A CO2 capture and low temperature condensate coupling system

Abstract

The present invention provides a carbon dioxide capture and low-pressure heater condensate coupling system, which belongs to the technical field of carbon dioxide capture, and comprises: an absorption tower, a regeneration tower and a reboiler, wherein the regeneration tower is connected with the rich liquid in the absorption tower through a pipeline, and the regeneration tower is provided with a rough gas exhaust port, and the rear end of the rough gas exhaust port of the regeneration tower is connected with a first cooling heat exchanger, and the first cooling heat exchanger is connected with a condensate pipeline of a low-pressure heater of a power plant; the carbon dioxide capture and low-pressure heater condensate coupling system of the present invention is connected with a first cooling heat exchanger at the rear end of the rough gas exhaust port of the regeneration tower, and the first cooling heat exchanger is connected with the low-pressure heater condensate of the power plant, and is used for heating the condensate entering the low-pressure heater, thereby reducing the energy consumption of heating the condensate by exhausting air from a steam turbine, and reducing the energy consumption of the carbon dioxide capture system as a whole, thereby achieving the purpose of energy saving.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon dioxide capture, and in particular to a carbon dioxide capture and low-temperature condensate coupling system. Background Art

[0002] CCS technology is the abbreviation of Carbon Capture and Storage, which is a technology for capturing and storing carbon dioxide (CO2). CCS technology refers to separating carbon dioxide produced by industry and related energy industries through carbon capture technology, and then transporting and storing it to the seabed or underground, etc., isolated from the atmosphere, through carbon storage methods.

[0003] CCS technology consists of two parts: carbon capture and carbon storage. Among them, carbon capture technology was first applied in the oil refining and chemical industries. Since the CO2 emitted by these industries is of high concentration and high pressure, the capture cost is not high. However, the CO2 emitted by coal-fired power plants is just the opposite. Capturing carbon dioxide from power plant emissions has the problem of high energy consumption and cost.

[0004] The energy consumption of the carbon dioxide capture system is mainly the regeneration steam consumption of the regeneration tower. Since the temperature difference between the lean liquid at the bottom of the regeneration tower and the regeneration gas at the top of the tower is not much, the heat they contain is also relatively close. If the heat is recovered by the rich liquid at the bottom of the absorption tower, only the heat of the lean liquid at the bottom of the tower or the top of the tower can be recovered. The temperature of the heated rich liquid is not much different from the temperature of the remaining other logistics, and the heat contained in the other logistics cannot be recovered. At present, the other logistics can only be cooled by circulating cooling water, resulting in almost half of the heat being wasted. Summary of the invention

[0005] Therefore, the technical problem to be solved by the present invention is to overcome the defect of excessively high energy consumption of the carbon dioxide capture system used in power plants in the prior art, thereby providing a carbon dioxide capture and low-temperature condensate coupling system.

[0006] In order to solve the above technical problems, the present invention provides a carbon dioxide capture and low-temperature condensate coupling system, comprising:

[0007] An absorption tower, one end of which is connected to the flue gas outlet of the power plant, and the interior of which is suitable for containing an absorption liquid, wherein the absorption liquid in the absorption tower absorbs carbon dioxide in the flue gas and becomes a rich liquid;

[0008] A regeneration tower is connected to the rich liquid in the absorption tower through a pipeline, the regeneration tower is provided with a coarse gas exhaust port, the rear end of the coarse gas exhaust port of the regeneration tower is connected to a first cooling heat exchanger, and the first cooling heat exchanger is connected to a condensate water pipeline of a low-temperature heater of a power plant;

[0009] The reboiler is connected to the regeneration tower and is used to vaporize the rich liquid entering the regeneration tower into gas-liquid two-phases, wherein the liquid phase becomes the lean liquid and the gas phase is discharged from the raw gas exhaust port of the regeneration tower.

[0010] Optionally, the cooling water inlet of the first cooling heat exchanger is connected to the outlet of the condenser, and the cooling water outlet of the first cooling heat exchanger is connected to the condensate inlet of the low-temperature heater.

[0011] Optionally, the absorption tower is provided with a self-circulation pipe, one end of which leads to the absorption liquid at the bottom of the absorption tower, and the other end of which leads to the inner cavity at the top of the absorption tower.

[0012] Optionally, a self-circulation heat exchanger is provided on the self-circulation pipeline.

[0013] Optionally, a spray device is provided on the outlet of one end of the self-circulating pipeline leading to the inner cavity at the top of the absorption tower.

[0014] Optionally, the absorption tower is provided with a tail gas exhaust port, a tail gas heat exchanger is provided at the front end of the tail gas exhaust port, and the tail gas heat exchanger is arranged above the self-circulation pipeline.

[0015] Optionally, a demister is further provided at the front end of the tail gas exhaust port of the absorption tower.

[0016] Optionally, a demister is provided at the front end of the rough gas exhaust port of the regeneration tower.

[0017] Optionally, the raw 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.

[0018] Optionally, a second cooling heat exchanger is further provided at the rear end of the first cooling heat exchanger, and the separation water discharged from the gas-liquid separator is first used as cooling water for the second cooling heat exchanger and then flows back to the regeneration tower.

[0019] The technical solution of the present invention has the following advantages:

[0020] 1. The carbon dioxide capture and low-pressure heater condensate coupling system provided by the present invention is connected to a first cooling heat exchanger at the rear end of the raw gas exhaust port of the regeneration tower. The first cooling heat exchanger is connected to the low-pressure heater condensate of the power plant and is used to heat the condensate entering the low-pressure heater, thereby reducing the energy consumption of heating the condensate through steam turbine extraction, reducing the energy consumption of the carbon dioxide capture system as a whole, and achieving the purpose of energy saving.

[0021] The low-pressure heater proposed in the present invention refers to a low-pressure heater. The function of the low-pressure heater is to utilize the steam that has done part of the work in the turbine and draw it into the heater to heat the feed water, thereby increasing the temperature of the water, reducing the amount of steam discharged from the turbine to the condenser, reducing energy loss, and improving the circulation efficiency of the thermal system. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0023] Figure 1 This is a schematic diagram of a carbon dioxide capture and low-temperature condensate coupling system provided in an embodiment of the present invention.

[0024] Figure 2 for Figure 1 Schematic diagram of the carbon dioxide capture system.

[0025] Figure 3 This is a schematic diagram of a second implementation of a carbon dioxide capture system provided in an embodiment of the present invention.

[0026] Description of reference numerals:

[0027] 1. Boiler; 2. High-pressure steam turbine; 3. Medium-pressure steam turbine; 4. Low-pressure steam turbine; 5. Condenser; 6. Low-pressure heat exchanger; 7. Deaerator; 8. High-pressure heat exchanger; 9. Reboiler; 10. Pre-washing tower; 11. Absorption tower; 12. Regeneration tower; 13. Crude gas exhaust port; 14. First cooling heat exchanger; 15. Flue gas inlet; 16. Booster fan; 17. Pre-washing pump; 18. Washing liquid heat exchanger; 19. PH value detection element; 20. Self-circulation pump; 21. Self-circulation heat exchanger; 22. Tail gas exhaust port; 23. Tail gas heat exchanger; 24. Rich liquid supply pipe; 25. Lean liquid return pipe; 26. Lean-rich liquid heat exchanger; 27. Lean liquid heat exchanger; 28. Gas-liquid separator; 29. ​​Second cooling heat exchanger. DETAILED DESCRIPTION

[0028] The technical solution of the present invention will be described clearly and completely below in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0029] In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", and "third" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance.

[0030] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0031] In addition, the technical features involved in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.

[0032] This embodiment provides a carbon dioxide capture and low-temperature condensate coupling system, such as Figure 1 As shown, it includes: a carbon dioxide capture system and a low-pressure condensate system. The thermal system of the power plant includes: a boiler 1, a high-pressure steam turbine 2, a medium-pressure steam turbine 3, a low-pressure steam turbine 4, a condenser 5, a low-pressure heat exchanger 6, a deaerator 7 and a high-pressure heat exchanger 8. The thermal system is the entire system of a coal-fired power plant that uses coal combustion to generate electricity. The steam turbine burns in the boiler 1 to generate steam, and the steam enters the steam turbine to generate electricity. The steam after power generation is condensed into water through the condenser 5, and then heated by the low-pressure, deaerator 7 and high-pressure heat exchanger and recirculated to the boiler 1, and circulated in sequence to achieve continuous power generation. Among them, among the devices that the steam from the steam turbine passes through in sequence, there are multiple low-pressure heat exchangers 6 located between the condenser 5 and the deaerator 7. The system composed of multiple low-pressure heat exchangers 6 is called a low-pressure system in this embodiment.

[0033] like Figure 1As shown, the carbon dioxide capture system has a reboiler 9, through which the rich liquid in the regeneration tower 12 is heated to precipitate crude carbon dioxide gas from the rich liquid. The reboiler 9 extracts heat by extracting air from the low-pressure steam turbine 4, and then the steam after heat exchange becomes condensed water, which is sent to the deaerator 7. In addition, the carbon dioxide capture system also has a first cooling heat exchanger 14 at the top of the regeneration tower 12, and the first cooling heat exchanger 14 is used to cool the crude carbon dioxide gas precipitated from the regeneration tower 12, also known as regeneration gas. The cooling water of the first cooling heat exchanger 14 uses the low-pressure condensate of the power plant, that is, before the condensate from the condenser enters the low-pressure heat exchanger 6, at least part of the condensate enters the first cooling heat exchanger 14 of the carbon dioxide system, and the condensate is used to cool the regeneration gas precipitated from the regeneration tower 12, so as to achieve the purpose of utilizing the residual temperature of the regeneration gas. Furthermore, the residual temperature of the regenerated gas is used to heat the LP heater condensate, thereby saving part of the heat consumption of the LP heater heat exchanger 6. The heating steam of the LP heater heat exchanger 6 comes from the exhaust of the steam turbine. Therefore, by utilizing the residual temperature of the regenerated gas to return part of the heat to the steam turbine, the steam consumption of the carbon dioxide capture system is reduced as a whole. Specifically, by adopting the carbon dioxide capture and LP heater condensate coupling system of this embodiment, the overall steam consumption can be reduced by 30%-40%.

[0034] like Figure 2 As shown, the carbon dioxide capture system provided in this embodiment includes: a pre-washing tower 10, an absorption tower 11 and a regeneration tower 12. The regeneration tower 12 has a crude gas exhaust port 13, and the rear end of the crude gas exhaust port 13 of the regeneration tower 12 is connected to a first cooling heat exchanger 14, and is connected to the low-pressure condensate pipeline of the power plant through the first cooling heat exchanger 14; that is, the cooling water inlet of the first cooling heat exchanger 14 is connected to part of the low-pressure condensate, and the cooling water outlet of the first cooling heat exchanger 14 is connected to the deaerator 7; or, the cooling water outlet of the first cooling heat exchanger 14 is connected to part of the low-pressure heat exchanger 6, so that the first cooling heat exchanger 14 is used to replace the function of part of the low-pressure heat exchanger 6 to save the air extraction amount of the steam turbine.

[0035] The pre-washing tower 10 is provided with a flue gas inlet 15, which is used to communicate with the flue gas after desulfurization, and the flue gas enters the pre-washing tower 10 through the flue gas inlet 15. The pre-washing tower 10 is mainly used to remove trace acidic gases in the flue gas, reduce the flue gas temperature by circulating and spraying alkali solution, and reduce the flue gas moisture content and flue gas volume. The top of the pre-washing tower 10 is provided with an outlet, which is connected to the inlet of the absorption tower 11 through a booster fan 16. The pre-washing tower 10 is provided with a circulation pipeline, and the two ends of the circulation pipeline are respectively connected to the bottom and the top of the pre-washing tower 10. The circulation pipeline is also connected to a pre-washing pump 17, and the washing liquid in the pre-washing tower 10 is transported from the bottom of the tower to the top of the tower through the pre-washing pump 17, and returns to the bottom of the tower by spraying in the top of the tower; in the process of the flue gas flowing from the flue gas inlet 15 to the outlet in the pre-washing tower 10, the flue gas and the washing liquid are convectively flowed, so that the flue gas is pre-washed by the washing liquid. In addition, as a preferred embodiment, a washing liquid heat exchanger 18 is also connected to the circulation pipeline, and the washing liquid heat exchanger 18 is used to cool the washing liquid to control the flue gas temperature at the outlet of the pre-wash tower, that is, the inlet temperature of the absorption tower 11, so as to adjust the water balance of the absorption liquid in the absorption and capture system. In addition, as a preferred embodiment, a pH value detection element 19 is also connected in parallel to the circulation pipeline, and the pH value detection element 19 is used to detect the pH value of the washing liquid in real time, so as to replenish the alkaline washing liquid in time.

[0036] like Figure 2As shown, the inlet at one end of the absorption tower 11 is connected to the outlet of the pre-washing tower 10 so as to be connected to the flue gas of the thermal power plant. The interior of the absorption tower 11 is suitable for accommodating absorption liquid. When the absorption liquid in the absorption tower 11 absorbs the carbon dioxide in the flue gas, it becomes a rich liquid. Specifically, the absorption tower 11 has a self-circulation pipeline, one end of which leads to the absorption liquid at the bottom of the absorption tower 11, and the other end of the self-circulation pipeline leads to the inner cavity at the top of the absorption tower 11. A spray device is provided at the outlet of one end of the self-circulation pipeline leading to the inner cavity at the top of the absorption tower 11, and the absorption liquid is sprayed downward from the top of the tower through the spray device to fully contact with the flue gas. The self-circulation pipeline is provided with a self-circulation heat exchanger 21 and a self-circulation pump 20. The self-circulation heat exchanger 21 is used to cool the absorbent, and the self-circulation pump 20 is used to maintain the circulation of the absorption liquid. The absorption tower 11 controls the temperature inside the absorption tower 11 through the heat exchange of the self-circulation heat exchanger 21. The lower the temperature and the higher the pressure, the more conducive it is for the absorbent to absorb carbon dioxide. On the self-circulation pipeline arranged on the outside of the absorption tower 11, the self-circulation pump 20 extracts the absorption liquid from the bottom of the absorption tower 11 and sends it to the self-circulation heat exchanger 21 for heat exchange with the cooling circulating water. The cooled absorption liquid can be sent to the top of the absorption tower 11 or the middle part of the absorption tower 11. The cold absorption liquid contacts the flue gas in the absorption tower 11 for heat exchange, thereby controlling the tower temperature of the absorption tower 11 so as to increase the absorption capacity of the absorption liquid per unit mass. The tower temperature of the absorption tower 11 is controlled by the self-circulation system to change the absorption capacity of the absorption liquid.

[0037] like Figure 2 As shown, the absorption tower 11 has an exhaust gas outlet 22, and the front end of the exhaust gas outlet 22 has an exhaust gas heat exchanger 23, and the exhaust gas heat exchanger 23 is arranged above the spray port of the self-circulating pipeline, and the flue gas discharged from the absorption tower 11 is cooled by the exhaust gas heat exchanger 23. Specifically, the exhaust gas heat exchanger 23 is a wide channel plate heat exchanger, and the plate heat exchanger can reduce the escape rate of the absorbent from the top of the absorption tower 11. The wide channel plate heat exchanger has the advantages of small heat exchange end difference and large heat exchange coefficient. The cooling circulating water exchanges heat with the flue gas through the inter-wall heat exchange, and the flue gas temperature at the top of the absorption tower 11 is saturated flue gas. After heat exchange with the cooling circulating water, water is precipitated, and the absorption liquid carried in the flue gas is also precipitated. The precipitated water and absorbent flow back to the absorption tower 11 along the heat exchange wall of the plate heat exchanger for reuse. In addition, the absorption tower 11 is further provided with a demister between the exhaust gas heat exchanger 23 and the exhaust gas exhaust port 22, and the demister is used to reduce the water content in the flue gas.

[0038] like Figure 2As shown, the regeneration tower 12 is connected to the rich liquid in the absorption tower 11 through a rich liquid supply pipe 24, one end of the rich liquid supply pipe 24 extends from the bottom of the absorption tower 11 into the absorption tower 11, and the other end of the rich liquid supply pipe 24 extends from the top of the regeneration tower 12 into the regeneration tower 12, and the rich liquid enters the top of the regeneration tower 12 from the absorption tower 11, and sprays downward from the top of the regeneration tower 12 by spraying, so that the carbon dioxide gas contained in the rich liquid is precipitated. In addition, a lean liquid return pipe 25 is also connected between the regeneration tower 12 and the absorption tower 11, one end of the lean liquid return pipe 25 is connected to the bottom of the regeneration tower 12, and the other end of the lean liquid return pipe 25 is connected to the top of the absorption tower 11, and sprays in the top of the absorption tower 11 by spraying. In addition, the lean liquid return pipe 25 and the rich liquid supply pipe 24 are connected via a lean-rich liquid heat exchanger 26, that is, after the hotter lean liquid in the lean liquid return pipe 25 transfers heat to the rich liquid in the rich liquid supply pipe 24 through the lean-rich liquid heat exchanger 26, the lean liquid in the lean liquid return pipe 25 returns to the absorption tower 11, thereby recovering the heat of the lean liquid in the regeneration tower 12; in addition, the rich liquid enters the top of the regeneration tower 12 after being heated by the lean liquid in the lean-rich liquid heat exchanger 26, and the regeneration tower 12 A reboiler 9 is provided at the bottom of the tower. The steam used in the reboiler 9 comes from the steam turbine exhaust. After the steam turbine exhaust is heat exchanged and condensed in the reboiler 9, the condensed water is returned to the thermal system deaerator 7. The exhaust gas at the top of the regeneration tower 12 exchanges heat with the condensed water of the low-pressure heater. After the condensed water of the low-pressure heater is heated by the exhaust gas of the regeneration tower 12, the condensed water is sent to the downstream low-pressure heater, thereby realizing the preheating of the condensed water, reducing the steam turbine exhaust used by the low-pressure heater heat exchanger 6 or not using it at all, so as to realize the waste heat recovery of the regeneration gas of the carbon dioxide capture system. In addition, a lean liquid heat exchanger 27 is also provided on the lean liquid return pipe 25, through which the lean liquid is cooled to restore the absorption of carbon dioxide in the flue gas by the absorption liquid.

[0039] like Figure 2 As shown, the top of the regeneration tower 12 has a crude gas outlet 13, and a demister is provided at the front end of the crude gas outlet 13, through which the water content in the exhaust gas is reduced. The crude gas outlet 13 of the regeneration tower 12 is connected to the gas-liquid separator 28, and the separated water of the gas-liquid separator 28 can flow back into the regeneration tower 12. In addition, the separated water discharged from the gas-liquid separator 28, if redundant, can be sent to the desulfurization system of the power plant for reuse.

[0040] like Figure 2As shown, the regeneration tower 12 is connected to the reboiler 9, and the reboiler 9 is used to vaporize the rich liquid entering the regeneration tower 12 into gas-liquid two-phase, that is, the carbon dioxide gas in the rich liquid is precipitated by heating, so that the rich liquid becomes a lean liquid, and the carbon dioxide gas in the rich liquid is discharged from the raw gas exhaust port 13 of the regeneration tower 12. The reboiler 9 can be understood as a heat exchanger, and the reboiler 9 is connected to the steam turbine exhaust gas, so that the absorption liquid is heated by the steam turbine exhaust gas.

[0041] like Figure 2 As shown, the raw gas exhaust port 13 of the regeneration tower 12 is connected to a first cooling heat exchanger 14, and the first cooling heat exchanger 14 is used to exchange heat with low-temperature condensed water, so as to achieve heat recovery of the carbon dioxide saturated gas precipitated in the regeneration tower 12. In addition, a second cooling heat exchanger 29 is also provided at the rear end of the first cooling heat exchanger 14, and the second cooling heat exchanger 29 is used to further recover the heat of the carbon dioxide saturated gas.

[0042] like Figure 3 As shown, as a preferred embodiment, the separated water discharged from the gas-liquid separator 28 is first used as cooling water for the second cooling heat exchanger 29, and then refluxed into the regeneration tower 12, so as to further recover the heat of the carbon dioxide gas.

[0043] The gas discharged from the gas-liquid separator 28 is compressed by a compressor and then utilized to complete the capture of carbon dioxide in the flue gas. The carbon dioxide capture and low-pressure condensate coupling system provided in this embodiment can realize the energy cascade utilization of extracted steam, reduce the overall steam consumption of the carbon dioxide capture and low-pressure system, and reduce the steam consumption of carbon dioxide capture by 30%-40%.

[0044] Obviously, the above embodiments are merely examples for clear explanation, and are not intended to limit the implementation methods. For those skilled in the art, other different forms of changes or modifications can be made based on the above description. It is not necessary and impossible to list all the implementation methods here. The obvious changes or modifications derived from these are still within the scope of protection of the present invention.

Claims

1. A carbon dioxide capture and low-temperature condensate coupling system, characterized in that: include: An absorption tower (11), one end of which is connected to the flue gas outlet of the power plant, and the interior of which is suitable for containing an absorption liquid. The absorption liquid in the absorption tower (11) absorbs carbon dioxide in the flue gas and becomes a rich liquid; The regeneration tower (12) is connected to the rich liquid in the absorption tower (11) through a pipeline, the regeneration tower (12) is provided with a coarse gas exhaust port (13), the rear end of the coarse gas exhaust port (13) of the regeneration tower (12) is connected to a first cooling heat exchanger (14), and the first cooling heat exchanger (14) is connected to a condensate water pipeline of a low-temperature heater of the power plant; A reboiler (9) is connected to the regeneration tower (12) and is used to vaporize the rich liquid entering the regeneration tower (12) into gas and liquid phases, wherein the liquid phase becomes a lean liquid and the gas phase is discharged from the raw gas exhaust port (13) of the regeneration tower (12); The cooling water inlet of the first cooling heat exchanger (14) is connected to the outlet of the condenser (5), and the cooling water outlet of the first cooling heat exchanger (14) is connected to the condensate inlet of the low-temperature heater; the absorption tower (11) is provided with a self-circulating pipeline, one end of the self-circulating pipeline leads to the absorption liquid at the bottom of the absorption tower (11), and the other end of the self-circulating pipeline leads to the inner cavity of the top of the absorption tower (11).

2. The carbon dioxide capture and low-temperature condensate coupling system according to claim 1 is characterized in that: A self-circulating heat exchanger (21) is provided on the self-circulating pipeline.

3. The carbon dioxide capture and low temperature condensate coupling system according to claim 1, characterized in that: A spray device is provided at the outlet of one end of the self-circulating pipeline leading to the inner cavity at the top of the absorption tower (11).

4. The carbon dioxide capture and low temperature condensate coupling system according to claim 1, characterized in that: The absorption tower (11) is provided with a tail gas exhaust port (22), and a tail gas heat exchanger (23) is provided at the front end of the tail gas exhaust port (22). The tail gas heat exchanger (23) is arranged above the self-circulating pipeline.

5. The carbon dioxide capture and low temperature condensate coupling system according to claim 4, characterized in that: The front end of the tail gas exhaust port (22) of the absorption tower (11) is also provided with a demister.

6. The carbon dioxide capture and low temperature condensate coupling system according to any one of claims 1 to 5, characterized in that: A demister is provided at the front end of the rough gas exhaust port (13) of the regeneration tower (12).

7. The carbon dioxide capture and low temperature condensate coupling system according to any one of claims 1 to 5, characterized in that: The raw gas exhaust port (13) of the regeneration tower (12) is in communication with the gas-liquid separator (28), and the separated water of the gas-liquid separator (28) flows back into the regeneration tower (12).

8. The carbon dioxide capture and low temperature condensate coupling system according to claim 7, characterized in that: A second cooling heat exchanger (29) is also provided at the rear end of the first cooling heat exchanger (14). Separation water discharged from the gas-liquid separator (28) is first used as cooling water for the second cooling heat exchanger (29) and then flows back into the regeneration tower (12).

Images