CN214914758U - Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system - Google Patents
Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system Download PDFInfo
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- CN214914758U CN214914758U CN202121092520.1U CN202121092520U CN214914758U CN 214914758 U CN214914758 U CN 214914758U CN 202121092520 U CN202121092520 U CN 202121092520U CN 214914758 U CN214914758 U CN 214914758U
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- 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
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- 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]
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Abstract
The utility model provides a carbon dioxide entrapment rich solution flash distillation regeneration waste heat recovery system belongs to carbon dioxide entrapment technical field, include: the absorption tower is communicated with the regeneration tower through the lean-rich liquid heat exchanger, the tower top of the regeneration tower is provided with a first cooling heat exchanger, and the flash tank is communicated between the lean-rich liquid heat exchanger and the first cooling heat exchanger; the utility model discloses a carbon dioxide entrapment rich liquid flash distillation regeneration waste heat recovery system utilizes the low temperature of rich liquid to retrieve the heat of the top of the tower regeneration gas of barren liquor and regeneration tower that returns in the regeneration tower in proper order to the rich liquid after will carrying out a heat transfer through the flash tank carries out the flash distillation, realizes the partial regeneration of rich liquid and the cooling of rich liquid, the rich liquid after the cooling again with regeneration tower top of the tower regeneration gas heat transfer, thereby reach the recovery to the waste heat bigger degree of returning barren liquor and top of the tower regeneration gas.
Description
Technical Field
The utility model relates to a carbon dioxide entrapment technical field specifically relates to a carbon dioxide entrapment rich solution flash distillation regeneration waste heat recovery system.
Background
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 regenerated gas at the top of the regeneration tower is not large, the heat contained in the lean solution is relatively close to that contained in the regenerated gas, if the heat of the lean solution at the bottom of the regeneration tower 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 first cooling heat exchanger can only be realized, the temperature difference between the heated rich solution and the temperature of the other stream is not large, and the heat recovery of the other stream cannot be realized.
For example, the rich liquid can be respectively connected in series with the lean-rich liquid heat exchanger and the first cooling heat exchanger of the regeneration tower, but because the lean-rich liquid heat exchanger and the first cooling heat exchanger which are sequentially connected with the rich liquid are connected in series, the heat exchange end difference of the whole heat exchanger is doubled, the temperature difference between the rich liquid and the lean liquid after heat exchange and the temperature difference between the tower top regeneration gas are limited, all heat at the tower top of the regeneration tower cannot be well utilized, a large amount of tower top heat still needs to be cooled by cooling circulating water, and almost half of the heat is wasted.
SUMMERY OF THE UTILITY MODEL
Therefore, the utility model discloses in overcoming prior art's carbon dioxide entrapment system, when adopting rich solution to retrieve barren liquor and regenerator column top of the tower waste heat, can not effectively retrieve the defect of waste heat completely to the technical problem who solves provides a carbon dioxide entrapment rich solution flash distillation regeneration waste heat recovery system.
In order to solve the technical problem, the utility model provides a carbon dioxide entrapment rich solution flash distillation regeneration waste heat recovery system, include:
the absorption tower is suitable for being communicated with the flue gas, the absorption tower is internally used for containing absorption liquid, the absorption liquid in the absorption tower absorbs carbon dioxide in the flue gas and then becomes rich liquid, a rich liquid supply pipe is connected to the absorption tower, and the rich liquid is suitable for being sent into the regeneration tower through the rich liquid supply pipe;
the regeneration tower is internally suitable for containing absorption liquid, the absorption liquid in the regeneration tower is changed into lean liquid after carbon dioxide is separated out, a lean liquid return pipe is communicated with the regeneration tower, and the lean liquid is suitable for flowing back to the absorption tower through the lean liquid return pipe;
the lean-rich liquid heat exchanger is communicated with the rich liquid supply pipe and the lean liquid return pipe respectively and is used for exchanging heat between the rich liquid in the rich liquid supply pipe and the lean liquid in the lean liquid return pipe;
the first cooling heat exchanger is arranged at the outlet of the tower top of the regeneration tower and is used for recovering waste heat of the tower top regenerated gas of the regeneration tower, the first cooling heat exchanger is communicated with the rich liquid supply pipe, and the waste heat of the regenerated gas is recovered through the rich liquid in the rich liquid supply pipe;
and the flash tank is communicated with the lean-rich liquid heat exchanger and the first cooling heat exchanger through the rich liquid supply pipe respectively, after the rich liquid in the rich liquid supply pipe is subjected to primary heat exchange in the lean-rich liquid heat exchanger or the first cooling heat exchanger, partial flash evaporation is performed in the flash tank, and then the residual rich liquid enters the lean-rich liquid heat exchanger or the first cooling heat exchanger for secondary heat exchange.
Optionally, an air supply pipeline is communicated with the flash tank, a compressor is communicated with the air supply pipeline, and the flash gas of the flash tank is suitable for being compressed by the compressor and then is conveyed to the regeneration tower.
Optionally, the rich liquid of the absorption tower passes through a lean rich liquid heat exchanger, a flash tank and a first cooling heat exchanger in sequence in the rich liquid supply pipe through a rich liquid pump, and finally enters the regeneration tower.
Optionally, a spraying device is arranged at the tower top of the absorption tower, the spraying device performs circulating spraying through a spraying pump, and an outlet of the spraying pump is suitable for being communicated with the tower top of the regeneration tower.
Optionally, the spray device comprises: the water receiving tray is arranged inside the tower top of the absorption tower, a smoke through port communicated with the tower bottom of the absorption tower is formed in the water receiving tray, and a smoke pipeline extends upwards from the smoke through port on the water receiving tray.
Optionally, the top end of the flue gas duct has a waterproof cap.
Optionally, a tail gas emptying port is arranged at the top end of the absorption tower, and a demister is arranged above the spraying device at the front end of the tail gas emptying port.
Optionally, the top end of the regeneration tower is provided with a crude gas exhaust port, the crude gas exhaust port is communicated with a gas-liquid separator, and the separated water of the gas-liquid separator flows back into the regeneration tower.
Optionally, a second cooling heat exchanger is further disposed at the rear end of the first cooling heat exchanger, and the separated water of the gas-liquid separator enters the regeneration tower after passing through the second cooling heat exchanger.
Optionally, the absorption tower is provided with a self-circulation pipeline, one end of the self-circulation pipeline is communicated with the tower bottom absorption liquid of the absorption tower, and the other end of the self-circulation pipeline is communicated with the tower top inner cavity of the absorption tower.
The utility model discloses technical scheme has following advantage:
1. the utility model provides a carbon dioxide entrapment rich liquid flash distillation regeneration waste heat recovery system utilizes the low temperature of rich liquid to retrieve the heat of the top of the tower regeneration gas of barren liquor and regeneration tower that returns in the regeneration tower in proper order to set up the flash tank between barren rich liquid heat exchanger and first cooling heat exchanger, carry out the rich liquid after the heat transfer through the flash tank and carry out the flash evaporation cooling, thereby improve and utilize the rich liquid to carry out the effect of secondary heat transfer, thereby reach the recovery to the waste heat bigger degree of returning barren liquor and top of the tower regeneration gas.
2. The utility model provides a rich liquid flash regeneration waste heat recovery system of carbon dioxide entrapment, rich liquid utilize earlier with the heat transfer of barren solution after heaies up, reentry flash tank flash distillation realizes rich liquid partial regeneration, reduces the regeneration load who is sent to the regenerator column, realizes that regenerator column steam consumption reduces. The flash evaporation gas of the rich liquid in the flash evaporation tank can be used as the tower bottom regeneration heating gas of the regeneration tower after the temperature is raised by the compressor, so that the energy consumption of the reboiler can be reduced. Specifically, the flash steam evaporated from the rich solution through the flash tank is compressed by the compressor and then is conveyed to the regeneration tower, a large amount of water vapor is contained in the flash steam, the temperature of the flash steam is further increased by pressurizing the water vapor, and therefore the flash steam plays a part of the reboiler function of the regeneration tower and reduces the energy consumption of the reboiler.
3. The utility model provides a carbon dioxide entrapment rich liquid flash distillation regeneration waste heat recovery system, the rich liquid that derives from the absorption tower at first carries out the heat exchange with the barren solution that returns from the regenerator column to satisfy the cooling to the barren solution, guarantee the absorptive capacity of absorption liquid in the absorption tower.
4. The utility model provides a carbon dioxide entrapment rich liquid flash distillation regeneration waste heat recovery system can deliver to the regenerator column with spray water among the top of the tower spray set of absorber column, reduces the top of the tower absorption liquid escape of absorber column, reduces the absorption liquid loss.
5. The utility model provides a carbon dioxide entrapment rich liquid flash distillation regeneration waste heat recovery system can further retrieve the regeneration gas waste heat with regeneration gas heat transfer in second cooling heat exchanger with vapour and liquid separator bottom liquid phase, reduces the regenerator tower energy consumption.
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 embodiments or the technical solutions in 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 for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a front view of an embodiment of a carbon dioxide capture rich liquid flash evaporation regeneration waste heat recovery system provided in an embodiment of the present invention.
Fig. 2 is a front view of another embodiment of the carbon dioxide capture rich liquid flash regeneration waste heat recovery system provided in the embodiment of the present invention.
Description of reference numerals:
1. an absorption tower; 2. a regeneration tower; 3. a tail gas evacuation port; 4. a self-circulating pipe; 5. a self-circulating pump; 6. a self-circulating heat exchanger; 7. a water pan; 8. a smoke through hole; 9. a waterproof cap; 10. a spray pump; 11. spraying a heat exchanger; 12. a demister; 13. a rich liquid supply pipe; 14. a rich liquor pump; 15. a lean-rich liquid heat exchanger; 16. a flash tank; 17. a first cooling heat exchanger; 18. a reboiler; 19. a barren liquor return pipe; 20. a barren liquor pump; 21. a crude gas vent; 22. a gas-liquid separator; 23. a second cooling heat exchanger; 24. an air supply duct; 25. a compressor.
Detailed Description
The technical solution of the present invention will be described clearly and completely with reference to the accompanying drawings, and obviously, the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to 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", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific 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 is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; 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 meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Furthermore, the technical features mentioned in the different embodiments of the invention described below can be combined with each other as long as they do not conflict with each other.
The embodiment provides a carbon dioxide capture rich solution flash regeneration waste heat recovery system, which can be used for carbon dioxide recovery of electric power or other industrial flue gas to reduce emission of carbon dioxide.
As shown in fig. 1, includes: the absorption tower comprises an absorption tower 1 and a regeneration tower 2, wherein absorption liquid is contained in the absorption tower 1, after flue gas discharged from a power plant is mixed with the absorption liquid in the absorption tower 1, the absorption liquid absorbs carbon dioxide in the flue gas and then becomes rich liquid, then the flue gas is discharged from a tail gas vent 3 at the top of the absorption tower 1, the content of the carbon dioxide in the discharged flue gas is reduced, and therefore the environment protection is facilitated.
As shown in fig. 1, the absorption tower 1 is provided with a self-circulation pipeline 4, one end of the self-circulation pipeline 4 is led into the tower bottom absorption liquid of the absorption tower 1, and the other end of the self-circulation pipeline 4 is led into the tower top inner cavity of the absorption tower 1. The self-circulation pipeline 4 is provided with a self-circulation pump 5, the self-circulation pump 5 is used for pumping the absorption liquid from the tower bottom to the tower top, then the absorption liquid falls from the tower top to the tower bottom in the absorption tower 1 under the action of gravity, and the absorption liquid is fully contacted with the flue gas in the falling process. In addition, the self-circulation pipe 4 is provided with a self-circulation heat exchanger 6, and the self-circulation heat exchanger 6 is used for reducing the temperature of the absorption liquid in the self-circulation pipe 4, thereby improving the absorption capacity of the absorption liquid.
As shown in fig. 1, a spray device is arranged at the top of the absorption tower 1, and the spray device circularly sprays spray liquid through a spray pump 10, so that saturated flue gas is cooled and condensed to form condensed water, and the condensed water contains an absorbent, thereby reducing the escape of the absorbent from the top of the absorption tower 1. Specifically, the spray device includes: the water receiving tray 7 is arranged inside the tower top of the absorption tower 1, a smoke through opening 8 communicated with the tower bottom of the absorption tower 1 is formed in the water receiving tray 7, a smoke pipeline extends upwards from the smoke through opening 8 on the water receiving tray 7, and a waterproof cap 9 is arranged at the top end of the smoke pipeline. The flue gas in the absorption tower 1 passes through the flue gas inlet 8 upwards and then passes through the flue gas channel to be led to the spraying area from the periphery of the waterproof cap 9. Then the spraying liquid in the spraying device is fully mixed with the flue gas, so that the flue gas is cooled and the absorption liquid is separated out from the flue gas, and the absorption liquid is prevented from being brought into the atmosphere by the flue gas. The water pan 7 is communicated with an inlet of a spray pump 10 through a pipeline, an outlet of the spray pump 10 is communicated with a tee joint, and spray liquid can be led to the top of the regeneration tower 2 through the tee joint, so that the spray liquid dissolved with absorption liquid is supplemented into the regeneration tower 2; in addition, the tee joint can also lead the spraying liquid to the top spraying area of the absorption tower 1 so as to lead the spraying liquid to achieve the purpose of circulating spraying, and a spraying heat exchanger 11 is connected on a spraying pipeline of the spraying liquid so as to reduce the temperature of the spraying liquid, improve the cooling effect on the flue gas and ensure the precipitation effect of the absorption liquid in the flue gas. That is, in the spraying area of the absorption tower 1, the saturated flue gas is cooled and condensed to form condensed water, the condensed water enters the water pan 7 along with the spraying liquid, the condensed water is sent to the spraying heat exchanger 11 through the spraying pump 10 for heat exchange and then is circularly sprayed, and the condensed redundant water is sent to the top of the regeneration tower 2 to be mixed with the separated water at the bottom of the gas-liquid separator 22 and then enters the top of the regeneration tower 2. In a preferred embodiment, a demister 12 is provided above the spray device at the front end of the exhaust gas vent 3 at the top end of the absorption tower 1, and the amount of water contained in the flue gas is further reduced by the demister 12.
As shown in fig. 1, a rich liquid supply pipe 13 is connected to the absorption tower 1, and the rich liquid at the bottom of the absorption tower 1 is suitable for being sent into the regeneration tower 2 through the rich liquid supply pipe 13. Specifically, the rich solution at the bottom of the absorption tower 1 is pumped out of the absorption tower 1 by a rich solution pump 14, passes through a lean rich solution heat exchanger 15, a flash tank 16 and a first cooling heat exchanger 17 in sequence, and finally enters the regeneration tower 2. In an alternative embodiment, after the rich liquid at the bottom of the absorption tower 1 is pumped out from the absorption tower 1 by the rich liquid pump 14, the following steps may be performed: sequentially passes through a first cooling heat exchanger 17, a flash tank 16 and a lean-rich liquid heat exchanger 15, and finally enters a regeneration tower 2. The flash tank 16 is located between the lean rich liquid heat exchanger 15 and the first cooling heat exchanger 17, the rich liquid is flashed by the flash tank 16, part of the rich liquid is flashed into a gaseous state, and part of the rich liquid becomes semi-rich liquid, the temperature of the semi-rich liquid is lower than that of the rich liquid before entering the flash tank 16, so that the recovery effect can be improved by performing waste heat recovery on the tower top regeneration gas of the regeneration tower 2 through the semi-rich liquid.
According to the carbon dioxide capture rich solution flash regeneration waste heat recovery system, the heat of the lean solution returned from the regeneration tower 2 and the heat of the tower top regenerated gas of the regeneration tower 2 are sequentially recovered by using the low temperature of the rich solution, the flash tank 16 is arranged between the lean and rich solution heat exchanger 15 and the first cooling heat exchanger 17, and the lean solution subjected to primary heat exchange is subjected to flash cooling through the flash tank 16, so that the effect of performing secondary heat exchange by using the rich solution is improved, and the waste heat of the lean solution and the tower top regenerated gas is recovered to a greater extent.
As shown in fig. 1, the regeneration tower 2 is adapted to accommodate an absorption liquid therein, and the absorption liquid in the regeneration tower 2 is a rich liquid flowing from the inside of the absorption tower 1 and heated to precipitate carbon dioxide and then changed into a lean liquid. Specifically, a reboiler 18 is connected to the bottom of the regeneration tower 2, the reboiler 18 is used to heat the rich liquid in the regeneration tower 2, so that carbon dioxide in the rich liquid is precipitated and changed into a lean liquid, and the reboiler 18 heats the absorption liquid by the extraction of a steam turbine.
As shown in fig. 1, a lean liquid return pipe 19 is connected to the regeneration tower 2, and the lean liquid at the bottom of the regeneration tower 2 is adapted to flow back into the absorption tower 1 through the lean liquid return pipe 19. Specifically, the barren solution in the tower bottom of the regeneration tower 2 is pumped out of the regeneration tower 2 by a barren solution pump 20, then sequentially passes through the barren and rich solution heat exchanger 15 and the barren solution cooling heat exchanger, and finally enters the absorption tower 1 to continuously absorb the carbon dioxide in the flue gas.
As shown in fig. 1, the lean-rich liquid heat exchanger 15 is connected to the rich liquid supply pipe 13 and the lean liquid return pipe 19, and is configured to exchange heat between the rich liquid in the rich liquid supply pipe 13 and the lean liquid in the lean liquid return pipe 19, so as to heat the rich liquid that is about to enter the regeneration tower 2 by using the temperature of the lean liquid returned from the regeneration tower 2, thereby achieving the purpose of recovering the waste heat of the lean liquid returned from the regeneration tower 2, reducing the temperature of the lean liquid returned from the regeneration tower 2, improving the absorption capacity of the lean liquid for carbon dioxide in the absorption tower 1, and reducing the energy consumption of the regeneration tower 2.
As shown in fig. 1, the outlet at the top of the regeneration tower 2 is a crude gas vent 21, and the carbon dioxide gas precipitated from the regeneration tower 2 enters a gas-liquid separator 22 through the crude gas vent 21, and the high-purity carbon dioxide gas is separated by the gas-liquid separator 22 and sent to the subsequent compression unit. While the liquid phase separated from the gas-liquid separator 22 may be refluxed into the regeneration column 2. Specifically, a crude gas exhaust port 21 of the regeneration tower 2 is communicated with a first cooling heat exchanger 17, and the first cooling heat exchanger 17 is used for performing waste heat recovery on the tower top regenerated gas of the regeneration tower 2; the first cooling heat exchanger 17 communicates with the rich liquid supply pipe 13, and recovers the residual heat of the regeneration gas by the rich liquid in the rich liquid supply pipe 13, thereby realizing the internal circulation of the system.
As an alternative embodiment, as shown in fig. 2, a second cooling heat exchanger 23 is further disposed at the rear end of the first cooling heat exchanger 17, and the separated water of the gas-liquid separator 22 passes through the second cooling heat exchanger 23 and then enters the regeneration tower 2.
As shown in fig. 1, a gas supply pipe 24 is connected to the flash tank 16, and the flash gas flashed off from the flash tank 16 of the rich liquid is supplied to the regeneration tower 2 through the gas supply pipe 24. The flash gas comprises carbon dioxide and water vapor, which contain a large amount of heat, and can function as a reboiler 18 on part of the regeneration tower 2 after being sent to the regeneration tower 2.
In a preferred embodiment, as shown in fig. 1, a compressor 25 is connected to the feed pipe 24, and the flash gas in the flash tank 16 is suitably compressed by the compressor 25 and then fed to the regeneration column 2. The rich liquid is compressed by the compressor 25 in the flash vapor evaporated by the flash tank 16 and is then sent to the regeneration tower 2, and the flash vapor contains a large amount of water vapor, and the temperature of the flash vapor is further increased by pressurizing the water vapor, so that the flash vapor functions as the reboiler 18 of the regeneration tower 2, and the energy consumption of the reboiler 18 is reduced.
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 changes and modifications may be made without departing from the scope of the present invention.
Claims (10)
1. The utility model provides a carbon dioxide entrapment pregnant solution flash distillation regeneration waste heat recovery system which characterized in that includes:
the absorption tower (1) is suitable for being communicated with the flue gas, the absorption tower (1) is internally used for containing absorption liquid, the absorption liquid in the absorption tower (1) absorbs carbon dioxide in the flue gas and then becomes rich liquid, a rich liquid supply pipe (13) is connected to the absorption tower (1), and the rich liquid is suitable for being sent into the regeneration tower (2) through the rich liquid supply pipe (13);
the regeneration tower (2) is internally suitable for containing absorption liquid, the absorption liquid in the regeneration tower (2) is changed into lean liquid after carbon dioxide is separated out, a lean liquid return pipe (19) is communicated with the regeneration tower (2), and the lean liquid is suitable for flowing back to the absorption tower (1) through the lean liquid return pipe (19);
a lean-rich liquid heat exchanger (15) which is communicated with the rich liquid supply pipe (13) and the lean liquid return pipe (19) respectively and is used for exchanging heat between the rich liquid in the rich liquid supply pipe (13) and the lean liquid in the lean liquid return pipe (19);
the first cooling heat exchanger (17) is arranged at the outlet of the tower top of the regeneration tower (2) and is used for recovering waste heat of the tower top regeneration gas of the regeneration tower (2), the first cooling heat exchanger (17) is communicated with the rich liquid supply pipe (13), and the waste heat of the regeneration gas is recovered through the rich liquid in the rich liquid supply pipe (13);
and the flash tank (16) is communicated with the lean-rich liquid heat exchanger (15) and the first cooling heat exchanger (17) through the rich liquid supply pipe (13), after the rich liquid in the rich liquid supply pipe (13) is subjected to primary heat exchange in the lean-rich liquid heat exchanger (15) or the first cooling heat exchanger (17), partial flash evaporation is performed in the flash tank (16), and then the residual rich liquid enters the lean-rich liquid heat exchanger (15) or the first cooling heat exchanger (17) again for secondary heat exchange.
2. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system according to claim 1, wherein a gas supply pipeline (24) is communicated with the flash tank (16), a compressor (25) is communicated with the gas supply pipeline (24), and flash gas of the flash tank (16) is suitable for being compressed by the compressor (25) and then is conveyed to the regeneration tower (2).
3. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system according to claim 1, wherein the rich liquid of the absorption tower (1) passes through a lean rich liquid heat exchanger (15), a flash tank (16) and a first cooling heat exchanger (17) in sequence in the rich liquid supply pipe (13) through a rich liquid pump (14) and finally enters the regeneration tower (2).
4. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system according to claim 1, wherein a spray device is arranged at the top of the absorption tower (1), the spray device performs circulating spraying through a spray pump (10), and an outlet of the spray pump (10) is suitable for being communicated with the top of the regeneration tower (2).
5. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system of claim 4, wherein the spraying device comprises: the water receiving tray (7) is arranged inside the tower top of the absorption tower (1), a smoke through hole (8) communicated with the tower bottom of the absorption tower (1) is formed in the water receiving tray (7), and a smoke pipeline extends upwards from the smoke through hole (8) on the water receiving tray (7).
6. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system of claim 5, characterized in that the top end of the flue gas pipeline is provided with a waterproof cap (9).
7. The carbon dioxide capture rich liquid flash evaporation regeneration waste heat recovery system according to claim 4, wherein a tail gas emptying port (3) is arranged at the top end of the absorption tower (1), and a demister (12) is arranged above the spraying device at the front end of the tail gas emptying port (3).
8. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system according to claim 1, wherein the top end of the regeneration tower (2) is provided with a crude gas exhaust port (21), the crude gas exhaust port (21) is communicated with a gas-liquid separator (22), and separated water of the gas-liquid separator (22) flows back into the regeneration tower (2).
9. The system for recovering the waste heat in the flash regeneration of the carbon dioxide capture rich solution according to claim 8, characterized in that a second cooling heat exchanger (23) is further arranged at the rear end of the first cooling heat exchanger (17), and the separated water of the gas-liquid separator (22) passes through the second cooling heat exchanger (23) and then enters the regeneration tower (2).
10. The carbon dioxide capture rich liquid flash regeneration waste heat recovery system according to any one of claims 1-9, wherein the absorption tower (1) is provided with a self-circulation pipeline (4), one end of the self-circulation pipeline (4) is opened into the tower bottom absorption liquid of the absorption tower (1), and the other end of the self-circulation pipeline (4) is opened into the tower top inner cavity of the absorption tower (1).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121092520.1U CN214914758U (en) | 2021-05-20 | 2021-05-20 | Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system |
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| CN202121092520.1U CN214914758U (en) | 2021-05-20 | 2021-05-20 | Carbon dioxide capture rich solution flash evaporation regeneration waste heat recovery system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114247272A (en) * | 2021-12-28 | 2022-03-29 | 北京华源泰盟节能设备有限公司 | Energy-saving system based on carbon dioxide capture technology |
| CN116371152A (en) * | 2023-03-23 | 2023-07-04 | 中国能源建设集团广东省电力设计研究院有限公司 | Carbon trapping system and method |
| CN116531918A (en) * | 2022-01-26 | 2023-08-04 | 中国石油天然气集团有限公司 | Energy-saving low-partial pressure carbon dioxide capturing system and method |
-
2021
- 2021-05-20 CN CN202121092520.1U patent/CN214914758U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114247272A (en) * | 2021-12-28 | 2022-03-29 | 北京华源泰盟节能设备有限公司 | Energy-saving system based on carbon dioxide capture technology |
| CN116531918A (en) * | 2022-01-26 | 2023-08-04 | 中国石油天然气集团有限公司 | Energy-saving low-partial pressure carbon dioxide capturing system and method |
| CN116371152A (en) * | 2023-03-23 | 2023-07-04 | 中国能源建设集团广东省电力设计研究院有限公司 | Carbon trapping system and method |
| CN116371152B (en) * | 2023-03-23 | 2024-03-12 | 中国能源建设集团广东省电力设计研究院有限公司 | Carbon trapping system and method |
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