Alcohol amine absorption method carbon dioxide capturing and regenerating device and operation method

Abstract

The invention relates to the technical field of alcohol amine solution rich solution regeneration, and provides an alcohol amine absorption method carbon dioxide capture regeneration device and an operation method, the device comprises a regeneration tower, a compression enthalpy increasing module, a heat exchange module, a condensate water tank and a regeneration system; a regenerated gas outlet is formed in the top of the regeneration tower; an inlet of the compression enthalpy increasing module is connected with the regenerated gas outlet and is used for performing compression enthalpy increasing on the regenerated gas; an inlet of the first side of the heat exchange module is connected with an outlet of the compression enthalpy increasing module, an outlet of the first side is connected with a condensate water tank, and a condensate water outlet of the condensate water tank is connected to the regeneration tower; the regeneration tower is connected with the second side of the heat exchange module through a regeneration system and used for recycling waste heat in regenerated gas to the regeneration tower for use through heat exchange. By means of the arrangement, latent heat in the regeneration gas is fully recycled, heat efficiency is improved, system energy consumption is reduced, energy is saved, the regeneration gas does not need to be cooled and condensed through a chemical refrigeration working medium, and pollution to the environment due to leakage of the working medium is fundamentally eradicated.

Description

Technical Field

[0001] The invention relates to the technical field of alcohol amine solution rich solution regeneration, and in particular to an alcohol amine absorption method carbon dioxide capture and regeneration device and an operation method. Background Art

[0002] Alcoholamine rich solution regeneration is the main stage of carbon dioxide desorption in the alcoholamine carbon capture system. Alcoholamine carbon capture is a type of carbon capture in which alcoholamine solution absorbs carbon dioxide to form alcoholamine rich solution, and the alcoholamine rich solution after absorption is desorbed to recover the alcoholamine solution for recycling.

[0003] The stage of desorption of the alcoholamine rich solution is called the regeneration stage. Under the desorption conditions, carbon dioxide is separated from the alcoholamine solution. This process requires heating the rich solution to reach the temperature for desorption of carbon dioxide.

[0004] However, during the amine rich liquid regeneration stage, a large amount of heat in the high-temperature regeneration gas will be wasted in the condensation process, resulting in high energy consumption, which has always been the pain point of the regeneration system in the existing amine-based carbon dioxide capture device.

[0005] Therefore, how to effectively recycle waste heat and reduce energy consumption is an important issue that needs to be solved urgently. Summary of the invention

[0006] The present invention provides an alcohol amine absorption method carbon dioxide capture and regeneration device and an operation method, which are used to solve the defect of high energy consumption in the alcohol amine rich liquid regeneration stage in the prior art, and can effectively recycle the waste heat in the high-temperature regeneration gas to reduce system energy consumption.

[0007] The present invention provides an alcohol amine absorption method carbon dioxide capture and regeneration device, comprising: a regeneration tower, a compression enthalpy increase module, a heat exchange module, a condensed water tank and a regeneration system; A regeneration gas outlet is provided at the top of the regeneration tower; the inlet of the compression enthalpy increase module is connected to the regeneration gas outlet, and is used to compress the regeneration gas to increase enthalpy; The heat exchange module is provided with a first side and a second side, the inlet of the first side is connected to the outlet of the compression enthalpy increasing module, the outlet of the first side is connected to the condensed water tank, and the condensed water outlet of the condensed water tank is connected to the regeneration tower; The regeneration tower is connected to the second side of the heat exchange module through the regeneration system, and is used to recover the waste heat in the regeneration gas to the regeneration tower for utilization through heat exchange.

[0008] According to the present invention, a carbon dioxide capture and regeneration device using an alcohol amine absorption method is provided, wherein the regeneration system comprises a first subsystem, and the first subsystem comprises a first loop; The inlet of the first loop is connected to the kettle of the regeneration tower, and the outlet is connected back to the kettle of the regeneration tower through the second side; a pump body is provided on the first loop.

[0009] According to the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention, the regeneration system includes a second subsystem, and the second subsystem includes a gas-liquid separator, a second loop and a regeneration loop; The liquid inlet of the gas-liquid separator is connected to the kettle of the regeneration tower through a pump body; the inlet of the second circuit is connected to the liquid outlet of the gas-liquid separator, and the outlet is connected back to the gas-liquid separator through the second side; A pump body is provided on the second circuit; the steam outlet of the gas-liquid separator is connected to the kettle of the regeneration tower through the regeneration circuit, and a first compressor is provided on the regeneration circuit.

[0010] According to the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention, the regeneration system includes a third subsystem, and the third subsystem includes a third loop and a regeneration loop; The inlet of the third circuit is connected to the condensate outlet of the condensate tank, and the outlet is connected to the regeneration circuit through the second side. The regeneration circuit is connected to the kettle of the regeneration tower. A pump body is provided on the third circuit, and a first compressor is provided on the regeneration circuit.

[0011] According to the present invention, a carbon dioxide capture and regeneration device using an alcohol amine absorption method is provided, wherein the regeneration system comprises: A first subsystem includes a first loop, wherein an inlet of the first loop is connected to the kettle of the regeneration tower, and an outlet of the first loop is connected back to the kettle of the regeneration tower through the second side; The second subsystem includes a gas-liquid separator, a second loop and a regeneration loop; the liquid inlet of the gas-liquid separator is connected to the tower kettle; the inlet of the second loop is connected to the liquid outlet of the gas-liquid separator, and the outlet is connected back to the gas-liquid separator through the second side; the steam outlet of the gas-liquid separator is connected to the tower kettle through the regeneration loop, and the regeneration loop is provided with a first compressor; The third subsystem includes a third circuit and the regeneration circuit; the inlet of the third circuit is connected to the condensed water outlet of the condensed water tank, and the outlet is connected to the regeneration circuit through the second side.

[0012] According to the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention, the first loop comprises: a first passage, the inlet of which is connected to the tower kettle, and the outlet of which is connected to the inlet of the second side; a first valve and a first pump body are provided on the first passage; The second passage has an inlet connected to the outlet of the second side and an outlet connected to the tower kettle; and a second valve is arranged on the second passage.

[0013] According to an alcohol amine absorption method carbon dioxide capture and regeneration device provided by the present invention, a third valve and a second pump body are provided between the liquid inlet of the gas-liquid separator and the tower kettle; a fourth valve is provided at the steam outlet of the gas-liquid separator, and a fifth valve is provided on the regeneration circuit; the second circuit includes: the first passage and the second passage; a third passage, the inlet of which is connected to the liquid outlet of the gas-liquid separator, the outlet of which is connected to the first passage, and the third passage is provided with a sixth valve; The fourth passage has an inlet connected to the second passage and an outlet connected to the middle of the gas-liquid separator. The fourth passage is provided with a seventh valve.

[0014] According to the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention, the third loop comprises: a fifth passage, the inlet of which is connected to the condensed water outlet of the condensed water tank, and the outlet of which is connected to the inlet of the second side through the third pump body; an eighth valve is provided at the outlet of the fifth passage; The sixth passage has an inlet connected to the outlet of the second side and an outlet connected to the regeneration circuit. A ninth valve is disposed on the fifth passage.

[0015] According to a carbon dioxide capture and regeneration device using an amine absorption method provided by the present invention, the compression enthalpy increase module includes a regeneration gas pipeline and a second compressor; the inlet of the regeneration gas pipeline is connected to the regeneration gas outlet, and the outlet is connected to the inlet of the first side through the second compressor.

[0016] According to the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention, the heat exchange module includes a first heat exchanger and a second heat exchanger; The outlet of the compression enthalpy increasing module is connected to the inlet of the first side of the first heat exchanger through a first branch, and is connected to the inlet of the first side of the second heat exchanger through a second branch; a tenth valve is provided on the first branch, and an eleventh valve is provided on the second branch; The first passage is connected to an inlet of a second side of the first heat exchanger; the second passage is connected to an outlet of the second side of the first heat exchanger; The inlet of the fifth passage is connected to the inlet of the second side of the second heat exchanger, and the sixth passage is connected to the outlet of the second side of the second heat exchanger.

[0017] According to the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention, a fourth pump body and a twelfth valve are provided between the condensate outlet of the condensate tank and the regeneration tower.

[0018] According to the present invention, a carbon dioxide capture and regeneration device using an alcohol amine absorption method further comprises a drain pipe for draining the lean liquid in the regeneration system, and a drain valve is provided on the drain pipe.

[0019] According to the alcohol amine absorption method carbon dioxide capture and regeneration device provided by the present invention, the exhaust pipe is connected to the first passage.

[0020] The present invention also provides an operation method of an alcoholamine absorption method carbon dioxide capture and regeneration device, comprising at least one of the following operation modes: In the MVC direct compression regeneration mode of the tower top gas, the first subsystem is started. At the beginning, the lean liquid pumped out from the tower bottom is heated by an external heat source to generate initial regeneration steam and return to the tower bottom. The regeneration gas at the top of the tower is compressed and increased in enthalpy by the compression enthalpy increase module, and then the lean liquid pumped out from the tower bottom is heated by the heat exchange module. The regeneration gas after heat exchange enters the condensate tank, the carbon dioxide gas is separated, and the condensate is returned to the regeneration tower; the preset condensate tank liquid level is used as the target value to control the water replenishment flow from the condensate tank to the regeneration tower, and the residual carbon dioxide in the water continues to be regenerated. The lean liquid that is heated and produces steam returns to the tower bottom and flashes to separate steam for the next regeneration; In the MVC composite enthalpy-increasing regeneration mode of the tower top / tower bottom, the second subsystem is started, the liquid level of the gas-liquid separator is preset, and the lean liquid is added to the gas-liquid separator through the tower bottom. After that, the lean liquid supplement flow rate is controlled at the preset liquid level during operation, and the lean liquid pumped out of the gas-liquid separator is heated by an external heat source. The initial regeneration steam is separated by the first compressor through air extraction and flash evaporation and enters the regeneration tower. The regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression and enthalpy-increasing module, and then the circulating lean liquid pumped out of the gas-liquid separator is heated by the heat exchange module. After heat exchange, the regeneration gas enters the condensed water tank, the carbon dioxide gas is separated, and the condensed water returns to the regeneration tower; the lean liquid that is heated and produces steam returns to the gas-liquid separator and is separated by air extraction and flash evaporation by the first compressor, and then enters the regeneration tower for regeneration after pressure and temperature increase; In the MVC enthalpy-increasing regeneration mode of flash evaporation of lean liquid in the tower bottom, the second subsystem is started, the liquid level of the gas-liquid separator is preset, and lean liquid is added to the gas-liquid separator through the tower bottom. After that, the lean liquid supplement flow rate is controlled at the preset liquid level during operation, and the lean liquid pumped out of the gas-liquid separator is heated by an external heat source. The initial regeneration steam is separated by pumping and flashing by the first compressor, and then enters the regeneration tower after being pressurized and heated. The regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression enthalpy-increasing module, and then the circulating lean liquid pumped out from the gas-liquid separator is heated by the heat exchange module. The regeneration gas enters the condensed water tank after heat exchange, and the carbon dioxide gas is separated. After the first compressor pumps and decompresses the lean liquid in the gas-liquid separator, a small part of steam is flashed and the temperature is reduced. The lean liquid that is heated and produces steam by the heat exchange module returns to the gas-liquid separator, and the flashed steam also enters the first compressor. The first compressor continuously pressurizes and heats the two steam streams and discharges them into the tower bottom for regeneration. In the direct steam regeneration mode of the tower bottom, the third subsystem is started. At the beginning, the lean liquid in the tower bottom is heated by an external heat source to generate initial regeneration steam. The regeneration gas at the top of the tower is compressed and increased in enthalpy by the compression enthalpy increase module and then enters the heat exchange module. After heat exchange, the regeneration gas enters the condensate tank, the carbon dioxide gas is separated, and the condensed water falls. The liquid level of the condensate tank is pre-set and used to control the discharge flow rate of the condensed water in the condensate tank. The discharged condensed water enters the heat exchange module after throttling, reducing the pressure and cooling, and enters the first compressor after heat exchange with the regeneration gas to increase the pressure and temperature, and then is directly discharged into the tower bottom for regeneration.

[0021] Beneficial effects: 1. After being compressed and enthalpy increased, the regenerated gas is exchanged with the regeneration system, and the heat in the regeneration gas is recovered to the regeneration tower for repeated use through the regeneration system, so that the latent heat energy in the regeneration gas can be fully recovered and utilized, thereby improving thermal efficiency, reducing system energy consumption, and saving energy.

[0022] Second, there is no need to use chemical refrigeration fluid to cool and condense the regenerated gas, which fundamentally eliminates the pollution to the environment caused by fluid leakage.

[0023] 3. Multiple line options, with a higher degree of automation. According to the required regeneration temperature, carbon dioxide capture rate, power consumption and other requirements, the appropriate MVC enthalpy-increasing regeneration line can be selected, and the line switching can be achieved simply by controlling the opening and closing of different valves and the operation of the pump body. The same compressor and pump body can play multiple roles by adopting different control strategies.

[0024] Fourth, through the MVC enthalpy-increasing regeneration mode of the lean liquid flash evaporation in the bottom of the tower, the temperature required for the evaporation of the lean liquid can be reduced, and at the same time, the required condensation temperature of the regenerated gas after compression can be reduced, and the water vapor content in the carbon dioxide can be reduced, so that a larger proportion of water vapor can participate in heat exchange condensation, releasing more heat to evaporate more water in the lean liquid, and generating more water vapor to desorb more carbon dioxide in the rich liquid, thereby increasing the output of the entire carbon dioxide capture system; the required water vapor temperature is lower, and the required compressor power will also be lower. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] In order to more clearly illustrate the technical solutions in the present invention or the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0026] Figure 1 It is a structural schematic diagram of a carbon dioxide capture and regeneration device using an alcohol amine absorption method provided in an embodiment of the present invention.

[0027] Reference numerals: 10. Regeneration tower; 20. Compression enthalpy increase module; 200. Regeneration gas pipeline; 201. Second compressor; 202. First branch; 203. Second branch; 204. Twelve valves; 205. Thirteen valves; 30. Heat exchange module; 300. First heat exchanger; 301. Second heat exchanger; 40. Condensate tank; 400. Seventh passage; 401. Fourth pump body; 402. Tenth valve; 50. Regeneration system; 510. First passage; 511. Second passage; 512. First valve; 513. 3. The first pump body; 514. The second valve; 520. The gas-liquid separator; 521. The third valve; 522. The second pump body; 523. The fourth valve; 524. The third passage; 525. The fourth passage; 526. The sixth valve; 527. The seventh valve; 530. The regeneration circuit; 531. The first compressor; 532. The fifth valve; 540. The fifth passage; 541. The sixth passage; 542. The third pump body; 543. The eighth valve; 544. The ninth valve; 550. The exhaust pipe; 551. The eleventh valve. DETAILED DESCRIPTION

[0028] In order to make the purpose, technical solution and advantages of the present invention clearer, the technical solution of the present invention will be clearly and completely described below in conjunction with the drawings of the present invention. Obviously, the described embodiments are 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 order to facilitate the understanding of the alcohol amine absorption method carbon dioxide capture and regeneration device and operation method provided by the present invention, its application background is first introduced. Alkolamine rich solution regeneration is the most important link in the alcohol amine method carbon capture system. During the regeneration stage, carbon dioxide is separated from the alcohol amine rich solution, and the alcohol amine lean solution is recovered for recycling. During the entire regeneration stage, heating is required to ensure that the temperature of the rich solution reaches the conditions for carbon dioxide desorption.

[0030] However, continuous heating not only increases the energy consumption cost of the entire system, but also in the subsequent condensation and separation section, a large amount of heat in the high-temperature regeneration gas will be wasted during the condensation process, resulting in high energy consumption, which has always been a pain point of the regeneration system in the existing amine-based carbon dioxide capture device.

[0031] Therefore, how to effectively recycle waste heat and reduce energy consumption is an important issue that needs to be solved urgently.

[0032] In view of the above technical problems, the present invention provides an amine absorption method carbon dioxide capture and regeneration device and an operation method, which can effectively recycle the waste heat in the high-temperature regeneration gas and reduce the energy consumption of the system.

[0033] Combine the following Figure 1The present invention describes an alcohol amine absorption method carbon dioxide capture and regeneration device and an operation method.

[0034] Reference Figure 1 A carbon dioxide capture and regeneration device using an amine absorption method comprises a regeneration tower 10, a compression enthalpy increase module 20, a heat exchange module 30, a condensed water tank 40 and a regeneration system 50; wherein, a regeneration gas outlet is provided at the top of the regeneration tower 10; the inlet of the compression enthalpy increase module 20 is connected to the regeneration gas outlet for compressing and increasing the enthalpy of the regeneration gas; the heat exchange module 30 is provided with a first side and a second side, the inlet of the first side is connected to the outlet of the compression enthalpy increase module 20, the outlet of the first side is connected to the condensed water tank 40, and the condensed water outlet of the condensed water tank 40 is connected to the regeneration tower 10; the regeneration tower 10 is connected to the second side of the heat exchange module 30 through the regeneration system 50, for recovering the waste heat in the regeneration gas to the regeneration tower 10 for utilization through heat exchange.

[0035] In actual applications, the high-temperature regeneration gas is discharged through the regeneration gas outlet at the top of the regeneration tower 10. The compression enthalpy increase module 20 can compress the regeneration gas to increase the enthalpy and increase the temperature of the regeneration gas. The regeneration gas after compression enthalpy increase enters the heat exchange module 30 and exchanges heat with the regeneration system 50, so that the regeneration system 50 can recover the heat in the regeneration gas to the regeneration tower 10 for reuse. The regeneration gas after heat exchange enters the condensation water tank 40 for condensation, the condensed water falls and returns to the regeneration tower 10, and the carbon dioxide gas is separated out.

[0036] Compared with the related art, the regenerated gas is compressed to increase enthalpy and then exchanges heat with the regeneration system 50, and the heat in the regenerated gas is recovered to the regeneration tower 10 for repeated utilization through the regeneration system 50, so that the latent heat energy in the regenerated gas can be fully recovered and utilized, thereby improving thermal efficiency, reducing system energy consumption, and saving energy; in addition, there is no need to use chemical refrigerants to cool and condense the regenerated gas, which fundamentally eliminates the pollution of the environment caused by leakage of refrigerants.

[0037] As an optional embodiment of the present invention, the regeneration system 50 includes a first subsystem, which includes a first loop; the inlet of the first loop is connected to the bottom of the regeneration tower 10, and the outlet is connected back to the bottom of the regeneration tower 10 through the second side of the heat exchange module 30, and a pump body is provided on the first loop.

[0038] Through the technical solution of this embodiment, the MVC direct compression regeneration mode of the tower top gas can be realized. In this mode, the first subsystem is started. At the beginning, the lean liquid pumped out from the tower bottom is heated by an external heat source to generate initial regeneration steam and the initial regeneration steam is returned to the tower bottom. The regeneration gas at the top of the tower is compressed and enthalpy increased by the compression enthalpy increase module 20 and then heated by the heat exchange module 30 to heat the lean liquid pumped out from the tower bottom. The regeneration gas after heat exchange enters the condensed water tank 40, the carbon dioxide gas rises and separates, and the condensed water falls and returns to the regeneration tower 10. The preset liquid level of the condensed water tank 40 is used as the target value to control the water replenishment flow rate from the condensed water tank 40 to the regeneration tower 10, and the residual carbon dioxide in the water continues to be separated. The lean liquid that is heated and produces steam returns to the tower bottom and flash evaporates to separate steam for subsequent regeneration.

[0039] Specifically, the MVC direct compression regeneration mode of the tower top gas is suitable for situations where the water vapor content in the regeneration gas is high. For example, when the water vapor content in the regeneration gas reaches CO2:H2O=1:3 or above, the MVC direct compression regeneration mode of the tower top gas can be used for regeneration.

[0040] As an optional embodiment of the present invention, the regeneration system 50 includes a second subsystem, which includes a gas-liquid separator 520, a second loop and a regeneration loop 530; the liquid inlet of the gas-liquid separator 520 is connected to the kettle of the regeneration tower 10 via a pump body; the inlet of the second loop is connected to the liquid outlet of the gas-liquid separator 520, and the outlet is connected back to the gas-liquid separator 520 through the second side of the heat exchange module 30; a pump body is provided on the second loop, and the steam outlet of the gas-liquid separator 520 is connected to the kettle of the regeneration tower 10 via the regeneration loop 530, and a first compressor 531 is provided on the regeneration loop 530.

[0041] Through the technical solution of this embodiment, the tower top / tower bottom MVC composite enthalpy increase regeneration mode and the tower bottom lean liquid flash MVC enthalpy increase regeneration mode can be realized: In the MVC composite enthalpy-increasing regeneration mode of the tower top / tower bottom, the second subsystem is started, the liquid level of the gas-liquid separator 520 is preset, and the lean liquid is added to the gas-liquid separator 520 through the tower bottom to the preset liquid level. After that, the lean liquid replenishment flow is controlled by the preset liquid level during operation, and the lean liquid pumped out of the gas-liquid separator 520 is heated by an external heat source. The initial regeneration steam is separated by the first compressor 531 through air extraction flash evaporation and enters the regeneration tower 10. The regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression enthalpy-increasing module 20 and then heated by the heat exchange module 30. The circulating lean liquid pumped out from the gas-liquid separator 520 enters the condensate tank 40 after heat exchange with the regenerated gas, the carbon dioxide gas rises and separates, the condensate falls and returns to the regeneration tower 10, and the preset liquid level of the condensate tank 40 is used as the target value to control the water replenishment flow from the condensate tank 40 to the regeneration tower 10, and the residual carbon dioxide in the water continues to be regenerated, and the lean liquid that is heated and produces steam returns to the gas-liquid separator 520 and is separated by flash evaporation of the first compressor 531, and the steam is pressurized and heated to enter the regeneration tower 10 for regeneration.

[0042] Specifically, the top / bottom MVC composite enthalpy increase regeneration mode is suitable for situations where the water vapor content in the regeneration gas is medium. For example, when the water vapor content in the regeneration gas reaches about CO2:H2O=1:1.5, the top / bottom MVC composite enthalpy increase regeneration mode can be selected for regeneration.

[0043] In the MVC enthalpy-increasing regeneration mode of the flash evaporation of the lean liquid in the tower bottom, the second subsystem is started, the liquid level of the gas-liquid separator 520 is preset, and the lean liquid is added to the gas-liquid separator 520 through the tower bottom to the preset liquid level. After that, the lean liquid replenishment flow rate is controlled by the preset liquid level during operation, and the lean liquid pumped out of the gas-liquid separator 520 is heated by an external heat source, and the initial regeneration steam is separated by the first compressor 531 through air extraction flash evaporation and enters the regeneration tower 10 after the pressure and temperature are increased. The regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression enthalpy-increasing module 20, and then the circulating lean liquid pumped out of the gas-liquid separator 520 is heated by the heat exchange module 30. After the regeneration gas is heat-exchanged The carbon dioxide enters the condensate tank 40, where the carbon dioxide gas is separated and the condensate is returned to the regeneration tower 10. The preset liquid level of the condensate tank 40 is used as the target value to control the water replenishment flow from the condensate tank 40 to the regeneration tower 10, and the carbon dioxide remaining in the water continues to be regenerated. The lean liquid in the gas-liquid separator 520 flashes out a small amount of steam and the temperature is reduced after the first compressor 531 exhausts air and reduces pressure. The lean liquid that is heated and produces steam through the heat exchange module 30 returns to the gas-liquid separator 520, and the flashed steam also enters the first compressor 531. The first compressor 531 continuously increases the pressure and temperature of the two streams of steam and discharges them into the tower kettle for regeneration.

[0044] Through the MVC enthalpy-increasing regeneration mode of the lean liquid flash evaporation in the bottom of the tower, the temperature required for the evaporation of the lean liquid can be reduced. At the same time, the required condensation temperature of the regenerated gas after compression can be reduced, and the water vapor content in the carbon dioxide can be reduced, so that a larger proportion of water vapor can participate in heat exchange condensation, releasing more heat to evaporate more water in the lean liquid, and generating more water vapor to desorb more carbon dioxide in the rich liquid, thereby increasing the output of the entire carbon dioxide capture system; and the required water vapor temperature is lower, and the required compressor power will also be lower.

[0045] Specifically, the MVC enthalpy-increasing regeneration mode of the tower bottom lean liquid flash evaporation is suitable for situations where the water vapor content in the regeneration gas is low. For example, when the water vapor content in the regeneration gas reaches below CO2:H2O=1:1.2, the MVC enthalpy-increasing regeneration mode of the tower bottom lean liquid flash evaporation can be selected for regeneration.

[0046] As an optional embodiment of the present invention, the regeneration system 50 includes a third subsystem, and the third subsystem includes a third loop and a regeneration loop 530; wherein, the inlet of the third loop is connected to the condensate outlet of the condensate tank 40, and the outlet is connected to the regeneration loop 530 through the second side, and the regeneration loop 530 is connected to the bottom of the regeneration tower 10, and a pump body is provided on the third loop, and a first compressor 531 is provided on the regeneration loop 530.

[0047] Through the technical solution of this embodiment, it is possible to realize the direct steam regeneration mode of the tower bottom. In this mode, the third subsystem is started. At the beginning, the lean liquid in the tower bottom is heated by an external heat source to generate initial regeneration steam. The top regeneration gas is compressed and enthalpy increased by the compression enthalpy increase module 20 and then enters the heat exchange module 30. The regeneration gas enters the condensate tank 40 after heat exchange, and the carbon dioxide gas is separated and the condensed water falls. The liquid level of the condensate tank 40 is pre-set and used to control the discharge flow rate of the condensed water in the condensate tank 40. The discharged condensed water enters the heat exchange module 30 after throttling, reducing the pressure and cooling, and enters the first compressor 531 after heat exchange with the regeneration gas to increase the pressure and temperature, and then is directly discharged into the tower bottom for regeneration.

[0048] Specifically, when the circulation volume of the lean and rich liquids increases or is not suitable for external discharge through a branch line, it is appropriate to use the tower bottom direct steam regeneration mode for regeneration.

[0049] In some optional embodiments of the present invention, the regeneration system 50 may include one, two or three of the first subsystem, the second subsystem and the third system, and the specific configuration may be flexibly performed according to actual needs.

[0050] In this embodiment, the regeneration system 50 includes the first subsystem, the second subsystem and the third subsystem. Such a configuration can provide multiple selectable routes with a higher degree of automation. According to the required regeneration temperature, carbon dioxide capture rate, power consumption and other requirements, a suitable MVC enthalpy increase regeneration route can be selected to achieve the best mode matching and improve the waste heat utilization efficiency and cost efficiency.

[0051] In order to facilitate the switching of lines between different subsystems, thereby realizing the switching of different operation modes, in one embodiment of the present invention, referring to Figure 1 The first circuit includes a first passage 510 and a second passage 511; wherein, the inlet of the first passage 510 is connected to the tower kettle, and the outlet is connected to the inlet of the second side of the heat exchange module 30, and the first passage 510 is provided with a first valve 512 and a first pump body 513; the inlet of the second passage 511 is connected to the outlet of the second side of the heat exchange module 30, and the outlet is connected to the tower kettle, and the second passage 511 is provided with a second valve 514.

[0052] As a specific scheme of this embodiment, a third valve 521 and a second pump body 522 are provided between the liquid inlet of the gas-liquid separator 520 and the tower kettle, a fourth valve 523 is provided at the steam outlet of the gas-liquid separator 520, and a fifth valve 532 is provided on the regeneration circuit 530; the second circuit includes the above-mentioned first passage 510, the above-mentioned second passage 511, the third passage 524 and the fourth passage 525; wherein, the inlet of the third passage 524 is connected to the liquid outlet of the gas-liquid separator 520, the outlet is connected to the first passage 510 and the connection point is located between the first valve 512 and the first pump body 513, and the third passage 524 is provided with a sixth valve 526; the inlet of the fourth passage 525 is connected to the second passage 511 and the connection point is located upstream of the second valve 514, the outlet is connected to the middle of the gas-liquid separator 520, and the fourth passage 525 is provided with a seventh valve 527.

[0053] As a specific scheme of this embodiment, the third circuit includes a fifth passage 540 and a sixth passage 541, wherein the inlet of the fifth passage 540 is connected to the condensed water outlet of the condensed water tank 40, and the outlet is connected to the inlet of the second side of the heat exchange module 30 through the third pump body 542, and the outlet of the fifth passage 540 is provided with an eighth valve 543; the inlet of the sixth passage 541 is connected to the outlet of the second side of the heat exchange module 30, and the outlet is connected to the regeneration circuit 530, and the sixth passage 541 is provided with a ninth valve 544.

[0054] As a specific solution of this embodiment, the eighth valve 543 at the outlet of the fifth passage 540 can also serve as a throttle valve to throttle, reduce the pressure and temperature of the condensed water, so that the condensed water evaporates quickly and a part of it is converted into gas.

[0055] As a specific solution of this embodiment, the condensed water outlet of the condensed water tank 40 is connected to the upper side of the regeneration tower 10 through the seventh passage 400, and the seventh passage 400 is provided with a fourth pump body 401 and a tenth valve 402. The condensed water in the condensed water tank 40 can be returned to the regeneration tower 10 through the seventh passage 400.

[0056] As a specific solution of this embodiment, there are two condensate outlets for the condensed water, one of which is connected to the inlet on the second side of the heat exchange module 30 through the fifth passage 540 mentioned above, and the other is connected to the regeneration tower 10 through the seventh passage 400 mentioned above.

[0057] As a specific solution of this embodiment, in order to facilitate the regulation of the lean liquid flow in the regeneration system 50 , the regeneration system 50 also includes a drain pipe 550 for draining the lean liquid in the regeneration system 50 , and eleven valves 551 are provided on the drain pipe 550 .

[0058] As a specific solution of this embodiment, the drain pipe 550 is connected to the first passage 510 and the connection point is located downstream of the first pump body 513. By controlling the opening of the eleventh valve 551, the lean liquid flow in the regeneration system 50 can be controlled, thereby adjusting the liquid level in the bottom of the tower.

[0059] By adopting the above technical solution, the line switching can be achieved only by controlling the opening and closing of different valves and the operation of the pump body. The same compressor and pump body can play multiple roles by adopting different control strategies.

[0060] As a specific solution of this embodiment, the operation mode can be switched in the following manner: 1) In the MVC direct compression regeneration mode of the tower top gas, the first valve 512, the second valve 514, the tenth valve 402, and the eleventh valve 551 are opened, and the other valves are closed. At the beginning, the lean liquid pumped from the tower bottom by the first pump body 513 is heated by an external heat source to generate initial regeneration steam, and the initial regeneration steam returns to the tower bottom through the first loop. The regeneration steam at the top of the tower enters the heat exchange module 30 after compression and enthalpy increase, and transfers heat to the lean liquid pumped from the tower bottom by the first pump body 513. The regeneration gas after heat exchange enters the condensed water tank 40, carbon dioxide gas rises and separates, condensed water falls, and the preset liquid level of the condensed water tank 40 is used as the target value to control the frequency of the fourth pump body 401 and thus control the amount of water added to the regeneration tower 10, and the residual carbon dioxide in the water continues to be regenerated, and the lean liquid that is heated and produces steam returns to the tower kettle and flashes to separate steam for the next regeneration, wherein the first pump body 513 has a fixed frequency, and the opening of the eleventh valve 551 is adjusted with the preset tower kettle liquid level as the target value to control the flow of lean liquid discharged from the regeneration system 50.

[0061] 2) In the MVC compound enthalpy increase regeneration mode of the tower top / tower bottom, the third valve 521, the fourth valve 523, the fifth valve 532, the sixth valve 526, the seventh valve 527, the tenth valve 402 and the eleventh valve 551 are opened, and other valves are closed. The liquid level of the gas-liquid separator 520 is preset, and the second pump body 522 is controlled to replenish the preset liquid level of the lean liquid in the gas-liquid separator 520. Then, the frequency of the second pump body 522 is controlled with the preset liquid level of the gas-liquid separator 520 as the target value, thereby controlling the lean liquid replenishment flow rate. The lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513 is heated by an external heat source, and the initial regeneration steam is separated by the first compressor 531 to enter In the regeneration tower 10, the regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression and enthalpy-increasing module 20, and then heated by the heat exchange module 30 to heat the circulating lean liquid pumped out from the gas-liquid separator 520 by the first pump body 513. After heat exchange, the regeneration gas enters the condensed water tank 40, and the carbon dioxide gas is separated. The condensed water returns to the regeneration tower 10 in the same manner as above. The lean liquid that is heated and produces steam returns to the gas-liquid separator 520 and is separated by flash evacuation by the first compressor 531 to separate the steam. The lean liquid is pressurized and heated by the first compressor 531 and enters the regeneration tower 10 for regeneration. Among them, the first pump body 513 has a fixed frequency, and adjusts the opening of the eleventh valve 551 with the preset tower bottom liquid level as the target value to control the flow rate of the lean liquid discharged from the regeneration system 50.

[0062] 3) In the MVC regeneration mode of flash evaporation of lean liquid in the tower bottom, the third valve 521, the fourth valve 523, the fifth valve 532, the sixth valve 526, the seventh valve 527, the tenth valve 402 and the eleventh valve 551 are opened, and other valves are closed. The liquid level of the gas-liquid separator 520 is preset, and the second pump body 522 is controlled to replenish lean liquid into the gas-liquid separator 520. Then, the frequency of the second pump body 522 is controlled with the preset liquid level of the gas-liquid separator 520 as the target value, thereby controlling the lean liquid replenishment flow rate. The lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513 is heated by an external heat source, and the initial regeneration steam is separated by the first compressor 531 to enter the regeneration tower 10. The regeneration gas at the top of the tower is compressed and enthalpy increased. The circulating lean liquid pumped out from the gas-liquid separator 520 is then heated by the heat exchange module 30, and the regenerated gas enters the condensed water tank 40 after heat exchange, and the carbon dioxide gas is separated, and the condensed water is returned to the regeneration tower 10 in the same manner as above. The lean liquid in the gas-liquid separator 520 flashes out a small amount of steam and the temperature is reduced after the first compressor 531 exhausts air and reduces pressure, and the lean liquid that is heated and produces steam by the heat exchange module 30 returns to the gas-liquid separator 520, and the flashed steam also enters the first compressor 531. The first compressor 531 continuously increases the pressure and temperature of the two streams of steam and discharges them into the tower kettle for regeneration, wherein the first pump body 513 has a fixed frequency, and adjusts the opening of the eleventh valve 551 with the preset tower kettle liquid level as the target value to control the flow rate of the lean liquid discharged from the regeneration system 50.

[0063] 4) In the steam regeneration mode in which the bottom of the tower directly enters, the eighth valve 543, the ninth valve 544 and the fifth valve 532 are opened, and the other valves are closed. At the beginning, the lean liquid in the bottom of the tower is heated by an external heat source to generate initial regeneration steam. The top regeneration gas is compressed and increased in enthalpy by the compression and enthalpy increase module 20 and then enters the heat exchange module 30. The regeneration gas enters the condensed water tank 40 after heat exchange, and the carbon dioxide gas is separated, and the condensed water falls. The liquid level of the condensed water tank 40 is preset and used to control the frequency of the third pump body 542, and then the discharge flow rate of the condensed water. The discharged condensed water enters the heat exchange module 30 after throttling, reducing pressure and cooling, and enters the first compressor 531 after heat exchange with the regeneration gas to increase pressure and temperature, and then is directly discharged into the bottom of the tower for regeneration, wherein the opening of the eighth valve 543 is adjusted based on the temperature of the condensed water at the inlet of the heat exchange module 30 to control the flow rate of condensed water discharged from the condensed water tank 40.

[0064] As an optional embodiment of the present invention, the compression enthalpy increase module 20 includes a regeneration gas pipeline 200 and a second compressor 201; wherein the inlet of the regeneration gas pipeline 200 is connected to the regeneration gas outlet, and the outlet is connected to the inlet of the first side of the heat exchange module 30 through the second compressor 201.

[0065] In order to ensure the heat exchange efficiency and avoid mutual interference in different modes, the heat exchange module 30 includes a first heat exchanger 300 and a second heat exchanger 301; the outlet of the compression enthalpy increase module 20 is connected to the inlet of the first side of the first heat exchanger 300 through the first branch 202, and is connected to the inlet of the first side of the second heat exchanger 301 through the second branch 203; twelve valves 204 are provided on the first branch 202, and thirteen valves 205 are provided on the second branch 203; the first passage 510 is connected to the inlet of the second side of the first heat exchanger 300; the second passage 511 is connected to the outlet of the second side of the first heat exchanger 300; the inlet of the fifth passage 540 is connected to the inlet of the second side of the second heat exchanger 301, and the sixth passage 541 is connected to the outlet of the second side of the second heat exchanger 301.

[0066] As a specific scheme of this embodiment, in the tower top gas MVC direct compression regeneration mode, the tower top / tower bottom MVC composite enthalpy increase regeneration mode and the tower bottom lean liquid flash evaporation MVC enthalpy increase regeneration mode, the twelve valve 204 is opened and heat exchange is carried out through the first heat exchanger 300. In the tower bottom direct steam regeneration mode, the thirteenth valve 205 is opened and heat exchange is carried out through the second heat exchanger 301.

[0067] In one embodiment of the present invention, the first compressor 531 also has an air extraction function to perform air extraction and flash evaporation on the gas-liquid separator 520 .

[0068] It is to be understood that, without mutual contradiction, those skilled in the art may combine and combine the different embodiments or examples and the features of the different embodiments or examples described in this specification.

[0069] The operating method of the alcoholamine absorption method carbon dioxide capture and regeneration device provided by the present invention is described below. The operating method of the alcoholamine absorption method carbon dioxide capture and regeneration device described below can be referenced to each other with the alcoholamine absorption method carbon dioxide capture and regeneration device described above.

[0070] An operating method for an amine absorption method carbon dioxide capture and regeneration device comprises at least one operating mode of a tower top gas MVC direct compression regeneration mode, a tower top / tower bottom MVC composite enthalpy increase regeneration mode, a tower bottom lean liquid flash evaporation MVC enthalpy increase regeneration mode and a tower bottom direct steam regeneration mode.

[0071] The following will take the alcohol amine absorption method with an alcohol amine solution circulation volume of 0.5m³ / h, a carbon dioxide regeneration volume of 18kg / h, and a regeneration temperature of 100℃ as an example to explain in detail the operation modes of the four modes: 1) In the MVC direct compression regeneration mode of the tower top gas, the first valve 512, the second valve 514, the tenth valve 402, the eleventh valve 551 and the twelfth valve 204 are opened, and the other valves are closed. At the beginning, about 27kg / h, 110℃ external steam is introduced into the first heat exchanger 300 to heat the circulating lean liquid of about 2000kg / h pumped out from the tower bottom by the first pump body 513 and preheated to 100℃, and about 27kg / h, 100℃ saturated steam is generated and returned to the tower bottom. The steam rises along the tower to desorb carbon dioxide and becomes mixed regeneration gas, which is discharged from the top of the regeneration tower 10, sucked in by the second compressor 201 and pressurized and heated to a saturated temperature of about 110℃, and enters the first heat exchanger 300 to transfer heat to the regeneration gas pumped by the first pump body 5 13 The circulating lean liquid pumped out from the tower kettle enters the condensate tank 40 after heat exchange with the regenerated gas, about 18kg / h of carbon dioxide gas rises and is separated, and about 27kg / h of condensate falls. Taking the preset liquid level of the condensate tank 40 as the target value, PID controls the frequency of the fourth pump body 401 to control the water replenishment to the regeneration tower 10 at about 27kg / h, and the residual carbon dioxide in the water continues to be regenerated; the circulating lean liquid that is heated and produces steam returns to the tower kettle and flashes to separate about 27kg / h of 100℃ saturated steam for the next regeneration; the first pump body 513 and the second compressor 201 have fixed frequencies, and the eleventh valve 551 is adjusted with the tower kettle liquid level as the target value to control the discharge of about 0.5m³ / h of lean liquid from the regeneration system 50.

[0072] 2) In the MVC compound enthalpy increase regeneration mode of the tower top / tower bottom, the third valve 521, the fourth valve 523, the fifth valve 532, the sixth valve 526, the seventh valve 527, the tenth valve 402, the eleventh valve 551 and the twelfth valve 204 are opened, and other valves are closed. The liquid level of the gas-liquid separator 520 is preset, and the second pump body 522 is controlled to add lean liquid to the gas-liquid separator 520 to the preset liquid level. After that, about 27kg / h of 110℃ external steam is introduced into the first heat exchanger 300 to heat the circulating lean liquid of about 2000kg / h pumped out from the gas-liquid separator 520 by the first pump body 513 and preheated to 100℃. At the same time, the second pump body 522 is opened to control the frequency of the second pump body 522 with the preset liquid level as the target value, thereby controlling the addition of about 0.53m³ / h of lean liquid from the tower bottom to the gas-liquid separator 520, and the first compressor 531 is used to extract air for flash evaporation separation. 27kg / h, 100℃ saturated steam enters the regeneration tower 10, and the regeneration gas in the regeneration tower 10 is sucked in by the second compressor 201 and pressurized and heated to saturated 110℃, and then enters the first heat exchanger 300 to transfer heat to the circulating lean liquid pumped out from the gas-liquid separator 520 by the first pump body 513. After heat exchange, the regeneration gas enters the condensed water tank 40 and replenishes water to the regeneration tower 10 in the same way as above, and about 18kg / h of carbon dioxide is separated out; the circulating lean liquid that is heated and produces steam returns to the gas-liquid separator 520 and is separated by the first compressor 531 through air extraction and flash evaporation to obtain about 27kg / h, 100℃ saturated steam, which enters the regeneration tower 10 for regeneration; wherein, the first pump body 513, the first compressor 531, and the second compressor 201 have a fixed frequency, and the eleventh valve 551 is adjusted with the tower bottom liquid level as the target value to control the discharge of about 0.5m³ / h of lean liquid from the regeneration system 50.

[0073] 3) In the MVC enthalpy-increasing regeneration mode of flash evaporation of lean liquid in the tower bottom, the third valve 521, the fourth valve 523, the fifth valve 532, the sixth valve 526, the seventh valve 527, the tenth valve 402, the eleventh valve 551 and the twelfth valve 204 are opened, and other valves are closed. At the beginning, the lean liquid in the tower bottom is preheated to 100° C. by electrically heating the tower bottom and introducing steam and circulating lean liquid into the first heat exchanger 300, and the liquid level of the gas-liquid separator 520 is preset, and the second pump body 522 is controlled to replenish the lean liquid in the gas-liquid separator 520 to the preset liquid level, and then the first compressor 531 is used to pump air and reduce the pressure of the gas-liquid separator 520. The internal lean liquid flashes off a small portion of steam and the temperature is reduced to 90°C. At the same time, about 27kg / h, 100°C external steam is introduced into the first heat exchanger 300 to heat the circulating lean liquid of about 2000kg / h, 90°C pumped out from the gas-liquid separator 520 by the first pump body 513. The circulating lean liquid returns to the gas-liquid separator 520 and is pumped out by the first compressor 531 to flash off 27kg / h, 90°C saturated steam and pressurize and heat it to the saturated temperature of 100°C to enter the regeneration tower 10. At the same time, the second pump body 522 is turned on, and the frequency of the second pump body 522 is controlled with the preset liquid level of the gas-liquid separator 520 as the target value. Then, about 0.53 m³ / h of lean liquid is added from the tower bottom to the gas-liquid separator 520; the regenerated gas in the regeneration tower 10 is sucked into the first heat exchanger 300 through the second compressor 201, and the heat is transferred to the circulating lean liquid pumped out from the gas-liquid separator 520 by the first pump body 513. After heat exchange, the regenerated gas enters the condensed water tank 40 to replenish water to the regeneration tower 10 in the same manner as above, and about 18 kg / h of carbon dioxide is separated out; the lean liquid added from the tower bottom to the gas-liquid separator 520 by the second pump body 522 is pumped out and reduced in pressure by the first compressor 531, and a small amount of steam is flashed out in the gas-liquid separator 520, and the temperature is 40. The temperature is reduced to 90°C, and the circulating lean liquid is transported from the gas-liquid separator 520 to the first heat exchanger 300 by the first pump body 513. The lean liquid that is heated and produces steam returns to the gas-liquid separator 520, and flashes out about 27kg / h of 90°C saturated steam also enters the first compressor 531. The first compressor 531 increases the pressure and temperature of the steam to the saturation temperature of 100°C and discharges it into the tower kettle for regeneration. Among them, the first pump body 513, the first compressor 531, and the second compressor 201 are fixed in frequency, and the eleventh valve 551 is adjusted with the tower kettle liquid level as the target value to control the discharge of about 0.5m³ / h of lean liquid from the regeneration system 50.

[0074] 4) In the steam regeneration mode, the eighth valve 543, the ninth valve 544, the fifth valve 532 and the thirteenth valve 205 are opened, and other valves are closed. At the beginning, the tower kettle is electrically heated and steam and circulating lean liquid are introduced into the second heat exchanger 301 to preheat the lean liquid in the tower kettle to maintain it at 100°C. The regenerated gas reaches the top of the tower and is sucked in and transported to the second compressor 201 by about 49m³ / h of 100°C mixed regenerated gas (including 27kg / h of water vapor) to the second heat exchanger 301. After heat exchange, the regenerated gas enters the condensed water tank 40. About 18kg / h of carbon dioxide gas rises and is separated, and about 27kg / h of condensed water falls, according to the preset The liquid level of the condensate tank 40 is the target value, and the frequency of the third pump body 542 is controlled to control the water flow rate discharged from the condensate tank 40. The water enters the eighth valve 543, and after throttling and reducing the pressure and cooling to 90°C by the eighth valve 543, enters the second heat exchanger 301, and after heat exchange and evaporation with the regenerated gas, enters the first compressor 531 to increase the pressure and temperature to the saturation temperature of 100°C, and then is directly discharged into the tower kettle for regeneration; among them, the first compressor 531 and the second compressor 201 have fixed frequencies, and the opening of the eighth valve 543 is adjusted with the condensate inlet temperature of the second heat exchanger 301 as the target value, and together with the third pump body 542, about 27 kg / h of water is discharged from the condensate tank 40.

[0075] By means of the amine absorption method carbon dioxide capture and regeneration device and operation method provided in the embodiment of the present invention, the regenerated gas is compressed to increase enthalpy and then heat-exchanged with the regeneration system 50, and the heat in the regenerated gas is recovered to the regeneration tower 10 for repeated utilization through the regeneration system 50, so that the latent heat energy in the regenerated gas is fully recovered and utilized, thereby improving thermal efficiency, reducing system energy consumption, and saving energy; in addition, there is no need to use chemical refrigerants to cool and condense the regenerated gas, which fundamentally eliminates the pollution of the environment caused by leakage of refrigerants.

[0076] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some of the technical features therein. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A carbon dioxide capture and regeneration device using an alcohol amine absorption method, characterized in that: include: Regeneration tower, compression enthalpy increase module, heat exchange module, condensate tank and regeneration system; A regeneration gas outlet is provided at the top of the regeneration tower; the inlet of the compression enthalpy increase module is connected to the regeneration gas outlet, and is used to compress the regeneration gas to increase enthalpy; The heat exchange module is provided with a first side and a second side, the inlet of the first side is connected to the outlet of the compression enthalpy increasing module, the outlet of the first side is connected to the condensed water tank, and the condensed water outlet of the condensed water tank is connected to the regeneration tower; The regeneration tower is connected to the second side of the heat exchange module through the regeneration system, and is used to recover the waste heat in the regeneration gas to the regeneration tower for utilization through heat exchange.

2. The alcoholamine absorption method carbon dioxide capture and regeneration device according to claim 1, characterized in that: The regeneration system includes a first subsystem, the first subsystem includes a first loop; The inlet of the first loop is connected to the kettle of the regeneration tower, and the outlet is connected back to the kettle of the regeneration tower through the second side; a pump body is provided on the first loop.

3. The alcohol amine absorption method carbon dioxide capture and regeneration device according to claim 1, characterized in that: The regeneration system includes a second subsystem, and the second subsystem includes a gas-liquid separator, a second loop and a regeneration loop; The liquid inlet of the gas-liquid separator is connected to the kettle of the regeneration tower through a pump body; the inlet of the second circuit is connected to the liquid outlet of the gas-liquid separator, and the outlet is connected back to the gas-liquid separator through the second side; A pump body is provided on the second circuit; the steam outlet of the gas-liquid separator is connected to the kettle of the regeneration tower through the regeneration circuit, and a first compressor is provided on the regeneration circuit.

4. The alcohol amine absorption method carbon dioxide capture and regeneration device according to claim 1, characterized in that: The regeneration system includes a third subsystem, and the third subsystem includes a third loop and a regeneration loop; The inlet of the third circuit is connected to the condensate outlet of the condensate tank, and the outlet is connected to the regeneration circuit through the second side. The regeneration circuit is connected to the kettle of the regeneration tower. A pump body is provided on the third circuit, and a first compressor is provided on the regeneration circuit.

5. The carbon dioxide capture and regeneration device using an alcohol amine absorption method according to claim 1, characterized in that: The regeneration system comprises: A first subsystem includes a first loop, wherein an inlet of the first loop is connected to the kettle of the regeneration tower, and an outlet of the first loop is connected back to the kettle of the regeneration tower through the second side; The second subsystem includes a gas-liquid separator, a second loop and a regeneration loop; the liquid inlet of the gas-liquid separator is connected to the tower kettle; the inlet of the second loop is connected to the liquid outlet of the gas-liquid separator, and the outlet is connected back to the gas-liquid separator through the second side; the steam outlet of the gas-liquid separator is connected to the tower kettle through the regeneration loop, and the regeneration loop is provided with a first compressor; The third subsystem includes a third circuit and the regeneration circuit; the inlet of the third circuit is connected to the condensed water outlet of the condensed water tank, and the outlet is connected to the regeneration circuit through the second side.

6. The device for capturing and regenerating carbon dioxide by alcohol amine absorption method according to claim 5, characterized in that: The first circuit comprises: a first passage, the inlet of which is connected to the tower kettle, and the outlet of which is connected to the inlet of the second side; a first valve and a first pump body are provided on the first passage; The second passage has an inlet connected to the outlet of the second side and an outlet connected to the tower kettle; and a second valve is arranged on the second passage.

7. The carbon dioxide capture and regeneration device using an alcohol amine absorption method according to claim 6, characterized in that: A third valve and a second pump body are provided between the liquid inlet of the gas-liquid separator and the tower kettle; a fourth valve is provided at the steam outlet of the gas-liquid separator, and a fifth valve is provided on the regeneration circuit; the second circuit includes: the first passage and the second passage; a third passage, the inlet of which is connected to the liquid outlet of the gas-liquid separator, the outlet of which is connected to the first passage, and the third passage is provided with a sixth valve; The fourth passage has an inlet connected to the second passage and an outlet connected to the middle of the gas-liquid separator. The fourth passage is provided with a seventh valve.

8. The carbon dioxide capture and regeneration device using an alcohol amine absorption method according to claim 7, characterized in that: The third loop comprises: a fifth passage, the inlet of which is connected to the condensed water outlet of the condensed water tank, and the outlet of which is connected to the inlet of the second side through the third pump body; an eighth valve is provided at the outlet of the fifth passage; The sixth passage has an inlet connected to the outlet of the second side and an outlet connected to the regeneration circuit. A ninth valve is disposed on the fifth passage.

9. The device for capturing and regenerating carbon dioxide by alcohol amine absorption method according to claim 8, characterized in that: The heat exchange module includes a first heat exchanger and a second heat exchanger; The outlet of the compression enthalpy increasing module is connected to the inlet of the first side of the first heat exchanger through a first branch, and is connected to the inlet of the first side of the second heat exchanger through a second branch; a tenth valve is provided on the first branch, and an eleventh valve is provided on the second branch; The first passage is connected to an inlet of a second side of the first heat exchanger; the second passage is connected to an outlet of the second side of the first heat exchanger; The inlet of the fifth passage is connected to the inlet of the second side of the second heat exchanger, and the sixth passage is connected to the outlet of the second side of the second heat exchanger.

10. An operating method of an alcohol amine absorption method carbon dioxide capture and regeneration device, characterized in that: Includes at least one of the following operating modes: In the MVC direct compression regeneration mode of the tower top gas, the first subsystem is started. At the beginning, the lean liquid pumped out from the tower bottom is heated by an external heat source to generate initial regeneration steam and return to the tower bottom. The regeneration gas at the top of the tower is compressed and increased in enthalpy by the compression enthalpy increase module, and then the lean liquid pumped out from the tower bottom is heated by the heat exchange module. The regeneration gas after heat exchange enters the condensate tank, the carbon dioxide gas is separated, and the condensate is returned to the regeneration tower; the preset condensate tank liquid level is used as the target value to control the water replenishment flow from the condensate tank to the regeneration tower, and the residual carbon dioxide in the water continues to be regenerated. The lean liquid that is heated and produces steam returns to the tower bottom and flashes to separate steam for the next regeneration; In the MVC composite enthalpy-increasing regeneration mode of the tower top / tower bottom, the second subsystem is started, the liquid level of the gas-liquid separator is preset, and the lean liquid is added to the gas-liquid separator through the tower bottom. After that, the lean liquid supplement flow rate is controlled at the preset liquid level during operation, and the lean liquid pumped out of the gas-liquid separator is heated by an external heat source. The initial regeneration steam is separated by the first compressor through air extraction and flash evaporation and enters the regeneration tower. The regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression and enthalpy-increasing module, and then the circulating lean liquid pumped out of the gas-liquid separator is heated by the heat exchange module. After heat exchange, the regeneration gas enters the condensed water tank, the carbon dioxide gas is separated, and the condensed water returns to the regeneration tower; the lean liquid that is heated and produces steam returns to the gas-liquid separator and is separated by air extraction and flash evaporation by the first compressor, and then enters the regeneration tower for regeneration after pressure and temperature increase; In the MVC enthalpy-increasing regeneration mode of flash evaporation of lean liquid in the tower bottom, the second subsystem is started, the liquid level of the gas-liquid separator is preset, and lean liquid is added to the gas-liquid separator through the tower bottom. After that, the lean liquid supplement flow rate is controlled at the preset liquid level during operation, and the lean liquid pumped out of the gas-liquid separator is heated by an external heat source. The initial regeneration steam is separated by pumping and flashing by the first compressor, and then enters the regeneration tower after being pressurized and heated. The regeneration gas at the top of the tower is compressed and enthalpy-increasing by the compression enthalpy-increasing module, and then the circulating lean liquid pumped out from the gas-liquid separator is heated by the heat exchange module. The regeneration gas enters the condensed water tank after heat exchange, and the carbon dioxide gas is separated. After the first compressor pumps and decompresses the lean liquid in the gas-liquid separator, a small part of steam is flashed and the temperature is reduced. The lean liquid that is heated and produces steam by the heat exchange module returns to the gas-liquid separator, and the flashed steam also enters the first compressor. The first compressor continuously pressurizes and heats the two steam streams and discharges them into the tower bottom for regeneration. In the direct steam regeneration mode of the tower bottom, the third subsystem is started. At the beginning, the lean liquid in the tower bottom is heated by an external heat source to generate initial regeneration steam. The regeneration gas at the top of the tower is compressed and increased in enthalpy by the compression enthalpy increase module and then enters the heat exchange module. After heat exchange, the regeneration gas enters the condensate tank, the carbon dioxide gas is separated, and the condensed water falls. The liquid level of the condensate tank is pre-set and used to control the discharge flow rate of the condensed water in the condensate tank. The discharged condensed water enters the heat exchange module after throttling, reducing the pressure and cooling, and enters the first compressor after heat exchange with the regeneration gas to increase the pressure and temperature, and then is directly discharged into the tower bottom for regeneration.

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