process in the prior art, and provides a carbon dioxide isothermal absorption capturing technology.
The technical route of the invention is as follows:
the absorbent is a phase change absorbent system, and is generally an aqueous or anhydrous solvent system composed of organic solvents, etc., wherein at least one of the organic solvents has CO 2 Chemical absorption properties. With CO 2 The organic solvent with chemical absorption performance comprises amine, amidine, amino acid, ionic liquid, etc., and is not CO 2 The absorbing organic solvent comprises alcohol, ethers, alkanes, aromatic hydrocarbons, cycloalkanes, ionic liquids and other solvents.
A heat pump comprisesLean liquor cooler, compressor, reboiler and choke valve. The lean solution cooler is connected with a compressor, the compressor is connected with a reboiler, the reboiler is connected with a throttle valve, and the throttle valve is connected with the lean solution cooler, namely, the heat pump system is formed by a circulation loop with the phase state, the temperature and the pressure of a high-temperature working medium changed along with the phase state, the temperature and the pressure of the high-temperature working medium. The lean solution exchanges heat with the high-temperature working medium in the lean solution cooler to gasify the working medium, and CO 2 And the rich liquid exchanges heat with the high-temperature working medium in the reboiler to condense the working medium. In addition, the compressor is used for pressurizing high-temperature working medium steam, and the throttle valve is used for decompressing high-temperature working medium liquid, so that the mechanical energy is utilized to convert heat energy from a low-temperature heat source to a high-temperature heat source.
The absorption tower is connected to the flue gas line in the lower part, connected to the lean liquid cooler of the heat pump system in the upper region of the tower, and connected to the decanter in the bottom region of the tower. The lean absorption liquid is changed into rich absorption liquid after absorbing carbon dioxide in flue gas in the absorption tower, and then enters the decanter through a pipeline, and a purified gas exhaust port is arranged at the top of the absorption tower, so that purified gas is discharged.
A decanter communicating with the absorption column and having a rich absorption liquid inlet for separating the rich liquid into separated liquid and CO in the decanter 2 Rich liquid. The decanter is connected with the lean solution cooler and the reboiler, and the separated solution enters the lean solution cooler to be used as a temperature diluent of the absorption tower after phase separation, and CO 2 The rich liquid enters a reboiler to receive heat.
The upper part of the regeneration tower is connected with a reboiler for introducing CO from the reboiler to a conveying pipe at the upper part of the tower into the regeneration tower 2 CO is sucked out by the solution-rich dissolution 2 And (3) gas-liquid phase separation. The lower part is connected with a reboiler and a lean liquid cooler for CO 2 The lean solution is output from a conveying pipe at the bottom of the regeneration tower and is split, and a part of solution and CO 2 The rich liquid is mixed, and a part of the solution is mixed with the separated liquid sent from the decanter. The top of the regeneration tower is provided with a regeneration gas discharge port, and the regeneration gas is discharged.
Optionally, an electric heating or other heating device is arranged in the lean liquid cooler of the heat pump system to supply CO to the heat pump system 2 The heat transferred by the rich liquid is compensated.
Alternatively, the heat pump system may be a conventional cycle as described above, or may be a conventional cycle modified optimization route that optimizes cycle efficiency by adding or replacing components, changing the cycle mode, and the like in the conventional cycle.
Alternatively, the heat pump system may be a conventional cycle as described above, or a transcritical cycle.
Alternatively, the heat pump system may be a conventional cycle as described above, or a variable temperature cycle.
Alternatively, CO flowing from the bottom of the regeneration column 2 After the lean solution is split, a part of the lean solution is separated from CO 2 Rich and rich
The mixed liquid enters a reboiler, and a part of the mixed liquid is mixed with the separated liquid after phase separation and enters a lean liquid cooler.
Optionally, a reflux condenser is arranged at the outer end of the top of the regeneration tower, the mixed gas flowing out from the top of the regeneration tower enters the reflux condenser and then the gasified absorption liquid is cooled and refluxed to the regeneration tower, and at the same time, CO is discharged 2 And (3) gas.
Optionally, the reflux condenser of the regeneration tower is connected to the upper part of the absorption tower through a recooler for further reducing part of the mixed liquor split from the reflux condenser, and the mixed liquor is fed into the absorption tower for reducing the temperature of the absorbent.
Optionally, the separation liquid in the decanter is separated from CO 2 The rich liquid can be separated into upper layer and lower layer of CO due to different physical and chemical properties of different solutions 2 A rich liquid; the upper layer after phase separation can be CO 2 Rich liquid and separating liquid in the lower layer.
Compared with the existing carbon dioxide capturing technology, the invention has the following advantages: 1. the invention can combine the absorbent and CO in the absorption tower 2 The reaction heat released after the reaction is partially or completely recovered, and the recovered reaction heat is used in the regeneration process, so that the regeneration energy consumption can be effectively reduced; 2. the invention can effectively reduce the quantity of rich liquid entering the regeneration tower by utilizing a phase separation mechanism, reduce the sensible heat of partial rich liquid supply and temperature rise, and effectively reduce the regeneration energy consumption.
Drawings
FIG. 1 is a schematic diagram of a carbon dioxide phase change near isothermal absorption capture technique according to the present invention.
Wherein, 1, an absorption tower; 2. a regeneration tower; 3. a decanter; 4. a lean solution cooler; 5. a compressor; 6. a reboiler; 7. a throttle valve; 8. a recooler; 9. a reflux condenser; 10. a flue gas delivery pipe; 11. a purge gas delivery pipe; 12. CO 2 A delivery tube; 13. CO 2 Rich liquid and CO 2 A lean solution mixing and conveying point; 14. separating liquid and CO 2 A lean solution mixing and conveying point; 15. CO 2 A lean liquid delivery pipe; 16. a reflux liquid split-flow conveying point; 17. a lean liquid return pipe; 18. a reflux liquid return pipe; 19. a rich liquid conveying pipe; 20. a mixed gas delivery pipe; 21. CO 2 A rich liquid conveying pipe; 22. an absorption liquid; 23. separating liquid; 24. CO 2 Rich liquid.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the invention, as presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, are intended to fall within the scope of the present invention.
In the description of the present invention, it should be noted that embodiments of the present invention and features in the embodiments may be combined with each other without conflict.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
In the description of the present invention, it should be noted that the terms "upper," "lower," "top," "bottom," and the like indicate an orientation or positional relationship based on that shown in the drawings, and are merely for convenience of description and simplification of the description, and do not indicate or imply that the apparatus or element in question must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
The embodiment provides a carbon dioxide phase-change approximate isothermal absorption trapping technology, as shown in fig. 1, the operation flow of the carbon dioxide phase-change isothermal absorption trapping technology for organic amine absorption of a water system is as follows:
the absorbent (22) used in the medium temperature phase change absorption trapping system in this embodiment is an organic amine aqueous system, wherein the aqueous system is organic amine/organic solvent/water, the organic amine is primary amine, secondary amine, tertiary amine and sterically hindered amine as representative, and other various amines, and the organic solvent is alcohols, ethers, alkanes, etc.
The heat pump comprises a lean solution cooler (4), a compressor (5), a reboiler (6) and a throttle valve (7). Gasifying a high-temperature working medium in the heat pump system in a lean solution cooler (4) to obtain high-temperature low-pressure gas, and removing heat of the lean solution at the moment; the high-temperature working medium flows through a compressor (5) to obtain high-temperature and high-pressure steam; the high-temperature working medium flows through a reboiler (6) to obtain low-temperature high-pressure liquid, and heat is transferred to the rich liquid at the moment; the high-temperature working medium flows through the throttle valve (7) to obtain low-temperature low-pressure liquid, so that the liquid is repeatedly circulated in the heat pump system, and the mechanical energy is utilized to convert heat energy from a low-temperature heat source to a high-temperature heat source.
The absorption tower (1) is communicated with the flue conveying pipe (10) at the bottom, is communicated with the lean solution cooler (4) of the heat pump system at the upper part, the lean solution from the lean solution cooler (4) of the heat pump system enters into the lean solution return pipe (17) at the upper part, the lean solution becomes rich absorption solution after absorbing carbon dioxide in flue gas in the absorption tower, and the rich absorption solution enters into the decanter (3) at the bottom of the absorption tower through the rich solution conveying pipe (19). Wherein the temperature range of the absorption tower is 40-90 ℃ and the pressure range is 90-150kPa.
A decanter (3) which is connected with the absorption tower (1) and has a rich absorption liquid entering, and the rich absorption liquid is separated into a separation liquid (23) and CO in the decanter (3) 2 Rich liquor (24), CO 2 Rich liquor (24) and partially split CO 2 The lean solution is mixed at a mixing point (13) and then is conveyed to a reboiler (6), and the separation solution and CO are separated 2 The lean solution is mixed at a mixing point (14) and becomes lean solution, and the lean solution is sent to a lean solution cooler (4).
Regeneration tower (3), CO 2 Rich liquid is fed from reboiler (6) to CO at the upper part of the tower 2 The rich liquid conveying pipe (21) enters the regeneration tower (3), CO 2 Lean solution self-regeneration tower bottom CO 2 The lean liquid delivery pipe (15) outputs and splits, and one part of the lean liquid is connected with CO 2 The rich liquid is mixed at a mixing point (13) and then is conveyed to a reboiler (6), the other part of the rich liquid and the separation liquid are mixed at a mixing point (14) and then become lean liquid, and the regeneration gas is discharged from a mixed gas conveying pipe (20) at the top of the tower. Wherein the temperature range of the regeneration tower is 40-120 ℃ and the pressure range is 100-250 kPa.
A reflux condenser (9) installed at the upper part of the regeneration tower (3), wherein the mixed gas discharged from the mixed gas conveying pipe (20) enters the reflux condenser (9) and then the gasified absorption liquid is cooled and refluxed to the regeneration tower (3), and at the same time, CO 2 Delivery pipe (12) CO 2 And (3) gas.
And a recooler (8), wherein a reflux condenser (9) of the regeneration tower (3) is connected with the upper part of the absorption tower (1) through the recooler (8), the recooler is used for further reducing part of mixed liquid split from the reflux condenser, and the mixed cold liquid is sent into the absorption tower for reducing the temperature of the absorbent.
Although the present invention has been described with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements and changes may be made without departing from the spirit and principles of the present invention.
Claims (7)
1. A carbon dioxide isothermal absorption trapping technology is characterized in that an absorbent (22), a heat pump system (4, 5, 6, 7), an absorption tower (1), a decanter (2) and a regeneration tower (3); the absorbent is a phase change absorbent system, and is generally an aqueous or anhydrous solvent system composed of organic solvents, etc., wherein at least one of the organic solvents has CO 2 Chemical absorption property of CO 2 The organic solvent with chemical absorption performance comprises amine, amidine, amino acid, ionic liquid, etc., and is not CO 2 The absorbing organic solvent comprises alcohol, ethers, alkane, naphthene, aromatic hydrocarbon, ionic liquid and other solvents; the heat pump comprises a lean solution cooler (4), a compressor (5), a reboiler (6) and a throttle valve (7); the lean solution cooler (4) is connected with the compressor (5), the compressor (5) is connected with the reboiler (6), the reboiler (6) is connected with the throttle valve (7), the throttle valve (7) is connected with the lean solution cooler (4) again, and the heat pump system is composed of a circulation loop which changes with the phase state, the temperature and the pressure of the high-temperature working medium; the absorption tower (1) is communicated with a flue conveying pipe (10), and d3] [d4]Is connected to a decanter (2) in the bottom region of the column; the decanter (2) is communicated with the absorption tower (1) and is provided with a rich absorption liquid, and the rich absorption liquid is separated into a separation liquid (23) and CO reacted with carbon dioxide in the decanter (3) 2 A rich liquid (24); CO for the regeneration tower (3) and reboiler (6) 2 The rich liquid delivery pipe (21) is communicated, the bottom is communicated with the reboiler (6) by CO 2 The lean liquid delivery pipe (15) is communicated with the separation liquid sent out by the decanter (2) at a mixing point (14), and is communicated with the reflux condenser (9) by a mixed gas delivery pipe (20).
2. The carbon dioxide phase-change isothermal absorption trapping technology according to claim 1, wherein an electric heating or other heating device is arranged in the lean liquid cooler (4) to compensate the heat transferred from the heat pump system (4, 5, 6, 7) to the CO2 rich liquid.
3. The carbon dioxide phase-change isothermal absorption trapping technology according to claim 1, wherein the heat pump system can be a conventional cycle improvement optimizing route for optimizing cycle efficiency by adding or replacing components, changing a cycle mode and the like in a conventional cycle, and can be a transcritical cycle or a variable-temperature cycle.
4. The carbon dioxide phase-change isothermal absorption trapping technology according to claim 1, wherein after the CO2 lean solution flowing out from the bottom of the regeneration tower (3) is split, a part of the lean solution is mixed with the CO2 rich solution and then enters a reboiler (6), and a part of the lean solution is mixed with the separated solution after phase separation and enters a lean solution cooler (4).
5. The carbon dioxide phase-change isothermal absorption trapping technology according to claim 1, wherein a reflux condenser (9) is arranged at the outer end of the top of the regeneration tower (3), and the mixed gas flowing out of the top of the regeneration tower (3) enters the reflux condenser (9) to cool and reflux the gasified absorption liquid part to the regeneration tower.
6. The carbon dioxide phase transition isothermal absorption trapping technology according to claim 1, wherein a reflux condenser of the regeneration tower (3) is connected to an upper portion of the absorption tower (1) through a recooler (8), and the recooler (8) is used for further reducing a part of the mixed liquor branched from the reflux condenser (9).
7. The carbon dioxide phase-change isothermal absorption trapping technology according to claim 1, wherein the separation liquid in the decanter (2) is separated from CO 2 The rich liquid can be separated into upper layer and lower layer of CO due to different physical and chemical properties of different solutions 2 A rich liquid; the upper layer after phase separation can be CO 2 Rich liquid and separating liquid in the lower layer.
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| CN202210569993.9A CN117138553A (en) | 2022-05-24 | 2022-05-24 | Isothermal carbon dioxide absorption and trapping technology |
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| CN202210569993.9A CN117138553A (en) | 2022-05-24 | 2022-05-24 | Isothermal carbon dioxide absorption and trapping technology |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102553396A (en) * | 2011-12-23 | 2012-07-11 | 武汉凯迪工程技术研究总院有限公司 | Method for trapping carbon dioxide in flue gas of power station with high efficiency and low energy consumption and equipment adopting same |
| CN103977683A (en) * | 2014-04-30 | 2014-08-13 | 天津大学 | Method and device for reducing regeneration energy consumption of decarburization absorption liquid |
| CN104874271A (en) * | 2014-02-28 | 2015-09-02 | 株式会社东芝 | Carbon dioxide recovery apparatus and carbon dioxide recovery method |
| CN105032126A (en) * | 2014-04-18 | 2015-11-11 | 株式会社东芝 | Carbon dioxide recovery apparatus and carbon dioxide recovery method |
| CN105396447A (en) * | 2015-10-21 | 2016-03-16 | 中石化节能环保工程科技有限公司 | Double phase absorption system for removing CO2 from flue gas |
| US20180193798A1 (en) * | 2015-08-21 | 2018-07-12 | Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd.) | Gas treatment system and gas treatment method |
| CN114159954A (en) * | 2021-12-07 | 2022-03-11 | 兰州理工大学 | Phase change solvent coupling membrane separation flue gas CO2System and method |
-
2022
- 2022-05-24 CN CN202210569993.9A patent/CN117138553A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102553396A (en) * | 2011-12-23 | 2012-07-11 | 武汉凯迪工程技术研究总院有限公司 | Method for trapping carbon dioxide in flue gas of power station with high efficiency and low energy consumption and equipment adopting same |
| CN104874271A (en) * | 2014-02-28 | 2015-09-02 | 株式会社东芝 | Carbon dioxide recovery apparatus and carbon dioxide recovery method |
| CN105032126A (en) * | 2014-04-18 | 2015-11-11 | 株式会社东芝 | Carbon dioxide recovery apparatus and carbon dioxide recovery method |
| CN103977683A (en) * | 2014-04-30 | 2014-08-13 | 天津大学 | Method and device for reducing regeneration energy consumption of decarburization absorption liquid |
| US20180193798A1 (en) * | 2015-08-21 | 2018-07-12 | Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd.) | Gas treatment system and gas treatment method |
| CN105396447A (en) * | 2015-10-21 | 2016-03-16 | 中石化节能环保工程科技有限公司 | Double phase absorption system for removing CO2 from flue gas |
| CN114159954A (en) * | 2021-12-07 | 2022-03-11 | 兰州理工大学 | Phase change solvent coupling membrane separation flue gas CO2System and method |
Non-Patent Citations (1)
| Title |
|---|
| 陆诗建等: ""烟气CO2捕集热能梯级利用节能工艺耦合优化"", 《化工进展》, vol. 39, no. 02, 14 November 2019 (2019-11-14), pages 728 - 737 * |
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