Device for capturing and regenerating carbon dioxide by alcohol amine absorption method

Abstract

The utility model relates to the technical field of rich liquid regeneration of an alcohol amine solution, and provides a carbon dioxide capturing and regenerating device adopting an alcohol amine absorption method, which comprises a regenerating tower, a compression enthalpy increasing module, a heat exchange module, a condensed water tank and a regenerating 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 utility model relates to the technical field of alcohol amine solution rich liquid regeneration, especially to a kind of alcohol amine absorption method carbon dioxide capture regeneration device. BACKGROUND

[0002] Alcohol amine rich liquid regeneration is the main stage of carbon dioxide desorption in alcohol amine method carbon capture system. Alcohol amine method carbon capture is to absorb carbon dioxide with alcohol amine solution to become alcohol amine rich liquid, and the alcohol amine rich liquid after absorption is desorbed to recover alcohol amine solution to realize cyclic utilization of carbon capture type.

[0003] The stage of desorbing and treating alcohol amine rich liquid is called regeneration stage, and under desorption condition, carbon dioxide is separated from alcohol amine solution, which needs to heat rich liquid to achieve carbon dioxide desorption temperature.

[0004] However, in the alcohol amine rich liquid regeneration stage, a large amount of heat in high-temperature regeneration gas is wasted in the condensation process, resulting in high energy consumption, which is a pain point of the regeneration system in the existing alcohol amine method carbon dioxide capture device.

[0005] Therefore, how to effectively recycle waste heat and reduce energy consumption is an important issue to be solved at present. INVENTION CONTENTS

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

[0007] The utility model provides a kind of alcohol amine absorption method carbon dioxide capture regeneration device, comprising: regeneration tower, compression enthalpy increasing module, heat exchange module, condensate tank and regeneration system;

[0008] The top of the regeneration tower is provided with a regeneration gas outlet; the inlet of the compression enthalpy increasing module is connected with the regeneration gas outlet, for compressing and increasing enthalpy of regeneration gas;

[0009] The heat exchange module is provided with a first side and a second side, the inlet of the first side is connected with the outlet of the compression enthalpy increasing module, the outlet of the first side is connected with the condensate tank, and the condensate outlet of the condensate tank is connected to the regeneration tower.

[0010] The regeneration tower is connected with the second side of the heat exchange module through the regeneration system, for recycling waste heat in regeneration gas to the regeneration tower by heat exchange.

[0011] According to the alcohol amine absorption method carbon dioxide capture regeneration device provided by the utility model, the regeneration system comprises a first subsystem, and the first subsystem comprises a first loop.

[0012] The inlet of the first loop is connected with the tower kettle of the regeneration tower, and the outlet is connected back to the tower kettle of the regeneration tower through the second side; and a pump body is arranged on the first loop.

[0013] According to the carbon dioxide capture and regeneration device for the alcohol amine absorption method, the regeneration system comprises a second subsystem, the second subsystem comprises a gas-liquid separator, a second loop and a regeneration loop;

[0014] The liquid inlet of the gas-liquid separator is connected with the tower kettle of the regeneration tower through a pump body; the inlet of the second loop is connected with the liquid outlet of the gas-liquid separator, and the outlet is connected back to the gas-liquid separator through the second side;

[0015] A pump body is arranged on the second loop; the steam outlet of the gas-liquid separator is connected to the tower kettle of the regeneration tower through the regeneration loop, and a first compressor is arranged on the regeneration loop.

[0016] According to the carbon dioxide capture and regeneration device for the alcohol amine absorption method, the regeneration system comprises a third subsystem, the third subsystem comprises a third loop and a regeneration loop;

[0017] The inlet of the third loop is connected with the condensate water outlet of the condensate water tank, the outlet is connected with the regeneration loop through the second side, the regeneration loop is connected to the tower kettle of the regeneration tower, a pump body is arranged on the third loop, and a first compressor is arranged on the regeneration loop.

[0018] According to the carbon dioxide capture and regeneration device for the alcohol amine absorption method, the regeneration system comprises:

[0019] A first subsystem comprises a first loop, the inlet of the first loop is connected with the tower kettle of the regeneration tower, and the outlet is connected back to the tower kettle of the regeneration tower through the second side;

[0020] A second subsystem comprises a gas-liquid separator, a second loop and a regeneration loop; the liquid inlet of the gas-liquid separator is connected with the tower kettle; the inlet of the second loop is connected with 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 a first compressor is arranged on the regeneration loop;

[0021] A third subsystem comprises a third loop and the regeneration loop; the inlet of the third loop is connected with the condensate water outlet of the condensate water tank, and the outlet is connected to the regeneration loop through the second side.

[0022] The utility model provides a kind of carbon dioxide capture and regeneration device of alcohol amine absorption method, the first circuit includes:

[0023] First passage, inlet is connected with the tower kettle, and the inlet of second side is connected with the first passage;First valve and first pump body are equipped on the first passage;

[0024] Second passage, the outlet of second side is connected with the inlet of the second passage, and the outlet is connected to the tower kettle;Second valve is equipped on the second passage.

[0025] The utility model provides a kind of carbon dioxide capture and regeneration device of alcohol amine absorption method, third valve and second pump body are equipped between the liquid inlet of gas-liquid separator and the tower kettle;Fourth valve is equipped at the steam outlet of gas-liquid separator, and fifth valve is equipped on the regeneration circuit;The second circuit includes:

[0026] The first passage and the second passage;

[0027] Third passage, inlet is connected with the liquid outlet of gas-liquid separator, and the outlet of first passage is connected with the third passage, and sixth valve is equipped on the third passage;

[0028] Fourth passage, inlet is connected with the second passage, and the middle part of gas-liquid separator is connected with the outlet of fourth passage, and seventh valve is equipped on the fourth passage.

[0029] The utility model provides a kind of carbon dioxide capture and regeneration device of alcohol amine absorption method, the third circuit includes:

[0030] Fifth passage, inlet is connected with the condensate water outlet of condensate water tank, and the inlet of second side is connected with the outlet of fifth passage by third pump body;Eighth valve is equipped at the outlet of fifth passage;

[0031] Sixth passage, inlet is connected with the outlet of second side, and the outlet of sixth passage is connected with the regeneration circuit, and ninth valve is equipped on the fifth passage.

[0032] The utility model provides a kind of carbon dioxide capture and regeneration device of alcohol amine absorption method, the compression enthalpy increasing module includes regeneration gas pipeline and second compressor;The inlet of regeneration gas pipeline is connected with the regeneration gas outlet, and the outlet is connected to the inlet of first side by second compressor.

[0033] The utility model provides a kind of carbon dioxide capture and regeneration device of alcohol amine absorption method, the heat exchange module includes first heat exchanger and second heat exchanger;

[0034] 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 connected to the inlet of the first side of the second heat exchanger through a second branch; the tenth valve is arranged on the first branch, and the eleventh valve is arranged on the second branch;

[0035] The first passage is connected to the inlet of the second side of the first heat exchanger; and the second passage is connected to the outlet of the second side of the first heat exchanger.

[0036] 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.

[0037] According to the carbon dioxide capture and regeneration device for the alcohol amine absorption method, the condensate outlet of the condensate tank is connected with the fourth pump body and the twelfth valve.

[0038] According to the carbon dioxide capture and regeneration device for the alcohol amine absorption method, the condensate outlet of the condensate tank is connected with the fourth pump body and the twelfth valve.

[0039] According to the carbon dioxide capture and regeneration device for the alcohol amine absorption method, the condensate outlet of the condensate tank is connected with the fourth pump body and the twelfth valve.

[0040] The utility model discloses still provide a kind of operation method of carbon dioxide capture and regeneration device for the alcohol amine absorption method, including at least one of the following operating modes:

[0041] In the MVC direct compression regeneration mode of tower top gas, start the first subsystem, at the beginning, generate initial regeneration steam by heating the lean liquid discharged from the tower kettle by external heat source and return to the tower kettle, and the regeneration gas at the top of the tower is compressed by the compression enthalpy-increasing module and then heated by the heat exchange module to heat the lean liquid discharged from the tower kettle, and the regenerated gas after heat exchange enters the condensate tank, carbon dioxide gas is separated, and the condensate water returns to the regeneration tower; the condensate tank liquid level is set as the target value, and the condensate tank is controlled to the water flow of the regeneration tower, the residual carbon dioxide in the water is continuously regenerated, the lean liquid with temperature rise and steam is returned to the tower kettle and flash separation steam is used for the next regeneration;

[0042] In the MVC compound enthalpy-increasing regeneration mode of the column top / column base, the second subsystem is started, the gas-liquid separator liquid level is preset, the lean liquid is supplemented into the gas-liquid separator through the column base, and then the lean liquid supplement flow is controlled according to the preset liquid level in the running process. The lean liquid discharged from the gas-liquid separator is heated by an external heat source, the initial regeneration vapor is separated by the flash evaporation of the lean liquid by the first compressor, and the lean liquid is pressurized and heated to enter the regeneration column. The regeneration gas at the top is compressed and increased in enthalpy by the compression enthalpy-increasing module, and then the lean liquid 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 water returns to the regeneration column. The lean liquid that is heated and generates steam returns to the gas-liquid separator and is separated by the flash evaporation of the lean liquid by the first compressor to generate steam, which is pressurized and heated to enter the regeneration column for regeneration.

[0043] In the MVC enthalpy-increasing regeneration mode of the column base lean liquid flash evaporation, the second subsystem is started, the gas-liquid separator liquid level is preset, the lean liquid is supplemented into the gas-liquid separator through the column base, and then the lean liquid supplement flow is controlled according to the preset liquid level in the running process. The lean liquid discharged from the gas-liquid separator is heated by an external heat source, the initial regeneration vapor is separated by the flash evaporation of the lean liquid by the first compressor, and the lean liquid is pressurized and heated to enter the regeneration column. The regeneration gas at the top is compressed and increased in enthalpy by the compression enthalpy-increasing module, and then the lean liquid 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 lean liquid in the gas-liquid separation vessel is flash evaporated by the first compressor to generate a small amount of steam and reduce the temperature. The lean liquid that is heated and generates steam by the heat exchange module returns to the gas-liquid separator, and the flash evaporated steam also enters the first compressor. The first compressor continuously pressurizes and heats the two streams of steam to be discharged into the column base for regeneration.

[0044] In the MVC direct steam regeneration mode of the column base, the third subsystem is started. At the beginning, the column base lean liquid is heated by an external heat source to generate initial regeneration vapor. The regeneration gas at the top is compressed and increased in enthalpy by the compression enthalpy-increasing module, and then enters the heat exchange module. The regeneration gas after heat exchange enters the condensate tank, the carbon dioxide gas is separated, and the condensate water falls. The liquid level of the condensate tank is preset and used to control the discharge flow of the condensate water in the condensate tank. The discharged condensate water is throttled, depressurized and cooled, and then enters the heat exchange module. After heat exchange with the regeneration gas, it enters the first compressor to be pressurized and heated, and then is directly discharged into the column base for regeneration.

[0045] Advantages:

[0046] I. The regeneration gas is heat-exchanged with the regeneration system after being compressed and increased in enthalpy, and the heat in the regeneration gas is recovered to the regeneration column through the regeneration system for repeated use, so that the latent heat energy in the regeneration gas is fully recovered and utilized, the thermal efficiency is improved, the system energy consumption is reduced, and energy is saved.

[0047] II. There is no need to use chemical refrigerant to cool and condense the regeneration gas, which fundamentally eliminates the pollution of refrigerant leakage to the environment.

[0048] Three, multiple line selection, higher degree of automation, according to the required regeneration temperature, carbon dioxide capture rate, power consumption, etc. requirements, can select the appropriate MVC enthalpy regeneration line, and only need to switch the line by controlling the opening and closing of different valves and pump operation, the same compressor and pump body using different control strategies can play multiple roles.

[0049] Four, through the MVC enthalpy regeneration mode of the tower kettle lean liquid flash, the required temperature of lean liquid evaporation can be reduced, and the required regeneration gas compression condensation temperature can be reduced, the water vapor content in the carbon dioxide is reduced, so that a larger proportion of water vapor can participate in heat exchange and condensation, release more heat to evaporate more water in the lean liquid, produce more water vapor to desorb more carbon dioxide in the rich liquid, improve the yield of the entire carbon dioxide capture system; The required water vapor temperature is lower, and the required compressor power is also lower. BRIEF DESCRIPTION OF DRAWINGS

[0050] In order to more clearly illustrate the technical scheme of the present application or the prior art, the following will briefly introduce the drawings needed to be used in the embodiment or the prior art description. Obviously, the drawings described below are some embodiments of the present application, and those skilled in the art can also obtain other drawings according to these drawings without creating labor.

[0051] Figure 1 It is a structure diagram of the alcohol amine absorption method carbon dioxide capture regeneration device provided by the embodiment of the present application.

[0052] Reference signs:

[0053] 10, regeneration tower; 20, compression enthalpy module; 200, regeneration gas pipeline; 201, second compressor; 202, first branch; 203, second branch; 204, twelve valve; 205, thirteen valve; 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, first pump body; 514, second valve; 520, gas-liquid separator; 521, third valve; 522, second pump body; 523, fourth valve; 524, third passage; 525, fourth passage; 526, sixth valve; 527, seventh valve; 530, regeneration loop; 531, first compressor; 532, fifth valve; 540, fifth passage; 541, sixth passage; 542, third pump body; 543, eighth valve; 544, ninth valve; 550, emptying pipe; 551, eleven valve. DETAILED DESCRIPTION

[0054] In order to make the purpose, technical scheme and advantages of the utility model clearer, the technical scheme in the utility model will be described clearly and completely in combination with the drawings in the utility model below. Obviously, the described embodiments are part of the embodiments of the utility model, rather than all the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by the ordinary skilled in the art without creative labor belong to the protection scope of the utility model.

[0055] In order to facilitate understanding of the alcohol amine absorption method carbon dioxide capture regeneration device provided by the utility model, first, the application background thereof is introduced, and alcohol amine rich liquid regeneration is the most important link in the alcohol amine method carbon capture system. In the regeneration stage, carbon dioxide is separated from the alcohol amine rich liquid, and alcohol amine lean liquid recovery realizes cyclic utilization. In the entire regeneration stage, the temperature of the rich liquid needs to be ensured to reach the carbon dioxide desorption condition through heating.

[0056] However, continuous heating not only increases the energy consumption cost of the entire system, and a large amount of heat in the high-temperature regeneration gas will be wasted in the subsequent condensation separation section, resulting in high energy consumption. The high energy consumption has been a pain point of the regeneration system in the existing alcohol amine method carbon dioxide capture device.

[0057] Therefore, how to effectively recycle the waste heat and reduce the energy consumption is an important topic to be solved at present.

[0058] In view of the above technical problems, the utility model provides an alcohol amine absorption method carbon dioxide capture regeneration device, which can effectively recycle the waste heat in the high-temperature regeneration gas and reduce the system energy consumption.

[0059] The alcohol amine absorption method carbon dioxide capture regeneration device of the utility model will be described below in combination with Figure 1 The alcohol amine absorption method carbon dioxide capture regeneration device of the utility model will be described below in combination with

[0060] Referring to Figure 1 An alcohol amine absorption method carbon dioxide capture regeneration device, comprising a regeneration tower 10, a compression enthalpy increasing module 20, a heat exchange module 30, a condensate tank 40 and a regeneration system 50. The top of the regeneration tower 10 is provided with a regeneration gas outlet. The inlet of the compression enthalpy increasing module 20 is connected with the regeneration gas outlet, and is used 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 with the outlet of the compression enthalpy increasing module 20, the outlet of the first side is connected with the condensate tank 40, and the condensate outlet of the condensate tank 40 is connected to the regeneration tower 10. The regeneration tower 10 is connected with the second side of the heat exchange module 30 through the regeneration system 50, and is used for recycling the waste heat in the regeneration gas to the regeneration tower 10 through heat exchange.

[0061] In actual application, the high-temperature regenerated gas is discharged through the regenerated gas outlet at the top of the regeneration tower 10, the compression enthalpy increasing module 20 can increase the enthalpy of the regenerated gas to increase the temperature of the regenerated gas, the regenerated gas after compression enthalpy increase enters the heat exchange module 30 to exchange heat with the regeneration system 50, so that the regeneration system 50 recovers the heat in the regenerated gas to the regeneration tower 10 for reuse, and the regenerated gas after heat exchange enters the condensate tank 40 to condense, the condensate falls down and returns to the regeneration tower 10, and the carbon dioxide gas is separated out.

[0062] Compared with the related art, the regenerated gas is exchanged heat with the regeneration system 50 after compression enthalpy increase, and the heat in the regenerated gas is recovered to the regeneration tower 10 for reuse through the regeneration system 50, so that the latent heat energy in the regenerated gas can be fully recovered and utilized, the thermal efficiency is improved, the system energy consumption is reduced, and the energy is saved; in addition, the regenerated gas does not need to be cooled and condensed by using chemical refrigerant, and the pollution of the leakage of the working medium to the environment is fundamentally eliminated.

[0063] As an optional embodiment of the utility model, the regeneration system 50 comprises a first subsystem, and the first subsystem comprises a first loop; the inlet of the first loop is connected with the tower kettle of the regeneration tower 10, the outlet is connected back to the tower kettle of the regeneration tower 10 through the second side of the heat exchange module 30, and a pump body is arranged on the first loop.

[0064] Through the technical scheme of the embodiment, the MVC tower top gas direct compression regeneration mode can be realized, in this mode, the first subsystem is started, the initial regenerated steam is generated by heating the lean liquid discharged from the tower kettle by an external heat source at the beginning and the initial regenerated steam is returned to the tower kettle, the regenerated gas at the top is compressed and increased in enthalpy by the compression enthalpy increasing module 20, then the regenerated gas after heat exchange heats the lean liquid discharged from the tower kettle through the heat exchange module 30, the regenerated gas after heat exchange enters the condensate tank 40, the carbon dioxide gas is separated out, the condensate falls down and returns to the regeneration tower 10, the condensate tank 40 is controlled to supply water to the regeneration tower 10 at a target value of the preset condensate tank 40 liquid level, the residual carbon dioxide in the water is continuously separated out, the lean liquid that is heated and generates steam returns to the tower kettle and is separated out by flashing to generate steam for the next regeneration.

[0065] Specifically, the MVC tower top gas direct compression regeneration mode is suitable for the case that the water vapor content in the regenerated gas is high, for example, when the water vapor content in the regenerated gas reaches CO2: H2O = 1: 3 and above, the MVC tower top gas direct compression regeneration mode can be selected for regeneration.

[0066] As an optional embodiment of the utility model, the regeneration system 50 comprises a second subsystem, the second subsystem comprises a gas-liquid separator 520, a second loop and a regeneration loop 530; the liquid inlet of the gas-liquid separator 520 is connected with the tower kettle of the regeneration tower 10 through a pump body; the inlet of the second loop is connected with 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 arranged on the second loop, and the steam outlet of the gas-liquid separator 520 is connected to the tower kettle of the regeneration tower 10 through the regeneration loop 530, and a first compressor 531 is arranged on the regeneration loop 530.

[0067] Through the technical scheme of the embodiment, the tower top / tower kettle MVC composite enthalpy-increasing regeneration mode and the tower kettle lean liquid flash MVC enthalpy-increasing regeneration mode can be realized.

[0068] In the tower top / tower kettle MVC composite enthalpy-increasing regeneration mode, the second subsystem is started, the liquid level of the gas-liquid separator 520 is pre-set, the lean liquid is supplemented into the gas-liquid separator 520 through the tower kettle to the pre-set liquid level, and then the lean liquid supplement flow is controlled at the pre-set liquid level in the running process, the lean liquid discharged from the gas-liquid separator 520 is heated by an external heat source, the initial regeneration steam is separated out by the gas flash of the first compressor 531 and enters the regeneration tower 10, the regeneration gas at the tower top is compressed and increased in enthalpy by the compression enthalpy-increasing module 20, heated by the heat exchange module 30 from the circulating lean liquid discharged from the gas-liquid separator 520, enters the condensate tank 40 after heat exchange of the regeneration gas, the carbon dioxide gas is separated and rises, the condensate falls back to the regeneration tower 10, the condensate tank 40 is controlled to the target value of the pre-set condensate tank 40 liquid level, the water supplement flow of the condensate tank 40 to the regeneration tower 10, the residual carbon dioxide in the water is continuously regenerated, the lean liquid that is heated and produces steam returns to the gas-liquid separator 520 and is separated out by the gas flash of the first compressor 531, the steam is increased in pressure and temperature and enters the regeneration tower 10 for regeneration.

[0069] Specifically, the tower top / tower kettle MVC composite enthalpy-increasing regeneration mode is suitable for the case that the water vapor content in the regeneration gas is medium, for example, when the water vapor content in the regeneration gas reaches CO2:H2O=1:1.5 or so, the tower top / tower kettle MVC composite enthalpy-increasing regeneration mode can be selected for regeneration.

[0070] In the MVC enthalpy-increasing regeneration mode of the flash evaporation of lean liquid in the tower kettle, the second subsystem is started, the liquid level of the gas-liquid separator 520 is pre-set, the lean liquid is supplemented into the gas-liquid separator 520 to the pre-set liquid level through the tower kettle, then the lean liquid supplement flow is controlled at the pre-set liquid level in the running process, the lean liquid discharged from the gas-liquid separator 520 is heated by an external heat source, the initial regeneration steam is separated out by the flash evaporation of the lean liquid by the first compressor 531 and then enters the regeneration tower 10 after being pressurized and heated, the regeneration gas at the top of the tower is compressed and increased in enthalpy by the compression enthalpy-increasing module 20, then the regeneration gas is heated by the circulating lean liquid discharged from the gas-liquid separator 520 by the heat exchange module 30, and then the regeneration gas enters the condensate tank 40 after heat exchange, the carbon dioxide gas is separated, the condensate water returns to the regeneration tower 10, the water supplement flow of the condensate tank 40 to the regeneration tower 10 is controlled with the pre-set condensate tank 40 liquid level as the target value, the residual carbon dioxide in the water continues to be regenerated, a small part of steam is flashed out by the lean liquid in the flash evaporation of the lean liquid in the gas-liquid separation tank 520 by the first compressor 531 and the temperature is reduced, the lean liquid is heated by the heat exchange module 30 and the lean liquid generates steam and returns to the gas-liquid separation tank 520, the steam flashed out also enters the first compressor 531, and the first compressor 531 continuously pressurizes and heats the two streams of steam and discharges them into the tower kettle for regeneration.

[0071] In the MVC enthalpy-increasing regeneration mode of the flash evaporation of lean liquid in the tower kettle, the temperature required for the evaporation of the lean liquid can be reduced, the condensation temperature of the compressed regeneration gas can be reduced, the water vapor content in the carbon dioxide can be reduced, a larger proportion of water vapor can participate in heat exchange and condensation, more heat can be released to evaporate more water in the lean liquid, more water vapor can be generated to desorb more carbon dioxide in the rich liquid, the yield of the entire carbon dioxide capture system can be improved, the required water vapor temperature is lower, and the required compressor power is also lower.

[0072] Specifically, the MVC enthalpy-increasing regeneration mode of the flash evaporation of lean liquid in the tower kettle is suitable for the case that the water vapor content in the regeneration gas is low, for example, when the water vapor content in the regeneration gas is less than or equal to CO2:H2O=1:1.2, the MVC enthalpy-increasing regeneration mode of the flash evaporation of lean liquid in the tower kettle can be selected for regeneration.

[0073] As an optional embodiment of the utility model, the regeneration system 50 includes a third subsystem, the third subsystem includes a third loop and a regeneration loop 530; wherein the inlet of the third loop is connected with the condensate water outlet of the condensate tank 40, the outlet is connected with the regeneration loop 530 through the second side, the regeneration loop 530 is connected to the tower kettle of the regeneration tower 10, a pump body is arranged on the third loop, and the first compressor 531 is arranged on the regeneration loop 530.

[0074] Through the technical scheme of the embodiment, the tower kettle direct steam regeneration mode can be realized, in which mode, the third subsystem is started, and initially, the initial regeneration steam is generated by heating the tower kettle lean liquid through the external heat source, the overhead regeneration gas enters the heat exchange module 30 after being compressed and enthalpy-increased by the compression enthalpy-increasing module 20, and enters the condensate tank 40 after heat exchange, the carbon dioxide gas is separated, and the condensate falls down, the liquid level of the condensate tank 40 is preset and used to control the discharge flow of the condensate in the condensate tank 40, the discharged condensate enters the heat exchange module 30 after being throttled, decompressed and cooled, and enters the first compressor 531 after heat exchange with the regeneration gas, and is directly discharged into the tower kettle for regeneration.

[0075] Specifically, when the lean-liquid and rich-liquid circulation amount changes and increases or is not suitable for being discharged by the branch road, the tower kettle direct steam regeneration mode is suitable for being selected for regeneration.

[0076] In some optional embodiments of the utility model, one, two or three of the first subsystem, the second subsystem and the third system can exist in the regeneration system 50, and specifically, the actual requirements can be flexibly configured.

[0077] In the embodiment, the first subsystem, the second subsystem and the third subsystem are simultaneously included in the regeneration system 50, so that multiple optional routes can be provided, the degree of automation is higher, and the suitable MVC enthalpy-increasing regeneration circuit can be selected according to the required regeneration temperature, the carbon dioxide capture rate, the power consumption and the like, so that the best mode matching is realized, and the waste heat utilization efficiency and the cost efficiency are improved.

[0078] In order to facilitate the switching of the lines between different subsystems and realize the switching of different operation modes, in one embodiment of the utility model, with reference to Figure 1 , the first circuit includes the first passage 510 and the second passage 511; the inlet of the first passage 510 is connected with the tower kettle, the outlet is connected with the inlet of the second side of the heat exchange module 30, the first passage 510 is provided with the first valve 512 and the first pump body 513; the inlet of the second passage 511 is connected with 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 the second valve 514.

[0079] As a specific scheme of the embodiment, the liquid inlet of the gas-liquid separator 520 and the tower kettle are provided with a third valve 521 and a second pump body 522, the steam outlet of the gas-liquid separator 520 is provided with a fourth valve 523, and the regeneration loop 530 is provided with a fifth valve 532; the second loop includes the first passage 510, the second passage 511, a third passage 524 and a fourth passage 525; the inlet of the third passage 524 is connected with the liquid outlet of the gas-liquid separator 520, the outlet is connected with 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 with the second passage 511 and the connection point is located upstream of the second valve 514, and the outlet is connected to the middle part of the gas-liquid separator 520, and the fourth passage 525 is provided with a seventh valve 527.

[0080] As a specific scheme of the embodiment, the third loop includes a fifth passage 540 and a sixth passage 541, wherein the inlet of the fifth passage 540 is connected with the condensate outlet of the condensate tank 40, the outlet is connected with the inlet of the second side of the heat exchange module 30 through a 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 with the outlet of the second side of the heat exchange module 30, and the outlet is connected with the regeneration loop 530, and the sixth passage 541 is provided with a ninth valve 544.

[0081] As a specific scheme of the embodiment, the eighth valve 543 at the outlet of the fifth passage 540 can simultaneously serve as a throttling valve, for throttling and depressurizing and cooling the condensate, so that part of the condensate is rapidly evaporated and converted into gas.

[0082] As a specific scheme of the embodiment, the condensate outlet of the condensate tank 40 is connected with the upper side of the regeneration tower 10 through a seventh passage 400, and the seventh passage 400 is provided with a fourth pump body 401 and a tenth valve 402. The condensate in the condensate tank 40 can return to the regeneration tower 10 through the seventh passage 400.

[0083] As a specific scheme of the embodiment, the condensate outlet of the condensate tank 40 has two condensate outlets, one of which is connected with the inlet of the second side of the heat exchange module 30 through the fifth passage 540, and the other of which is connected with the regeneration tower 10 through the seventh passage 400.

[0084] As a specific scheme of the embodiment, in order to facilitate the regulation of the lean liquid flow in the regeneration system 50, the regeneration system 50 further includes a venting pipe 550 for venting the lean liquid in the regeneration system 50, and the venting pipe 550 is provided with an eleventh valve 551.

[0085] As a specific scheme of the embodiment, the emptying 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 degree of the eleventh valve 551, the lean liquid flow in the regeneration system 50 can be controlled, and the liquid level of the tower kettle can be adjusted.

[0086] By adopting the technical scheme, the switching of the line can be achieved by only controlling the opening and closing of different valves and the operation of the pump body. Different control strategies of the same compressor and pump body can play multiple roles.

[0087] As a specific scheme of the embodiment, the switching of the operation mode can be performed in the following manner:

[0088] 1) In the tower top gas MVC direct compression regeneration mode, the first valve 512, the second valve 514, the tenth valve 402, and the eleventh valve 551 are opened, and other valves are closed. Initially, the lean liquid pumped out of the tower kettle by the first pump body 513 is heated by an external heat source to generate initial regeneration steam. The initial regeneration steam returns to the tower kettle through the first circuit. The regeneration steam at the top of the tower is compressed to increase the enthalpy and then enters the heat exchange module 30 to transfer heat to the lean liquid pumped out of the tower kettle by the first pump body 513. The regenerated gas after heat exchange enters the condensate tank 40, and the carbon dioxide gas rises and separates. The condensed water falls down. The liquid level of the condensate tank 40 is set as a target value, the frequency of the fourth pump body 401 is controlled to control the water supply amount to the regeneration tower 10, and the residual carbon dioxide in the water is continuously regenerated. The lean liquid that is warmed and generates steam returns to the tower kettle and is flashed to separate the steam for the next regeneration. The first pump body 513 has a fixed frequency, the opening degree of the eleventh valve 551 is adjusted with the preset tower kettle liquid level as a target value, and the lean liquid flow discharged from the regeneration system 50 is controlled.

[0089] 2) In the MVC compound enthalpy regeneration mode of the tower top / tower kettle, open 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, close other valves, pre-set the liquid level of the gas-liquid separator 520, control the second pump body 522 to supplement the lean liquid into the gas-liquid separator 520 to the pre-set liquid level, then control the frequency of the second pump body 522 with the pre-set liquid level of the gas-liquid separator 520 as the target value, thereby controlling the lean liquid supplement flow, heating the lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513 by an external heat source, separating the initial regeneration steam from the lean liquid by the first compressor 531 to enter the regeneration tower 10, and the regeneration gas at the top of the tower is compressed and increased in enthalpy by the compression enthalpy module 20, then heated by the heat exchange module 30 to the circulating lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513, enters the condensate tank 40 after the heat exchange of the regeneration gas, separates the carbon dioxide gas, returns to the regeneration tower 10 in the same way as above, the lean liquid with increased temperature and generated steam returns to the gas-liquid separator 520 and is separated into steam by the first compressor 531, and enters the regeneration tower 10 for regeneration after being pressurized and increased in temperature by the first compressor 531, wherein the first pump body 513 is fixed in frequency, the opening of the eleventh valve 551 is adjusted with the pre-set tower kettle liquid level as the target value, and the lean liquid flow out of the regeneration system 50 is controlled.

[0090] 3) In the MVC enthalpy regeneration mode of the tower kettle lean liquid flash, open 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, close other valves, pre-set the liquid level of the gas-liquid separator 520, control the second pump body 522 to supplement the lean liquid into the gas-liquid separator 520, then control the frequency of the second pump body 522 with the pre-set liquid level of the gas-liquid separator 520 as the target value, thereby controlling the lean liquid supplement flow, heating the lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513 by an external heat source, separating the initial regeneration steam from the lean liquid by the first compressor 531 to enter the regeneration tower 10, and the regeneration gas at the top of the tower is compressed and increased in enthalpy, then heated by the heat exchange module 30 to the circulating lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513, enters the condensate tank 40 after the heat exchange of the regeneration gas, separates the carbon dioxide gas, returns to the regeneration tower 10 in the same way as above, the lean liquid with increased temperature and generated steam returns to the gas-liquid separator 520 after being flash vaporized by the first compressor 531 to reduce the pressure of the lean liquid in the gas-liquid separator 520, and the lean liquid is heated and generates steam by the heat exchange module 30, the flash vaporized steam also enters the first compressor 531, and the first compressor 531 continuously pressurizes and increases the temperature of the two streams of steam to be discharged into the tower kettle for regeneration, wherein the first pump body 513 is fixed in frequency, the opening of the eleventh valve 551 is adjusted with the pre-set tower kettle liquid level as the target value, and the lean liquid flow out of the regeneration system 50 is controlled.

[0091] 4) In the tower kettle direct steam regeneration mode, the eighth valve 543, the ninth valve 544 and the fifth valve 532 are opened, and other valves are closed, at the beginning, the initial regeneration steam is generated by heating the tower kettle lean liquid through an external heat source, the tower top regeneration gas is compressed and enthalpy-increased by the compression enthalpy-increasing module 20, enters the heat exchange module 30 after being heat-exchanged, enters the condensate tank 40 after being heat-exchanged, the carbon dioxide gas is separated, the condensate falls down, the liquid level of the condensate tank 40 is preset and used to control the frequency of the third pump body 542, and then the discharge flow of the condensate, the discharged condensate enters the heat exchange module 30 after being throttled, decompressed and cooled, is heat-exchanged with the regeneration gas, enters the first compressor 531 after being pressurized and heated, and is directly discharged into the tower kettle for regeneration, wherein the opening degree of the eighth valve 543 is adjusted by taking the temperature of the condensate at the inlet of the heat exchange module 30 as a target, and the condensate flow discharged from the condensate tank 40 is controlled.

[0092] As an optional embodiment of the utility model, the compression enthalpy-increasing module 20 includes a regeneration gas pipeline 200 and a second compressor 201, wherein the inlet of the regeneration gas pipeline 200 is connected with 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.

[0093] 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-increasing module 20 is connected to the inlet of the first side of the first heat exchanger 300 through a first branch 202 and connected to the inlet of the first side of the second heat exchanger 301 through a second branch 203, the first branch 202 is provided with a twelfth valve 204, and the second branch 203 is provided with a thirteenth valve 205, the first passage 510 is connected with the inlet of the second side of the first heat exchanger 300, the second passage 511 is connected with the outlet of the second side of the first heat exchanger 300, and the inlet of the fifth passage 540 is connected with the inlet of the second side of the second heat exchanger 301, and the sixth passage 541 is connected with the outlet of the second side of the second heat exchanger 301.

[0094] As a specific scheme of the embodiment, in the tower top gas MVC direct compression regeneration mode, the tower top / tower kettle MVC composite enthalpy-increasing regeneration mode and the tower kettle lean liquid flash evaporation MVC enthalpy-increasing regeneration mode, the twelfth valve 204 is opened, heat exchange is carried out through the first heat exchanger 300, and in the tower kettle direct steam regeneration mode, the thirteenth valve 205 is opened, heat exchange is carried out through the second heat exchanger 301.

[0095] In an embodiment of the utility model, the first compressor 531 has an air extraction function, and is used for air extraction flash evaporation of the gas-liquid separator 520.

[0096] It can be understood that, without mutual contradiction, the person skilled in the art can combine and combine the different embodiments or examples described in the specification and the features of the different embodiments or examples.

[0097] The operation method of the carbon dioxide capture and regeneration device by alcohol amine absorption method provided by the utility model is described below, and the operation method of the carbon dioxide capture and regeneration device by alcohol amine absorption method described below can be correspondingly referred to the carbon dioxide capture and regeneration device by alcohol amine absorption method described above.

[0098] An operation method of a carbon dioxide capture and regeneration device by alcohol amine absorption method, comprising at least one of a tower top gas MVC direct compression regeneration mode, a tower top / tower kettle MVC composite enthalpy increase regeneration mode, a tower kettle lean liquid flash MVC enthalpy increase regeneration mode and a tower kettle direct steam regeneration mode.

[0099] The operation methods of the four modes are described in detail below by taking the alcohol amine absorption method with an alcohol amine solution circulation amount of 0.5 m³ / h, a carbon dioxide regeneration amount of 18 kg / h and a regeneration temperature of 100°C as an example:

[0100] 1) In the tower top gas MVC direct compression regeneration mode, the first valve 512, the second valve 514, the tenth valve 402, the eleventh valve 551 and the twelfth valve 204 are opened, and other valves are closed. At the beginning, about 27 kg / h of external steam at 110°C is introduced into the first heat exchanger 300 to heat about 2000 kg / h of circulating lean liquid pumped from the tower kettle by the first pump body 513 to about 100°C, generating about 27 kg / h of 100°C saturated steam back to the tower kettle. The steam rises along the tower to desorb carbon dioxide into mixed regeneration gas which is discharged from the tower top of the regeneration tower 10. The mixed regeneration gas is sucked into and pressurized to a saturated temperature of about 110°C by the second compressor 201, enters the first heat exchanger 300 to transfer heat to the circulating lean liquid pumped from the tower kettle by the first pump body 513, and then enters the condensate tank 40. About 18 kg / h of carbon dioxide gas is separated and discharged, and about 27 kg / h of condensate falls. The liquid level of the condensate tank 40 is set as a target value, and the frequency of the fourth pump body 401 is controlled by PID to control the water supply to the regeneration tower 10 at about 27 kg / h. The residual carbon dioxide in the water continues to be regenerated; the circulating lean liquid which is heated and generates steam returns to the tower kettle and is separated by flash evaporation to about 27 kg / h of 100°C saturated steam which is used for the next regeneration; wherein the first pump body 513 and the second compressor 201 have fixed frequencies, and the eleventh valve 551 is adjusted to control the discharge of about 0.5 m³ / h of lean liquid from the regeneration system 50 with the tower kettle liquid level as a target value.

[0101] 2) In the MVC composite enthalpy-increasing regeneration mode of the top / tower kettle, open 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, close other valves, pre-set the liquid level of the gas-liquid separator 520, control the second pump body 522 to supplement the lean liquid into the gas-liquid separator 520 to the pre-set liquid level, then about 27 kg / h, 110°C external steam is introduced into the first heat exchanger 300 to heat about 2000 kg / h, preheated to 100°C, the circulating lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513, at the same time, the second pump body 522 is opened to control the second pump body 522 frequency to control about 0.53 m³ / h of lean liquid from the tower kettle to the gas-liquid separator 520 at the pre-set liquid level as the target value, 27 kg / h, 100°C saturated steam is separated out by the first compressor 531 to enter the regeneration tower 10, the regenerated gas in the regeneration tower 10 is sucked in by the second compressor 201 and pressurized and heated to saturated 110°C, then enters the first heat exchanger 300 to transfer heat to the circulating lean liquid pumped out of the gas-liquid separator 520 by the first pump body 513, the regenerated gas after heat exchange enters the condensate tank 40 to supplement water to the regeneration tower 10 in the same way as above, about 18 kg / h of carbon dioxide is separated out; the circulating lean liquid which is heated and produces steam returns to the gas-liquid separator 520 and is separated out by the first compressor 531 to about 27 kg / h, 100°C 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 are fixed frequency, the eleventh valve 551 is adjusted to control about 0.5 m³ / h of lean liquid to be discharged from the regeneration system 50 with the tower kettle liquid level as the target value.

[0102] 3) In the MVC flash regeneration mode of the tower kettle lean liquid, open 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, close other valves, at the beginning, first through the tower kettle electric heating and into the first heat exchanger 300 steam and circulating lean liquid to preheat the tower kettle lean liquid to 100℃, pre-set the liquid level of the gas-liquid separator 520, control the second pump body 522 to supplement the lean liquid to the pre-set liquid level in the gas-liquid separator 520, then the first compressor 531 is used to flash a small part of the steam in the gas-liquid separator 520 and the temperature is reduced to 90℃, at the same time, about 27kg / h, 100℃ external steam is introduced into the first heat exchanger 300 to heat about 2000kg / h, 90℃ circulating lean liquid 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 separated from the 27kg / h, 90℃ saturated steam by the first compressor 531 and is pressurized and heated to the saturated temperature 100℃ into the regeneration tower 10, at the same time, the second pump body 522 is opened, the second pump body 522 is controlled by the frequency to control the supplement of about 0.53m³ / h lean liquid from the tower kettle to the gas-liquid separator 520, taking the pre-set liquid level of the gas-liquid separator 520 as the target value; the regeneration gas in the regeneration tower 10 is sucked into the first heat exchanger 300 by 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, the regeneration gas after heat exchange enters the condensate tank 40 to supplement water to the regeneration tower 10 in the same way as above, about 18kg / h carbon dioxide is separated out; the lean liquid supplemented from the tower kettle to the gas-liquid separator 520 by the second pump body 522 is flashed in the gas-liquid separator 520 by the first compressor 531 to flash a small part of the steam and reduce the temperature to 90℃, 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 is heated and steam is generated, and the lean liquid returns to the gas-liquid separator 520, about 27kg / h, 90℃ saturated steam is also flashed into the first compressor 531, the first compressor 531 pressurizes and heats the steam to the saturated temperature 100℃ and discharges it into the tower kettle for regeneration, wherein the first pump body 513, the first compressor 531 and the second compressor 201 have fixed frequencies, and the eleventh valve 551 is adjusted to control the discharge of about 0.5m³ / h lean liquid from the regeneration system 50, taking the tower kettle liquid level as the target value.

[0103] 4) In the mode of direct steam regeneration of the kettle, 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 kettle is heated by electricity, and steam and circulating lean liquid are introduced into the second heat exchanger 301 to preheat the kettle lean liquid to 100 DEG C. The regeneration gas reaches the top of the tower and is sucked into the delivery of the second compressor 201 at about 49 m3 / h. The 100 DEG C mixed regeneration gas (containing 27 kg / h water vapor) reaches the second heat exchanger 301. After heat exchange, the regeneration gas enters the condensate tank 40. About 18 kg / h of carbon dioxide gas is separated and rises, and about 27 kg / h of condensed water falls. The liquid level of the condensate tank 40 is set as the target value, the frequency of the third pump body 542 is controlled, and the water flow rate of the condensate tank 40 is controlled. The water enters the eighth valve 543, is throttled and pressure-reduced to 90 DEG C, and then enters the second heat exchanger 301. After heat exchange, the regeneration gas is evaporated and enters the first compressor 531 to be pressure-increased and temperature-increased to the saturated temperature 100 DEG C, and then is directly discharged into the kettle for regeneration. The first compressor 531 and the second compressor 201 are fixed in frequency, and the inlet temperature of the second heat exchanger 301 is set as the target value to adjust the opening of the eighth valve 543 and the third pump body 542 to control the water flow rate of the condensate tank 40 to be about 27 kg / h.

[0104] The alcohol amine absorption method carbon dioxide capture and regeneration device provided by the embodiment of the utility model, the regeneration gas is heat-exchanged with the regeneration system 50 after being compressed and the enthalpy is increased, and the heat of the regeneration gas is recovered to the regeneration tower 10 for reuse through the regeneration system 50, so that the latent heat energy in the regeneration gas can be fully recovered and reused, the heat efficiency is improved, the system energy consumption is reduced, and energy is saved. In addition, the regeneration gas does not need to be cooled and condensed by using a chemical refrigerant, and the pollution of the leakage of the working medium to the environment is fundamentally eliminated.

[0105] Finally, it should be noted that: the above embodiments are only used to illustrate the technical solutions of the utility model, and not to limit them; although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that: it can still modify the technical solutions recorded in the foregoing embodiments, or make equivalent replacement to part of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the utility model.

Claims

1. An alcohol amine absorption process carbon dioxide capture regeneration apparatus, characterized by, The application relates to a heat recovery system for a regenerative tower, which comprises a regenerative tower, a compression enthalpy-increasing module, a heat exchange module, a condensate tank and a regenerative system. The top of the regenerative tower is provided with a regenerative gas outlet; the inlet of the compression enthalpy-increasing module is connected with the regenerative gas outlet, and the compression enthalpy-increasing module is used for increasing the enthalpy of the regenerative gas. The heat exchange module is provided with a first side and a second side; the inlet of the first side is connected with the outlet of the compression enthalpy-increasing module; the outlet of the first side is connected with the condensate tank; and the condensate outlet of the condensate tank is connected to the regenerative tower. The regenerative tower is connected with the second side of the heat exchange module through the regenerative system, and the regenerative system is used for recovering the waste heat in the regenerative gas to the regenerative tower through heat exchange. The regenerative system comprises a first subsystem, and the first subsystem comprises a first loop.

2. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 1, characterized by, The inlet of the first loop is connected with the tower kettle of the regenerative tower, and the outlet is connected back to the tower kettle of the regenerative tower through the second side; and a pump body is arranged on the first loop. The regenerative system comprises a second subsystem, and the second subsystem comprises a gas-liquid separator, a second loop and a regenerative loop.

3. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 1, characterized by, The liquid inlet of the gas-liquid separator is connected with the tower kettle of the regenerative tower through a pump body; the inlet of the second loop is connected with 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 arranged on the second loop; the steam outlet of the gas-liquid separator is connected to the tower kettle of the regenerative tower through the regenerative loop, and a first compressor is arranged on the regenerative loop. The regenerative system comprises a third subsystem, and the third subsystem comprises a third loop and a regenerative loop.

4. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 1, characterized by, The inlet of the third loop is connected with the condensate outlet of the condensate tank, and the outlet is connected with the regenerative loop through the second side; the regenerative loop is connected to the tower kettle of the regenerative tower; a pump body is arranged on the third loop, and a first compressor is arranged on the regenerative loop. The regenerative system comprises:

5. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 1, characterized by, A first subsystem comprising a first loop, wherein the inlet of the first loop is connected with the tower kettle of the regenerative tower, and the outlet is connected back to the tower kettle of the regenerative tower through the second side; A second subsystem comprising a gas-liquid separator, a second loop and a regenerative loop, wherein the liquid inlet of the gas-liquid separator is connected with the tower kettle; the inlet of the second loop is connected with the liquid outlet of the gas-liquid separator, and the outlet is connected back to the gas-liquid separator through the second side; and the steam outlet of the gas-liquid separator is connected to the tower kettle through the regenerative loop, and a first compressor is arranged on the regenerative loop; A third subsystem comprising a third loop and the regenerative loop, wherein the inlet of the third loop is connected with the condensate outlet of the condensate tank, and the outlet is connected to the regenerative loop through the second side. The first loop comprises:

6. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 5, characterized by, A first passage, wherein the inlet is connected with the tower kettle, and the outlet is connected with the inlet of the second side; a first valve and a first pump body are arranged on the first passage; A second passage, wherein the inlet is connected with the outlet of the second side, and the outlet is connected to the tower kettle; a second valve is arranged on the second passage. ​ 7. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 6, characterized by, The third valve and the second pump body are arranged between the liquid inlet of the gas-liquid separator and the tower kettle; the fourth valve is arranged at the steam outlet of the gas-liquid separator, the fifth valve is arranged on the regeneration circuit; the second circuit comprises: The first passage and the second passage; The third passage is connected with the liquid outlet of the gas-liquid separator at the inlet and connected with the first passage at the outlet, and the sixth valve is arranged on the third passage; The fourth passage is connected with the second passage at the inlet and connected with the middle part of the gas-liquid separator at the outlet, and the seventh valve is arranged on the fourth passage.

8. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 7, characterized by, The third circuit comprises: The fifth passage is connected with the condensate outlet of the condensate tank at the inlet and connected with the inlet of the second side through the third pump body at the outlet; the eighth valve is arranged at the outlet of the fifth passage; The sixth passage is connected with the outlet of the second side at the inlet and connected with the regeneration circuit at the outlet, and the ninth valve is arranged on the fifth passage.

9. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 8, characterized by, The heat exchange module comprises 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 connected to the inlet of the first side of the second heat exchanger through a second branch; the tenth valve is arranged on the first branch, and the eleventh valve is arranged on the second branch; The first passage is connected with the inlet of the second side of the first heat exchanger; the second passage is connected with the outlet of the second side of the first heat exchanger; The inlet of the fifth passage is connected with the inlet of the second side of the second heat exchanger, and the sixth passage is connected with the outlet of the second side of the second heat exchanger.

10. The alcohol amine absorption process carbon dioxide capture regeneration device according to claim 1, characterized by, The compression enthalpy-increasing module comprises a regeneration gas pipeline and a second compressor; the inlet of the regeneration gas pipeline is connected with the regeneration gas outlet, and the outlet is connected to the inlet of the first side through the second compressor.

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