CN116272263A - Flue gas carbon dioxide entrapment system - Google Patents

Flue gas carbon dioxide entrapment system Download PDF

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Publication number
CN116272263A
CN116272263A CN202211628050.5A CN202211628050A CN116272263A CN 116272263 A CN116272263 A CN 116272263A CN 202211628050 A CN202211628050 A CN 202211628050A CN 116272263 A CN116272263 A CN 116272263A
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CN
China
Prior art keywords
liquid
rich liquid
lean
cooler
regeneration
Prior art date
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Pending
Application number
CN202211628050.5A
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Chinese (zh)
Inventor
徐冬
余学海
韩涛
冯蕾
刘毅
董文峰
张帅
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Qingdao University of Science and Technology
National Energy Group New Energy Technology Research Institute Co Ltd
Original Assignee
Qingdao University of Science and Technology
National Energy Group New Energy Technology Research Institute Co Ltd
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Application filed by Qingdao University of Science and Technology, National Energy Group New Energy Technology Research Institute Co Ltd filed Critical Qingdao University of Science and Technology
Priority to CN202211628050.5A priority Critical patent/CN116272263A/en
Publication of CN116272263A publication Critical patent/CN116272263A/en
Pending legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D21/0001—Recuperative heat exchangers
    • F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
    • 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
    • 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

Abstract

The invention relates to the technical field of flue gas treatment and discloses a flue gas carbon dioxide trapping system, which comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1; the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters the semi-rich liquid cooler 14 and is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13. The system provides a rich liquid fractional flow process, and combines a water washing section condensate water reflux process to realize comprehensive utilization of condensate water of a trapping system, and meanwhile, the water washing section condensate water is refluxed to a regeneration tower to reduce the temperature of regenerated gas, recover the heat of the regenerated gas and reduce the regeneration energy consumption.

Description

Flue gas carbon dioxide entrapment system
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to a flue gas carbon dioxide trapping system.
Background
The flue gas of the power plant in the chemical absorption method is subjected to the processes of cooling, dust removal, deep desulfurization, denitration and the like by a pretreatment tower, enters an absorption tower to be in countercurrent contact with lean liquid of an absorption liquid for heat and mass transfer, and the flue gas after decarburization is discharged into the atmosphere through the top of the absorption tower; the absorption liquid for absorbing the carbon dioxide in the flue gas is called rich liquid, cold rich liquid at the bottom of the absorption tower is heated by a lean-rich liquid heat exchanger and then is sent into a desorption tower, a reboiler arranged at the bottom of the desorption tower generates secondary steam to drive the regeneration of the hot rich liquid, and the regeneration gas is cooled by a regeneration gas cooler and then is subjected to compression, drying, liquefaction and other processes. The tail gas of the absorption tower enters a water washing section for washing and cooling, and condensed water flows back to the absorption tower. And (3) the regenerated gas of the regeneration tower flows back to the regeneration tower after passing through a regenerated gas cooler and gas-liquid separation. In the prior art, the absorption liquid is not fully cooled, the temperature of the absorption liquid is higher, the effect of absorbing carbon dioxide in the flue gas is poor, and the waste heat of the regenerated gas is not fully utilized.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention provides a flue gas carbon dioxide trapping system, which provides a rich liquid stage flow process and combines a water washing section condensate water reflux process to realize comprehensive utilization of condensed water of the trapping system, and meanwhile, the water washing section condensate water is refluxed to a regeneration tower to reduce the temperature of regenerated gas, recover the heat of the regenerated gas and reduce the regeneration energy consumption.
In order to achieve the above object, the present invention provides a carbon dioxide capturing system in flue gas, comprising an absorption tower for absorbing carbon dioxide in flue gas and a regeneration tower for regenerating cold rich liquid from the bottom of the absorption tower; the absorption tower comprises an absorption section and a water washing section which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector is arranged in the middle of the absorption section, liquid in the semi-rich liquid collector enters the semi-rich liquid cooler and is sprayed into the lower part of the absorption section through a first nozzle arranged at the lower part of the semi-rich liquid collector.
Preferably, the system further comprises a water washing liquid supply unit, wherein the water washing liquid supply unit comprises a water washing liquid storage tank and a water washing liquid cooler, water washing liquid in the water washing liquid storage tank is introduced into the water washing liquid cooler, and cooling water washing liquid at the outlet end of the water washing liquid cooler is introduced into the water washing section for recycling.
Preferably, the system further comprises a water wash pump, through which water wash in the water wash tank is led into the water wash cooler.
Preferably, a water washing liquid collector is arranged at the bottom of the water washing section, and liquid in the water washing liquid collector enters the water washing liquid storage tank.
Preferably, the system further comprises a cooling storage tank, and the cooling water washing liquid at the outlet end of the water washing liquid cooler enters the cooling storage tank, is mixed with the liquid in the semi-rich liquid collector and enters the semi-rich liquid cooler.
Preferably, the system further comprises a semi-rich liquid pump through which cooling water wash from the cooling storage tank is fed into the semi-rich liquid cooler.
Preferably, the system comprises a regeneration gas waste heat recovery unit, the regeneration gas waste heat recovery unit comprises a regeneration gas cooler and a gas-liquid separator, the regeneration gas flowing out of the top of the regeneration tower is input into the regeneration gas cooler, the cooled regeneration gas is input into the gas-liquid separator, and the liquid at the outlet end of the gas-liquid separator is input into the regeneration tower from the upper part of the regeneration tower.
Preferably, the system further comprises a water pump through which liquid at the outlet end of the gas-liquid separator is fed into the regeneration tower.
Preferably, a second nozzle is arranged at the upper part of the regeneration tower, and the liquid at the outlet end of the gas-liquid separator is input into the regeneration tower through the second nozzle.
Preferably, the cooling water wash liquid from the outlet end of the water wash cooler is partially fed into the gas-liquid separator, mixed with the cooled regeneration gas from the outlet end of the regeneration gas cooler and fed into the regeneration tower from the upper part of the regeneration tower.
Preferably, the system comprises a lean-rich liquid heat exchanger, wherein cold rich liquid from the bottom of the absorption tower exchanges heat with hot lean liquid from the bottom of the regeneration tower, and hot rich liquid output from a hot rich liquid outlet end of the lean-rich liquid heat exchanger is input into the regeneration tower from the middle part of the regeneration tower.
Preferably, the system further comprises a lean liquid pump through which the hot lean liquid from the bottom of the regeneration tower is passed into the lean-rich liquid heat exchanger.
Preferably, the system further comprises a rich liquid pump through which cold rich liquid from the bottom of the absorption tower is introduced into the lean rich liquid heat exchanger.
Preferably, a third nozzle is arranged in the middle of the regeneration tower, and the hot rich liquid output from the hot rich liquid outlet end of the lean rich liquid heat exchanger is input into the regeneration tower from the middle of the regeneration tower through the third nozzle.
Preferably, the system further comprises a lean liquor cooler, wherein the lean liquor output by the lean liquor outlet end of the lean-rich liquor heat exchanger enters the lean liquor cooler for heat exchange, and the cold lean liquor of the cold lean liquor outlet end of the lean liquor cooler is input into the absorption tower from the top of the absorption section.
Preferably, a fourth nozzle is provided at the top of the absorption section, and the cold lean solution at the cold lean solution outlet end of the lean solution cooler is introduced into the absorption tower from the top of the absorption section through the fourth nozzle.
Compared with the prior art, the invention has at least the following advantages:
(1) The tail gas washing condensed water of the absorption tower and the condensed water of the regenerated gas are mixed and flow back to the regeneration tower, so that the heat recovery rate of the regenerated gas is improved;
(2) The tail gas washing cooling water of the absorption tower is combined with the interstage cooling to improve the interstage cooling process effect.
Drawings
FIG. 1 is a schematic diagram of a flue gas carbon dioxide capture system according to the present invention.
Description of the reference numerals
1 an absorption tower; 2 a regeneration tower; 3, a lean-rich liquid heat exchanger; 4 lean liquid cooler; 11 absorption section; 12, washing the section with water; 13 a semi-rich liquid collector; 14 a semi-rich liquid cooler; 15 a first nozzle; a 16 water washing liquid supply unit; 17 a water washing liquid collector; 18 a fourth nozzle; 19 a water washing pump; 20 semi-rich liquid pumps; a regenerated gas waste heat recovery unit 21; 22 a second nozzle; 23 a third nozzle; 31 a hot rich liquor outlet end; 32 lean liquid outlet end; 33 lean liquid pump; 34 a rich liquid pump; 41 a cold lean liquid outlet end; 211 a regeneration gas cooler; 212 a gas-liquid separator; 213 water pump; 161 water wash tank; 162 water washing liquid cooler; 163 cool the reservoir.
Detailed Description
The following describes specific embodiments of the present invention in detail with reference to the drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
The invention provides a flue gas carbon dioxide capturing system, which is shown in fig. 1 and comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1.
In the flue gas carbon dioxide capturing system, the flue gas enters from the bottom of the absorption tower 1, contacts with the absorption liquid in the absorption tower 1 in a countercurrent manner, the cold rich liquid absorbing carbon dioxide in the flue gas is gathered at the bottom of the absorption tower 1, the cold rich liquid is input into the regeneration tower 2 from top to bottom and falls into the bottom of the regeneration tower 2 for regeneration through a reboiler, then the regenerated gas containing carbon dioxide and water vapor flows out from the top of the regeneration tower 2, and the bottom of the regeneration tower is the hot lean liquid after carbon dioxide is removed.
In the flue gas carbon dioxide capturing system of the present invention, the absorption tower 1 includes an absorption section 11 and a water washing section 12 for sequentially treating flue gas from bottom to top, a semi-rich liquid collector 13 is disposed in the middle of the absorption section 11, and liquid in the semi-rich liquid collector 13 enters the semi-rich liquid cooler 14 and sprays the cooled semi-rich liquid into the lower part of the absorption section 11 through a first nozzle 15 disposed at the lower part of the semi-rich liquid collector 13.
In the specific implementation process, the flue gas introduced from the bottom of the absorption tower 1 sequentially absorbs carbon dioxide in the flue gas in the absorption section 11, and then the flue gas with carbon dioxide droplets continuously enters the water washing section 12 upwards for water washing, so as to absorb carbon dioxide carried in the flue gas and absorb the flue gas at the same time; the semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, so that semi-rich liquid obtained by absorbing a small amount of carbon dioxide at the upper part of the absorption section 11 can be collected, then the semi-rich liquid is cooled outside the absorption tower 1 through the semi-rich liquid cooler 14, finally the cooled semi-rich liquid is sprayed into the absorption section 11 through the first nozzle 15, the adsorption capacity of the cooled semi-rich liquid on carbon dioxide is enhanced, and the cooled semi-rich liquid is continuously mixed with the flue gas containing high-concentration carbon dioxide downwards, so that the adsorption effect can be improved. By adopting the interstage cooling mode, the adsorption effect of carbon dioxide in the flue gas can be improved.
In the flue gas carbon dioxide capturing system according to the present invention, in a specific embodiment, the system further includes a water wash liquid supply unit 16, the water wash liquid supply unit 16 includes a water wash liquid storage tank 161 and a water wash liquid cooler 162, the water wash liquid in the water wash liquid storage tank 161 is led into the water wash liquid cooler 162, and the cooling water wash liquid at the outlet end of the water wash liquid cooler 162 is led into the water wash section 12 for recycling. The temperature of the water washing liquid in the water washing liquid storage tank 161 is about 40 ℃, the temperature of the water washing liquid is about 25 ℃ after the water washing liquid is introduced into the water washing liquid cooler 162 for cooling, and the cooled water washing liquid is introduced into the water washing section 12 for recycling, so that the water washing effect of the flue gas can be improved, and carbon dioxide can be removed better.
In a specific embodiment, the system further comprises a water wash pump 19, and the water wash in the water wash tank 161 is introduced into the water wash cooler 162 through the water wash pump 19. The water wash pump 19 may be a conventional choice in the art, such as a booster pump, etc.
In the flue gas carbon dioxide capturing system according to the present invention, a water washing liquid collector 17 is disposed at the bottom of the water washing section 12, and the liquid in the water washing liquid collector 17 enters the water washing liquid storage tank 161. In the system of the invention, after the flue gas is treated by the absorption section 11, only a small amount of carbon dioxide is entrained in the flue gas, and in the water washing section 12, the solution obtained after the water washing of the flue gas by the water washing liquid only contains a small amount of carbon dioxide, so that the flue gas can be collected and recycled, thereby saving resources. A water washing liquid collector 17 is arranged at the bottom of the water washing section 12, and can collect the liquid in the water washing section 12, then the collected liquid is introduced into the water washing liquid storage tank 161 to be used as water washing liquid to be input into the water washing liquid cooler 162 for cooling, and the cooling water washing liquid at the outlet end of the water washing liquid cooler 162 is introduced into the water washing section 12 for recycling.
In the flue gas carbon dioxide capturing system according to the present invention, in a specific embodiment, the system further includes a cooling storage tank 163, and the cooling water washing liquid at the outlet end of the water washing liquid cooler 162 enters the cooling storage tank 163, is mixed with the liquid in the semi-rich liquid collector 13, and then enters the semi-rich liquid cooler 14. The cooling water washing liquid at the outlet end of the washing liquid cooler 162 may be all recycled in the washing section 12, or part of the cooling water washing liquid may be introduced into the cooling storage tank 163 to be mixed with the liquid from the semi-rich liquid collector 13, then introduced into the semi-rich liquid cooler 14 to be cooled, and introduced into the absorption section 11 to absorb carbon dioxide in the flue gas.
In particular embodiments, the system further includes a semi-rich liquid pump 20, and the cooling water wash from the cooling storage tank 163 is fed to the semi-rich liquid cooler 14 via the semi-rich liquid pump 20. The semi-rich pump 20 may be a conventional choice in the art, such as a booster pump, etc.
In the flue gas carbon dioxide capturing system, the system comprises a regeneration gas waste heat recovery unit 21, the regeneration gas waste heat recovery unit 21 comprises a regeneration gas cooler 211 and a gas-liquid separator 212, the regeneration gas flowing out of the top of the regeneration tower 2 is input into the regeneration gas cooler 211 and the cooled regeneration gas is input into the gas-liquid separator 212, and the liquid at the outlet end of the gas-liquid separator 212 is input into the regeneration tower 2 from the upper part of the regeneration tower 2. After the regeneration gas containing carbon dioxide and water vapor flowing out from the top of the regeneration tower 2 is cooled by the regeneration gas cooler 211, the water vapor is changed into liquid water, the cooled regeneration gas still has higher temperature, enters the gas-liquid separator 212 for gas-liquid separation, carbon dioxide is discharged into the atmosphere or is introduced into other places for use, and the water with higher temperature is returned to the regeneration tower 2 for recycling.
In a specific embodiment, the system further comprises a water pump 213, and the liquid at the outlet end of the gas-liquid separator 212 is input into the regeneration tower 2 through the water pump 213. The water pump 213 may be a conventional choice in the art, such as a booster pump, etc.
In a preferred embodiment, a second nozzle 22 is provided at the upper portion of the regeneration tower 2, and the liquid (i.e., liquid water) at the outlet end of the gas-liquid separator 212 is introduced into the regeneration tower 2 through the second nozzle 22. The water at the outlet end of the gas-liquid separator 212 is sprayed into the regeneration tower 2 by adopting a nozzle, so that the mass transfer specific surface area can be increased, the water and the regenerated gas can be better contacted and heat exchanged, and the water entering the regeneration tower 2 has a certain temperature, so that the waste heat in the regenerated gas is fully recovered, and the regeneration energy consumption is reduced.
In the flue gas carbon dioxide capturing system according to the present invention, in a specific embodiment, a portion of the cooling water washing liquid from the outlet end of the water washing liquid cooler 162 enters the gas-liquid separator 212, is mixed with the cooled regeneration gas from the outlet end of the regeneration gas cooler 211, and is fed into the regeneration tower 2 from the upper portion of the regeneration tower 2. In a specific embodiment, a part of the cooling water washing liquid and the cooling regeneration gas may be mixed in the gas-liquid separator 212 according to actual needs to perform gas-liquid separation, so that a part of the cooling water washing liquid absorbs heat in the regeneration gas, and then the obtained liquid is input into the regeneration tower 2, so that not only can water be provided for rich liquid regeneration, but also heat of the regeneration gas can be fully recovered, and regeneration energy consumption is reduced.
In the flue gas carbon dioxide capturing system according to the present invention, in a preferred embodiment, the system comprises a lean-rich liquid heat exchanger 3, wherein cold rich liquid from the bottom of the absorption tower 1 exchanges heat with hot lean liquid from the bottom of the regeneration tower 2 in the lean-rich liquid heat exchanger 3, and hot rich liquid output from a hot rich liquid outlet end 31 of the lean-rich liquid heat exchanger 3 is input into the regeneration tower 2 from the middle part of the regeneration tower 2. The temperature of the cold rich liquid from the bottom of the absorption tower 1 is lower, the temperature of the hot lean liquid from the bottom of the regeneration tower 2 is higher, the cold rich liquid and the hot lean liquid exchange heat in the lean rich liquid heat exchanger 3, so that the cold rich liquid becomes the hot rich liquid with higher temperature, and the hot rich liquid enters the regeneration tower 2 for regeneration, thereby saving renewable energy sources.
In a specific embodiment, the system further comprises a lean liquid pump 33, and the hot lean liquid from the bottom of the regeneration tower 2 is introduced into the lean-rich liquid heat exchanger 3 through the lean liquid pump 33. The lean liquid pump 33 may be a conventional choice in the art, such as a booster pump or the like.
In a specific embodiment, the system further comprises a rich liquid pump 34, and cold rich liquid from the bottom of the absorption tower 1 is introduced into the lean rich liquid heat exchanger 3 through the rich liquid pump 34. The rich liquid pump 34 may be a conventional choice in the art, such as a booster pump, etc.
In the flue gas carbon dioxide capturing system according to the present invention, in a specific embodiment, a third nozzle 23 is disposed in the middle of the regeneration tower 2, and the hot rich liquid output from the hot rich liquid outlet end 31 of the lean-rich liquid heat exchanger 3 is input into the regeneration tower 2 from the middle of the regeneration tower 2 through the third nozzle 23. The hot rich liquid is sprayed into the regeneration tower 2 by adopting a nozzle, so that the mass transfer specific surface area of spray particles can be increased, and the regeneration effect is improved.
In the flue gas carbon dioxide capturing system according to the present invention, in a preferred embodiment, the system further comprises a lean liquor cooler 4, the lean liquor output from the lean liquor outlet end 32 of the lean liquor heat exchanger 3 enters the lean liquor cooler 4 for heat exchange and the cold lean liquor of the cold lean liquor outlet end 41 of the lean liquor cooler 4 is input into the absorption tower 1 from the top of the absorption section 11. And the lean solution obtained through heat exchange of the lean-rich solution heat exchanger 3 is sent into the lean solution cooler 4 for cooling, and the cold lean solution (absorption solution) enters the absorption section 11 to absorb carbon dioxide in the flue gas, so that the absorption capacity of the absorption solution is stronger.
In the flue gas carbon dioxide capturing system according to the present invention, in a specific embodiment, a fourth nozzle 18 is provided at the top of the absorption section 11, and the cold lean solution of the cold lean solution outlet end 41 of the lean solution cooler 4 is fed into the absorption tower 1 from the top of the absorption section 11 through the fourth nozzle 18. The cold lean solution is sprayed into the absorption section 11 by adopting a nozzle, so that the mass transfer specific surface area of spray particles can be increased, and the absorption effect of carbon dioxide in flue gas is improved.
In one specific embodiment, the flue gas carbon dioxide capturing system comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1; the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters a semi-rich liquid cooler 14 and the cooled semi-rich liquid is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13; the system further comprises a water washing liquid supply unit 16, wherein the water washing liquid supply unit 16 comprises a water washing liquid storage tank 161 and a water washing liquid cooler 162, water washing liquid in the water washing liquid storage tank 161 is introduced into the water washing liquid cooler 162, and cooling water washing liquid at the outlet end of the water washing liquid cooler 162 is introduced into the water washing section 12 for recycling.
In a second specific embodiment, the flue gas carbon dioxide capturing system comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1; the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters a semi-rich liquid cooler 14 and the cooled semi-rich liquid is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13; the system further comprises a water washing liquid supply unit 16, the water washing liquid supply unit 16 comprises a water washing liquid storage tank 161 and a water washing liquid cooler 162, water washing liquid in the water washing liquid storage tank 161 is led into the water washing liquid cooler 162 and cooling water washing liquid at the outlet end of the water washing liquid cooler 162 is led into the water washing section 12 for recycling, the system further comprises a water washing pump 19, water washing liquid in the water washing liquid storage tank 161 is led into the water washing liquid cooler 162 through the water washing pump 19, a water washing liquid collector 17 is arranged at the bottom of the water washing section 12, and liquid in the water washing liquid collector 17 enters the water washing liquid storage tank 161.
In a third specific embodiment, the flue gas carbon dioxide capturing system comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1; the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters a semi-rich liquid cooler 14 and the cooled semi-rich liquid is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13; the system further comprises a water washing liquid supply unit 16, wherein the water washing liquid supply unit 16 comprises a water washing liquid storage tank 161 and a water washing liquid cooler 162, water washing liquid in the water washing liquid storage tank 161 is introduced into the water washing liquid cooler 162, and cooling water washing liquid at the outlet end of the water washing liquid cooler 162 is introduced into the water washing section 12 for recycling; the system further includes a cooling reservoir 163, and a portion of the cooling water wash at the outlet end of the water wash cooler 162 enters the cooling reservoir 163, mixes with the liquid in the semi-rich liquid collector 13, and enters the semi-rich liquid cooler 14.
In a fourth specific embodiment, the flue gas carbon dioxide capturing system comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1; the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters a semi-rich liquid cooler 14 and the cooled semi-rich liquid is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13; the system comprises a regeneration gas waste heat recovery unit 21, wherein the regeneration gas waste heat recovery unit 21 comprises a regeneration gas cooler 211 and a gas-liquid separator 212, the regeneration gas flowing out of the top of the regeneration tower 2 is input into the regeneration gas cooler 211, the cooled regeneration gas is input into the gas-liquid separator 212, and the liquid at the outlet end of the gas-liquid separator 212 is input into the regeneration tower 2 from the upper part of the regeneration tower 2.
In a fifth specific embodiment, the flue gas carbon dioxide capturing system comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1; the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters a semi-rich liquid cooler 14 and the cooled semi-rich liquid is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13; the system comprises a lean-rich liquid heat exchanger 3, wherein cold rich liquid from the bottom of the absorption tower 1 exchanges heat with hot lean liquid from the bottom of the regeneration tower 2 in the lean-rich liquid heat exchanger 3, and hot rich liquid output by a hot rich liquid outlet end 31 of the lean-rich liquid heat exchanger 3 is input into the regeneration tower 2 from the middle part of the regeneration tower 2; the system further comprises a rich liquid pump 34, and cold rich liquid from the bottom of the absorption tower 1 is introduced into the lean rich liquid heat exchanger 3 through the rich liquid pump 34.
In a sixth specific embodiment, the flue gas carbon dioxide capturing system comprises an absorption tower 1 and a regeneration tower 2, wherein the absorption tower 1 is used for absorbing carbon dioxide in flue gas, and the regeneration tower 2 is used for regenerating cold rich liquid from the bottom of the absorption tower 1;
the absorption tower 1 comprises an absorption section 11 and a water washing section 12 which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector 13 is arranged in the middle of the absorption section 11, liquid in the semi-rich liquid collector 13 enters the semi-rich liquid cooler 14 and is sprayed into the lower part of the absorption section 11 through a first nozzle 15 arranged at the lower part of the semi-rich liquid collector 13. The system further comprises a water washing liquid supply unit 16, wherein the water washing liquid supply unit 16 comprises a water washing liquid storage tank 161 and a water washing liquid cooler 162, water washing liquid in the water washing liquid storage tank 161 is introduced into the water washing liquid cooler 162, and cooling water washing liquid at the outlet end of the water washing liquid cooler 162 is introduced into the water washing section 12 for recycling; the system further comprises a water wash pump 19, and the water wash in the water wash tank 161 is led into the water wash cooler 162 through the water wash pump 19; a water washing liquid collector 17 is arranged at the bottom of the water washing section 12, and liquid in the water washing liquid collector 17 enters the water washing liquid storage tank 161; the system further comprises a cooling storage tank 163, wherein a cooling water washing liquid part at the outlet end of the water washing liquid cooler 162 enters the cooling storage tank 163 and is mixed with the liquid in the semi-rich liquid collector 13 and then enters the semi-rich liquid cooler 14; the system further includes a semi-rich liquid pump 20, the cooling water wash from the cooling storage tank 163 being fed into the semi-rich liquid cooler 14 through the semi-rich liquid pump 20; the system comprises a regeneration gas waste heat recovery unit 21, wherein the regeneration gas waste heat recovery unit 21 comprises a regeneration gas cooler 211 and a gas-liquid separator 212, the regeneration gas flowing out of the top of the regeneration tower 2 is input into the regeneration gas cooler 211, the cooled regeneration gas is input into the gas-liquid separator 212, and the liquid at the outlet end of the gas-liquid separator 212 is input into the regeneration tower 2 from the upper part of the regeneration tower 2; the system further comprises a water pump 213, and the liquid at the outlet end of the gas-liquid separator 212 is input into the regeneration tower 2 through the water pump 213; the upper part of the regeneration tower 2 is provided with a second nozzle 22, and the liquid at the outlet end of the gas-liquid separator 212 is input into the regeneration tower 2 through the second nozzle 22. A portion of the cooling water wash liquid from the outlet end of the water wash cooler 162 enters the gas-liquid separator 212, is mixed with the cooled regeneration gas from the outlet end of the regeneration gas cooler 211, and is fed into the regeneration tower 2 from the upper portion of the regeneration tower 2; the system comprises a lean-rich liquid heat exchanger 3, cold rich liquid from the bottom of the absorption tower 1 exchanges heat with hot lean liquid from the bottom of the regeneration tower 2 in the lean-rich liquid heat exchanger 3, and hot rich liquid output by a hot rich liquid outlet end 31 of the lean-rich liquid heat exchanger 3 is input into the regeneration tower 2 from the middle part of the regeneration tower 2. The system further comprises a lean liquid pump 33, wherein hot lean liquid from the bottom of the regeneration tower 2 is introduced into the lean-rich liquid heat exchanger 3 through the lean liquid pump 33; the system further comprises a rich liquid pump 34, and cold rich liquid from the bottom of the absorption tower 1 is introduced into the lean rich liquid heat exchanger 3 through the rich liquid pump 34. A third nozzle 23 is arranged at the middle part of the regeneration tower 2, and the hot rich liquid output by the hot rich liquid outlet end 31 of the lean rich liquid heat exchange 3 is input into the regeneration tower 2 from the middle part of the regeneration tower 2 through the third nozzle 23. The system further comprises a lean liquor cooler 4, wherein the lean liquor output from the lean liquor outlet end 32 of the lean-rich liquor heat exchanger 3 enters the lean liquor cooler 4 for heat exchange and the cold lean liquor of the cold lean liquor outlet end 41 of the lean liquor cooler 4 is input into the absorption tower 1 from the top of the absorption section 11. A fourth nozzle 18 is provided at the top of the absorption section 11, and the cold lean solution at the cold lean solution outlet end 41 of the lean solution cooler 4 is fed into the absorption tower 1 from the top of the absorption section 11 through the fourth nozzle 18.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.

Claims (16)

1. A flue gas carbon dioxide capturing system, characterized in that the system comprises an absorption tower (1) and a regeneration tower (2), wherein the absorption tower (1) is used for absorbing carbon dioxide in flue gas, and the regeneration tower (2) is used for regenerating cold rich liquid from the bottom of the absorption tower (1);
the absorption tower (1) comprises an absorption section (11) and a water washing section (12) which are sequentially used for treating flue gas from bottom to top, a semi-rich liquid collector (13) is arranged in the middle of the absorption section (11), liquid in the semi-rich liquid collector (13) enters the semi-rich liquid cooler (14) and passes through a first nozzle (15) arranged at the lower part of the semi-rich liquid collector (13) to be sprayed into the lower part of the absorption section (11).
2. The system of claim 1, further comprising a water wash supply unit (16), the water wash supply unit (16) comprising a water wash tank (161) and a water wash cooler (162),
the water washing liquid in the water washing liquid storage tank (161) is introduced into the water washing liquid cooler (162) and the cooling water washing liquid at the outlet end of the water washing liquid cooler (162) is introduced into the water washing section (12) for recycling.
3. The system according to claim 2, characterized in that the system further comprises a water wash pump (19), the water wash in the water wash tank (161) being led into the water wash cooler (162) by means of the water wash pump (19).
4. The system according to claim 2, characterized in that the bottom of the washing section (12) is provided with a washing liquid collector (17), the liquid in the washing liquid collector (17) entering the washing liquid reservoir (161).
5. The system according to claim 2, further comprising a cooling reservoir (163), wherein a portion of the cooling water wash at the outlet end of the water wash cooler (162) enters the cooling reservoir (163) and mixes with the liquid in the semi-rich liquid collector (13) before entering the semi-rich liquid cooler (14).
6. The system of claim 5, further comprising a semi-rich liquid pump (20), wherein cooling water wash from the cooling storage tank (163) is input into the semi-rich liquid cooler (14) through the semi-rich liquid pump (20).
7. The system according to claim 2, characterized in that the system comprises a regeneration gas waste heat recovery unit (21), the regeneration gas waste heat recovery unit (21) comprising a regeneration gas cooler (211) and a gas-liquid separator (212),
the regenerated gas flowing out of the top of the regeneration tower (2) is input into the regenerated gas cooler (211) and the cooled regenerated gas is input into the gas-liquid separator (212), and the liquid at the outlet end of the gas-liquid separator (212) is input into the regeneration tower (2) from the upper part of the regeneration tower (2).
8. The system according to claim 7, further comprising a water pump (213), wherein the liquid at the outlet end of the gas-liquid separator (212) is fed into the regeneration tower (2) via the water pump (213).
9. The system according to claim 7, characterized in that the regeneration tower (2) is provided with a second nozzle (22) in its upper part, and that the liquid at the outlet end of the gas-liquid separator (212) is fed into the regeneration tower (2) through the second nozzle (22).
10. The system according to claim 7, characterized in that the cooling water wash fraction from the outlet end of the water wash cooler (162) enters the gas-liquid separator (212) to be mixed with the cooled regeneration gas from the outlet end of the regeneration gas cooler (211) and is fed into the regeneration column (2) from the upper part of the regeneration column (2).
11. The system according to claim 1, characterized in that the system comprises a lean-rich liquid heat exchanger (3), wherein cold rich liquid from the bottom of the absorption tower (1) exchanges heat with hot lean liquid from the bottom of the regeneration tower (2) in the lean-rich liquid heat exchanger (3), and wherein hot rich liquid output from a hot rich liquid outlet end (31) of the lean-rich liquid heat exchanger (3) is input into the regeneration tower (2) from the middle part of the regeneration tower (2).
12. The system according to claim 11, characterized in that the system further comprises a lean liquid pump (33), through which lean liquid pump (33) the hot lean liquid from the bottom of the regeneration tower (2) is led into the lean rich liquid heat exchanger (3).
13. The system according to claim 11, characterized in that the system further comprises a rich liquid pump (34), through which rich liquid pump (34) cold rich liquid from the bottom of the absorption column (1) is led into the lean rich liquid heat exchanger (3).
14. The system according to claim 11, characterized in that a third nozzle (23) is provided in the middle of the regeneration tower (2), and that the hot rich liquid output from the hot rich liquid outlet end (31) of the lean rich liquid heat exchanger (3) is fed into the regeneration tower (2) from the middle of the regeneration tower (2) through the third nozzle (23).
15. The system according to claim 11, characterized in that the system further comprises a lean liquor cooler (4), the lean liquor output from the lean liquor outlet end (32) of the lean-rich liquor heat exchanger (3) being fed into the lean liquor cooler (4) for heat exchange and the cold lean liquor of the cold lean liquor outlet end (41) of the lean liquor cooler (4) being fed into the absorption column (1) from the top of the absorption section (11).
16. The system according to claim 15, characterized in that the top of the absorption section (11) is provided with a fourth nozzle (18), through which fourth nozzle (18) cold lean solution of the cold lean solution outlet end (41) of the lean solution cooler (4) is fed from the top of the absorption section (11) into the absorption column (1).
CN202211628050.5A 2022-12-16 2022-12-16 Flue gas carbon dioxide entrapment system Pending CN116272263A (en)

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CN202211628050.5A CN116272263A (en) 2022-12-16 2022-12-16 Flue gas carbon dioxide entrapment system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202211628050.5A CN116272263A (en) 2022-12-16 2022-12-16 Flue gas carbon dioxide entrapment system

Publications (1)

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CN116272263A true CN116272263A (en) 2023-06-23

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Family Applications (1)

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CN202211628050.5A Pending CN116272263A (en) 2022-12-16 2022-12-16 Flue gas carbon dioxide entrapment system

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CN (1) CN116272263A (en)

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