CN112933886A - Carbon dioxide entrapment waste heat flash regeneration system - Google Patents
Carbon dioxide entrapment waste heat flash regeneration system Download PDFInfo
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- CN112933886A CN112933886A CN202110360502.5A CN202110360502A CN112933886A CN 112933886 A CN112933886 A CN 112933886A CN 202110360502 A CN202110360502 A CN 202110360502A CN 112933886 A CN112933886 A CN 112933886A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 230000008929 regeneration Effects 0.000 title claims abstract description 86
- 238000011069 regeneration method Methods 0.000 title claims abstract description 86
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 49
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 47
- 239000002918 waste heat Substances 0.000 title claims abstract description 29
- 238000010521 absorption reaction Methods 0.000 claims abstract description 105
- 239000007788 liquid Substances 0.000 claims abstract description 92
- 239000007789 gas Substances 0.000 claims abstract description 65
- 238000001816 cooling Methods 0.000 claims abstract description 33
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 16
- 239000003546 flue gas Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 230000002745 absorbent Effects 0.000 abstract description 6
- 239000002250 absorbent Substances 0.000 abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000032258 transport Effects 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
- B01D53/14—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
- B01D53/1412—Controlling the absorption process
-
- 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
- B01D53/14—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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
本发明提供一种二氧化碳捕集余热闪蒸再生系统，属于二氧化碳捕集技术领域，包括：吸收塔、再生塔和再沸器，所述吸收塔上具有自循环管道，所述自循环管道的一端通向吸收塔的塔底吸收液内，所述自循环管道的另一端通向吸收塔的塔顶内腔中，所述自循环管道在进入吸收塔的塔顶内腔之前连接有闪蒸罐；所述再生塔的粗气排气口后端连通有第一冷却换热器，所述第一冷却换热器与闪蒸罐连通；本发明的二氧化碳捕集余热闪蒸再生系统，在再生塔的粗气排气口后端连通有第一冷却换热器，该第一冷却换热器可用于对自循环管内的吸收液进行加热，从而对再生塔的排气余热进行回收，被加热的自循环吸收剂在闪蒸罐内闪蒸实现吸收剂部分再生，达到节能的目的。
The invention provides a carbon dioxide capture waste heat flash regeneration system, belonging to the technical field of carbon dioxide capture, comprising: an absorption tower, a regeneration tower and a reboiler, the absorption tower is provided with a self-circulation pipeline, and one end of the self-circulation pipeline is provided Leading to the absorption liquid at the bottom of the absorption tower, the other end of the self-circulating pipeline leads to the inner cavity of the tower top of the absorption tower, and the self-circulating pipeline is connected with a flash tank before entering the inner cavity of the tower top of the absorption tower ; The rear end of the crude gas exhaust port of the regeneration tower is communicated with a first cooling heat exchanger, and the first cooling heat exchanger is communicated with the flash tank; the carbon dioxide capture waste heat flash regeneration system of the present invention, in the regeneration The rear end of the crude gas exhaust port of the tower is connected with a first cooling heat exchanger. The first cooling heat exchanger can be used to heat the absorption liquid in the self-circulating pipe, so as to recover the exhaust heat of the regeneration tower and be heated. The self-circulating absorbent is flashed in the flash tank to achieve partial regeneration of the absorbent and achieve the purpose of energy saving.
Description
Technical Field
The invention relates to the technical field of carbon dioxide capture, in particular to a flash evaporation regeneration system for carbon dioxide capture waste heat.
Background
CCS technology is an abbreviation for Carbon Capture and Storage, a technology that captures and sequesters Carbon dioxide (CO 2). The CCS technology is a carbon capture technology that separates carbon dioxide produced by industry and related energy industries, and then transports and stores the separated carbon dioxide to places isolated from the atmosphere, such as the sea floor or the underground, by means of carbon storage.
CCS technology consists of two parts, carbon capture and carbon sequestration. Among them, the carbon capture technology is applied to industries such as oil refining and chemical industry for the earliest time. Due to the high concentration and pressure of CO2 emitted by these industries, the capture cost is not high. The opposite is true for CO2 emitted from coal-fired power plants, and carbon dioxide capture from power plant emissions has problems of high energy consumption and high cost.
The energy consumption of the carbon dioxide capture system is mainly the regeneration steam consumption of the regeneration tower, because the temperature difference between the lean solution at the bottom of the regeneration tower and the regeneration gas at the top of the regeneration tower is not large, the heat contained in the lean solution at the bottom of the regeneration tower and the heat contained in the regeneration gas at the top of the regeneration tower are relatively close, if the heat is recovered by the rich solution at the bottom of the absorption tower, the heat recovery of one stream in the lean solution at the bottom of the tower or the regenerator at the top of the tower can only be realized, the temperature difference between the heated rich solution and the temperature of the other stream is not large, the heat recovery of the other stream can not be realized, and the other.
Disclosure of Invention
Therefore, the technical problem to be solved by the invention is to overcome the defect of overhigh energy consumption of the carbon dioxide capturing system for the power plant in the prior art, and thus provide a flash evaporation regeneration system for the carbon dioxide capturing waste heat.
In order to solve the above technical problem, the present invention provides a flash evaporation regeneration system for carbon dioxide capture waste heat, comprising:
one end of the absorption tower is communicated with a flue gas outlet of the power plant, the absorption tower is suitable for containing absorption liquid, and the absorption liquid in the absorption tower absorbs carbon dioxide in the flue gas and then becomes rich liquid; the absorption tower is provided with a self-circulation pipeline, one end of the self-circulation pipeline is communicated into the tower bottom absorption liquid of the absorption tower, the other end of the self-circulation pipeline is communicated into the tower top inner cavity of the absorption tower, and the self-circulation pipeline is connected with a flash tank before entering the tower top inner cavity of the absorption tower;
the regeneration tower is communicated with rich liquid in the absorption tower through a pipeline, a crude gas exhaust port is formed in the regeneration tower, a first cooling heat exchanger is communicated with the rear end of the crude gas exhaust port of the regeneration tower, a cooling water inlet of the first cooling heat exchanger is communicated with a pipe section of a self-circulation pipeline of the absorption tower, which leads to absorption liquid at the bottom of the tower, and a cooling water outlet of the first cooling heat exchanger is communicated with a flash tank on the self-circulation pipeline of the absorption tower;
and the reboiler is communicated with the regeneration tower and is used for vaporizing the rich liquid entering the regeneration tower into a gas-liquid two-phase state, wherein the liquid phase is changed into a lean liquid, and the gas phase is discharged from a crude gas exhaust port of the regeneration tower.
Optionally, the self-circulation pipeline of the absorption tower is provided with a self-circulation heat exchanger before the pipeline is led to the tower top inner cavity of the absorption tower and after the flash tank.
Optionally, a spraying device is arranged on an outlet of one end of the self-circulation pipeline, which leads to the tower top inner cavity of the absorption tower.
Optionally, a tail gas emptying port is arranged on the absorption tower, a tail gas heat exchanger is arranged at the front end of the tail gas emptying port, and the tail gas heat exchanger is arranged above the self-circulation pipeline.
Optionally, a demister is further arranged at the front end of the tail gas evacuation port of the absorption tower.
Optionally, a demister is arranged at the front end of the raw gas exhaust port of the regeneration tower.
Optionally, the crude gas exhaust port of the regeneration tower is communicated with a gas-liquid separator, and the separated water of the gas-liquid separator flows back into the regeneration tower.
Optionally, the method further comprises: and the separated water discharged from the gas-liquid separator firstly enters the reflux liquid storage tank and then flows back to the regeneration tower.
Optionally, the flash evaporation tank is provided with a flash evaporation gas outlet which is communicated with the gas-liquid separator.
Optionally, a second cooling heat exchanger is further disposed at the rear end of the first cooling heat exchanger, and a flash gas exhaust port of the flash tank enters the gas-liquid separator after passing through the second cooling heat exchanger.
The technical scheme of the invention has the following advantages:
1. the flash evaporation regeneration system for the carbon dioxide trapping waste heat is characterized in that a first cooling heat exchanger is communicated with the rear end of a crude gas exhaust port of a regeneration tower, the first cooling heat exchanger is communicated with a self-circulation pipeline of an absorption tower and is used for heating absorption liquid in the self-circulation pipeline so as to recover the exhaust waste heat of the regeneration tower, the heated self-circulation absorbent flashes in a flash evaporation tank to realize partial regeneration of the absorbent, and under the condition of a certain regeneration amount, the regeneration system can reduce the regeneration degree of rich liquid sent to the regeneration tower so as to achieve the purpose of energy conservation.
2. According to the flash evaporation regeneration system for the carbon dioxide trapping waste heat, the absorption liquid of the absorption tower is heated through the first cooling heat exchanger and then enters the flash evaporation tank, so that part of carbon dioxide is desorbed, and the efficiency of the absorption tower is improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic diagram of a carbon dioxide capture waste heat flash regeneration system provided in an embodiment of the present invention.
Description of reference numerals:
1. a flash tank; 2. an absorption tower; 3. a regeneration tower; 4. a reboiler; 5. a gas-liquid separator; 6. a crude gas vent; 7. a first cooling heat exchanger; 8. a rich liquid supply pipe; 9. a barren liquor return pipe; 10. a lean-rich liquid heat exchanger; 11. a barren liquor heat exchanger; 12. a tail gas evacuation port; 13. a tail gas heat exchanger; 14. a reflux liquid storage tank; 15. a flash evaporation gas exhaust port; 16. a second cooling heat exchanger.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. 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 invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In addition, the technical features involved in the different embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
The embodiment provides a carbon dioxide capture waste heat flash regeneration system, as shown in fig. 1, including: carbon dioxide entrapment system and waste heat flash regeneration system, including flash tank 1 in the waste heat flash regeneration system, flash tank 1 carries out waste heat recovery through carrying out waste heat recovery to the regeneration gas of discharging in the regenerator 3 from the carbon dioxide entrapment system, utilizes this waste heat to carry out partial flash distillation to the absorption liquid in the absorption tower 2 of carbon dioxide entrapment system to carbon dioxide gas in the absorption liquid carries out the part in advance and separates out, reduces reboiler 4's steam consumption, thereby reduces the consumption that the system took out steam to the steam turbine on the whole.
As shown in fig. 1, the carbon dioxide capture system includes: an absorption tower 2, a regeneration tower 3, a reboiler 4 and a gas-liquid separator 5. One end of the absorption tower 2 is used for being communicated with a flue gas outlet of a power plant, the inside of the absorption tower 2 is suitable for containing absorption liquid, and the absorption liquid in the absorption tower 2 absorbs carbon dioxide in flue gas and then becomes rich liquid; the absorption tower 2 is provided with a self-circulation pipeline, one end of the self-circulation pipeline is communicated into the tower bottom absorption liquid of the absorption tower 2, the other end of the self-circulation pipeline is communicated into the tower top inner cavity of the absorption tower 2, the self-circulation pipeline is provided with a self-circulation pump, the self-circulation pump is used for forcibly pumping the absorption liquid at the bottom of the absorption tower 2 to the upper part or the middle part of the absorption tower 2 and uniformly dispersing the absorption liquid in the absorption tower 2 in a spraying mode, and therefore the absorption effect of the absorption liquid on carbon dioxide in the flue gas is improved.
As shown in fig. 1, the regeneration tower 3 is communicated with the rich liquid in the absorption tower 2 through a pipeline, the regeneration tower 3 is provided with a crude gas exhaust port 6, a first cooling heat exchanger 7 is communicated with the rear end of the crude gas exhaust port 6 of the regeneration tower 3, and the first cooling heat exchanger 7 is used for reducing the temperature of the regenerated gas discharged from the crude gas exhaust port 6, so that the waste heat of the regenerated gas can be conveniently recovered. The regeneration tower 3 is communicated with a reboiler 4, the reboiler 4 is used for vaporizing the rich liquid entering the regeneration tower 3 into a gas-liquid two-phase, wherein the liquid phase is changed into a lean liquid, and the gas phase is discharged from a crude gas exhaust port 6 of the regeneration tower 3. The heating steam of the reboiler 4 is extracted from a steam turbine, and the carbon dioxide gas is separated out by heating the absorbing liquid containing carbon dioxide by the steam turbine extraction.
As shown in fig. 1, the regeneration tower 3 is communicated with the rich liquid in the absorption tower 2 through a rich liquid supply pipe 8, one end of the rich liquid supply pipe 8 extends into the absorption tower 2 from the bottom of the absorption tower 2, the other end of the rich liquid supply pipe 8 extends into the regeneration tower 3 from the top of the regeneration tower 3, the rich liquid enters the top of the regeneration tower 3 from the absorption tower 2, and is sprayed downward from the inside of the top of the regeneration tower 3 in a spraying manner, so that the carbon dioxide gas contained in the rich liquid is precipitated. In addition, a lean liquid return pipe 9 is connected between the regeneration tower 3 and the absorption tower 2, one end of the lean liquid return pipe 9 is communicated to the inside of the bottom end of the regeneration tower 3, and the other end of the lean liquid return pipe 9 is communicated to the inside of the top of the absorption tower 2, and the lean liquid is sprayed in the top of the absorption tower 2 in a spraying mode. The lean liquid return pipe 9 and the rich liquid supply pipe 8 are connected by a lean-rich liquid heat exchanger 10, that is, after the hot lean liquid in the lean liquid return pipe 9 transfers heat to the rich liquid in the rich liquid supply pipe 8 by the lean-rich liquid heat exchanger 10, the lean liquid in the lean liquid return pipe 9 returns to the absorption tower 2, so as to recover the heat of the lean liquid in the regeneration tower 3. The barren liquor return pipe 9 is also provided with a barren liquor heat exchanger 11, and the barren liquor is cooled through the barren liquor heat exchanger 11 to recover the absorption of the absorption liquid on the carbon dioxide in the flue gas.
As shown in fig. 1, the self-circulation pipeline on the absorption tower 2 leads to a first cooling heat exchanger 7 at the top end of the regeneration tower 3 after extending out from the bottom of the absorption tower 2. The absorption liquid extracted from the bottom of the absorption tower 2 by the self-circulation pipeline is used as cooling water of the first cooling heat exchanger 7, a cooling water outlet of the first cooling heat exchanger 7 is communicated with the flash tank 1, and then the bottom of the flash tank 1 is communicated with an inner cavity of the top of the absorption tower 2, so that the absorption liquid is returned to the absorption tower 2. Carbon dioxide in part of the absorption liquid is flashed out by the flash tank 1, so that the absorption capacity of the absorption liquid is recovered in advance, and the efficiency of the absorption tower 2 is increased.
As shown in fig. 1, a spraying device is arranged at an outlet of one end of the self-circulation pipeline, which leads to the inner cavity of the tower top of the absorption tower 2, and the spraying device is used for uniformly distributing the absorption liquid in the absorption tower 2, so that the absorption liquid can absorb the carbon dioxide in the flue gas conveniently.
As shown in fig. 1, the absorption tower 2 is provided with a tail gas vent 12, a tail gas heat exchanger 13 is arranged at the front end of the tail gas vent 12, and the tail gas heat exchanger 13 is arranged above the self-circulation pipeline. The front end of the tail gas exhaust port 12 of the absorption tower 2 is also provided with a demister, and the demister is arranged between the tail gas heat exchanger 13 and the tail gas exhaust port 12 and is used for demisting the discharged flue gas so as to reduce the water content in the flue gas. Specifically, the tail gas heat exchanger 13 is a wide-channel plate heat exchanger, the escape rate of the absorbent from the top of the absorption tower 2 can be reduced through the plate heat exchanger, and the wide-channel plate heat exchanger has the advantages of small heat exchange end difference, large heat exchange coefficient and the like. The cooling circulating water exchanges heat with the flue gas through the partition wall, the temperature of the flue gas at the top of the absorption tower 2 is saturated flue gas, water is separated out after the heat exchange with the cooling circulating water, absorption liquid carried in the flue gas is also separated out, and the separated water and the absorbent flow back to the absorption tower 2 again along the heat exchange wall of the plate heat exchanger for recycling. In addition, the absorption tower 2 is also provided with a demister between the tail gas heat exchanger 13 and the tail gas exhaust port 12, and the demister is used for reducing the water content in the flue gas.
As shown in fig. 1, a demister is provided at the front end of the raw gas exhaust port 6 of the regeneration tower 3, and the water content of the discharged regeneration gas is reduced by the demister. And a crude gas exhaust port 6 of the regeneration tower 3 is communicated with a gas-liquid separator 5, and separated water of the gas-liquid separator 5 flows back into the regeneration tower 3. Specifically, still include: and a reflux liquid storage tank 14, wherein the separated water discharged from the gas-liquid separator 5 by the reflux liquid storage tank 14 firstly enters the reflux liquid storage tank 14 and then flows back to the regeneration tower 3.
As shown in fig. 1, the flash tank 1 is provided with a flash gas discharge port 15, and the flash gas discharge port 15 communicates with the gas-liquid separator 5 to separate carbon dioxide gas flashed from the flash tank 1 into steam and water. Preferably, a second cooling heat exchanger 16 is further arranged at the rear end of the first cooling heat exchanger 7, the flash gas exhaust port 15 of the flash tank 1 enters the gas-liquid separator 5 after passing through the second cooling heat exchanger 16, and the second cooling heat exchanger 16 is used for further cooling the carbon dioxide gas so as to recover waste heat and facilitate subsequent steam-water separation.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications of the invention may be made without departing from the scope of the invention.
Claims (10)
1. A carbon dioxide capture waste heat flash regeneration system, comprising:
one end of the absorption tower (2) is communicated with a flue gas outlet of a power plant, the absorption tower is suitable for containing absorption liquid, and the absorption liquid in the absorption tower (2) absorbs carbon dioxide in the flue gas and then becomes rich liquid; the absorption tower (2) is provided with a self-circulation pipeline, one end of the self-circulation pipeline is communicated into the tower bottom absorption liquid of the absorption tower (2), the other end of the self-circulation pipeline is communicated into the tower top inner cavity of the absorption tower (2), and the self-circulation pipeline is connected with a flash tank (1) before entering the tower top inner cavity of the absorption tower (2);
the regeneration tower (3) is communicated with rich liquid in the absorption tower (2) through a pipeline, a crude gas exhaust port (6) is formed in the regeneration tower (3), a first cooling heat exchanger (7) is communicated with the rear end of the crude gas exhaust port (6) of the regeneration tower (3), a cooling water inlet of the first cooling heat exchanger (7) is communicated with a pipe section of a self-circulation pipeline of the absorption tower (2) leading to absorption liquid at the tower bottom, and a cooling water outlet of the first cooling heat exchanger (7) is communicated with a flash tank (1) on the self-circulation pipeline of the absorption tower (2);
and the reboiler (4) is communicated with the regeneration tower (3) and is used for vaporizing the rich liquid entering the regeneration tower (3) into a gas-liquid two-phase state, wherein the liquid phase is changed into a lean liquid, and the gas phase is discharged from a crude gas exhaust port (6) of the regeneration tower (3).
2. The carbon dioxide capture waste heat flash regeneration system according to claim 1, characterized in that the self-circulation pipeline of the absorption tower (2) is provided with a self-circulation heat exchanger before the pipeline is led to the top inner cavity of the absorption tower (2) and after the flash tank (1).
3. The flash evaporation and regeneration system for carbon dioxide capture waste heat according to claim 1, wherein a spraying device is arranged on an outlet of one end of the self-circulation pipeline, which leads to the inner cavity of the tower top of the absorption tower (2).
4. The flash evaporation and regeneration system for carbon dioxide capture waste heat according to claim 1, wherein the absorption tower (2) is provided with a tail gas evacuation port (12), the front end of the tail gas evacuation port (12) is provided with a tail gas heat exchanger (13), and the tail gas heat exchanger (13) is arranged above the self-circulation pipeline.
5. The flash regeneration system for carbon dioxide capture waste heat according to claim 4, characterized in that a demister is further arranged at the front end of the tail gas exhaust port (12) of the absorption tower (2).
6. The flash regeneration system for carbon dioxide capture waste heat according to claim 1, characterized in that a demister is arranged at the front end of the crude gas exhaust port (6) of the regeneration tower (3).
7. The flash regeneration system for carbon dioxide capture waste heat according to claim 1, wherein the crude gas exhaust port (6) of the regeneration tower (3) is communicated with a gas-liquid separator (5), and separated water of the gas-liquid separator (5) flows back into the regeneration tower (3).
8. The carbon dioxide capture waste heat flash regeneration system of claim 7, further comprising: and a reflux liquid storage tank (14), wherein the separated water discharged from the gas-liquid separator (5) firstly enters the reflux liquid storage tank (14) and then refluxes into the regeneration tower (3).
9. The carbon dioxide capture waste heat flash regeneration system according to any one of claims 1-8, wherein the flash tank (1) is provided with a flash gas vent (15), and the flash gas vent (15) is communicated with the gas-liquid separator (5).
10. The flash regeneration system for the carbon dioxide capture waste heat according to claim 9, characterized in that a second cooling heat exchanger (16) is further arranged at the rear end of the first cooling heat exchanger (7), and a flash gas exhaust port (15) of the flash tank (1) passes through the second cooling heat exchanger (16) and then enters the gas-liquid separator (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110360502.5A CN112933886B (en) | 2021-04-02 | 2021-04-02 | Carbon dioxide entrapment waste heat flash distillation regeneration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110360502.5A CN112933886B (en) | 2021-04-02 | 2021-04-02 | Carbon dioxide entrapment waste heat flash distillation regeneration system |
Publications (2)
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| CN114100324A (en) * | 2021-12-10 | 2022-03-01 | 南京中昙气体有限公司 | Carbon dioxide capture process and equipment |
| CN114225653A (en) * | 2021-12-16 | 2022-03-25 | 中国华电科工集团有限公司 | A graded regeneration tower and carbon dioxide capture system with the graded regeneration tower |
| CN116585854A (en) * | 2023-05-17 | 2023-08-15 | 北京华源泰盟节能设备有限公司 | A carbon capture system with heat recovery |
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| CN112933886B (en) | 2025-01-17 |
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