Carbon dioxide trapping and liquefying system

Abstract

The invention provides a carbon dioxide trapping and liquefying system. The carbon dioxide trapping and liquefying system comprises a first absorption tower, a second absorption tower, a first desorption tower, a second desorption tower, a first heat pump and a second heat pump. By adopting the scheme of absorption tower series grading absorption, desorption tower series grading desorption and heat pump system, the total energy consumption of the system is reduced, and the trapping efficiency is improved. Wherein the absorption towers are connected in series for graded absorption and the desorption towers are connected in series for graded desorption, so that the height and scale of the towers are reduced, and the regeneration energy consumption of the system can be reduced while the initial construction cost of the absorption towers is reduced. A multi-stage heat pump system is adopted to recover and utilize steam waste heat of a second desorption tower, heat of carbon dioxide at an outlet of a compressor and heat released in the liquefaction process to reduce energy consumption of a reboiler, the temperature of extracted gaseous carbon dioxide can also be reduced, energy consumption is reduced in the liquefaction process, the liquefaction proportion is effectively increased, and the energy consumption is reduced. The liquefied carbon dioxide production efficiency is improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of flue gas treatment technology, in particular to a carbon dioxide capture and liquefaction system. BACKGROUND

[0002] The existing traditional carbon dioxide capture process for large thermal power plants and chemical plants mainly uses amine solution as an absorbent to react with carbon dioxide in the flue gas in the absorption tower, and the rich liquid flows out from the bottom of the tower, and the rich liquid enters the lean-rich liquid heat exchanger to exchange heat with the lean liquid and then enters the desorption tower, and the secondary steam generated by the reboiler at the bottom of the desorption tower drives the rich liquid desorption to obtain high-concentration carbon dioxide and lean liquid, and the lean liquid exchanges heat through the square liquid heat exchanger and then enters the absorption tower again.

[0003] However, the carbon dioxide chemical absorption method carbon capture process is difficult to apply to small and medium-sized enterprises, and has the following disadvantages: 1. The system is mainly for thermal power plants and large chemical plants, and the carbon dioxide capture scale reaches tens of thousands of tons or even millions of tons per year, and the supporting equipment is large in size and high in fixed investment. Once established, it is difficult to be flexible and applied to other occasions. However, due to the fluctuation of production capacity and seasonal supply and demand fluctuation of small and medium-sized enterprises, they cannot afford high-cost carbon capture equipment and prefer small and flexible or even rental form commercial service equipment.

[0004] 2. The operation cost is high, the solution regeneration temperature in the desorption tower needs to be maintained at 100-120 DEG C, and a large amount of steam or electric energy needs to be consumed by the reboiler, resulting in high overall energy consumption; the waste heat of the regenerated gas at the top of the desorption tower is not fully utilized, resulting in waste. SUMMARY

[0005] Therefore, the purpose of the present application is to provide a carbon dioxide capture and liquefaction system to solve the above problems.

[0006] The present application adopts the following scheme: The present application provides a carbon dioxide capture and liquefaction system, comprising a first absorption tower, a second absorption tower, a first desorption tower, a second desorption tower, a first heat pump and a second heat pump; wherein: The first absorption tower and the second absorption tower are used to absorb CO2 in the desulfurized flue gas by lean liquid absorbent to form rich liquid; The rich liquid inlet of the first desorption tower is connected with the bottom outlet of the absorption tower through a rich liquid pump; the lean liquid vapor from the reboiler enters the lean liquid inlet of the first desorption tower and then exits from the lean liquid outlet to enter the lean liquid distributor; and the remaining rich liquid flows out from the rich liquid outlet; The upper inlet of the second stripping column is connected to the rich liquid outlet of the first stripping column; the lean liquid vapor from the reboiler enters from the gas inlet at the lower part of the second stripping column; the bottom outlet of the second stripping column is connected to the reboiler; the lean liquid after being stripped by the second stripping column flows out from the liquid outlet at the bottom of the second stripping column, enters the lean liquid inlet of the first stripping column, and finally enters the lean liquid distributor; The first heat pump evaporator in the first heat pump is connected to the top gas outlet of the stripping column through the CO2 mixer; the heat generated by the first heat pump is transmitted to the reboiler; The carbon dioxide vapor cooled by the first heat pump evaporator enters the first liquefaction separator and the first liquefaction compressor, then enters the second heat pump first evaporator in the second heat pump, and then enters the second heat pump second evaporator in the second heat pump through the second liquefaction compressor; the heat generated by the second heat pump is transmitted to the reboiler; The carbon dioxide vapor cooled by the second heat pump second evaporator enters the second liquefaction separator, and then the separated gas enters the liquefaction system for liquefaction and storage.

[0007] Further, the liquefaction system comprises a third heat pump; the heat generated by the third heat pump is transmitted to the reboiler.

[0008] Further, the liquefaction system comprises a first liquefaction heat exchanger, a liquefaction mixer, a third liquefaction compressor, a first liquefaction cooler, a fourth liquefaction compressor, a third heat pump system, a second liquefaction heat exchanger, a first liquefaction throttle valve, and a third liquefaction separator connected in a circulation manner; The coolant is compressed by the third liquefaction compressor, cooled by the first liquefaction cooler, compressed by the fourth liquefaction compressor, cooled by the third heat pump evaporator of the third heat pump after compression, exchanged heat in the second liquefaction heat exchanger, enters the third liquefaction separator through the first liquefaction throttle valve, and the liquid part enters the first liquefaction heat exchanger after heat exchange, and then enters the liquefaction mixer; the gas part and the liquid part enter the second liquefaction heat exchanger after heat exchange, and then enter the liquefaction mixer for mixing, and then enter the third liquefaction compressor to complete the circulation.

[0009] Further, the first heat pump comprises the first heat pump evaporator, a first heat pump compressor, a first heat pump cooler, and a first heat pump throttle valve connected in a circulation manner; the heat released by the first heat pump cooler is provided to the reboiler.

[0010] Further, the second heat pump comprises the second heat pump first evaporator, a second heat pump second evaporator, a second heat pump compressor, a second heat pump cooler, and a second heat pump throttle valve connected in a circulation manner; the heat released by the second heat pump cooler is provided to the reboiler.

[0011] Further, the third heat pump comprises the third heat pump evaporator, the third heat pump compressor, the third heat pump cooler and the third heat pump throttling valve connected in a circulation; the heat released by the third heat pump cooler is provided to the reboiler.

[0012] Further, the first stripping tower is provided with a heating coil, the lean liquid inlet is arranged at the lower part of the first stripping tower, and the lean liquid outlet is arranged at the upper part of the first stripping tower.

[0013] Further, the second stripping tower is provided with a filler layer.

[0014] Further, the system further comprises a lean liquid replenisher connected to the lean liquid outlet, and the lean liquid replenisher is connected to the lean liquid distributor through a lean liquid cooling connection.

[0015] Further, the system is integrated on an integral base in a pry mode.

[0016] By adopting the technical scheme, the following technical effects can be achieved. The application adopts the scheme of absorption tower cascade absorption + stripping tower cascade stripping + heat pump system, reduces the total energy consumption of the system, and improves the capture efficiency. The absorption tower cascade absorption and the stripping tower cascade stripping are adopted to reduce the tower height and scale, reduce the initial construction cost of the absorption tower, and also reduce the regeneration energy consumption of the system. The multistage heat pump system is adopted to recover and utilize the heat of the vapor waste heat of the second stripping tower, the heat of the carbon dioxide at the outlet of the compressor, and the heat released in the liquefaction process, reduce the energy consumption of the reboiler, reduce the temperature of the gaseous carbon dioxide, reduce the energy consumption in the liquefaction process, effectively improve the liquefaction ratio, and increase the liquefaction carbon dioxide production efficiency. BRIEF DESCRIPTION OF DRAWINGS

[0017] In order to more clearly illustrate the technical scheme of the embodiments of the application, the following will briefly introduce the drawings needed to be used in the embodiments. It should be understood that the following drawings only show some embodiments of the application, and therefore should not be regarded as a limitation to the scope. Other related drawings can also be obtained by those skilled in the art without any creative effort.

[0018] Fig. 1 is a structure schematic diagram of a carbon dioxide capture and liquefaction system according to an embodiment of the application; Fig. 2 is a structure schematic diagram of a first stripping tower of a carbon dioxide capture and liquefaction system according to an embodiment of the application; Fig. 3 is a structure schematic diagram of a second stripping tower of a carbon dioxide capture and liquefaction system according to an embodiment of the application; Icon: first absorption column 1, inter-column cooler 2, second absorption column 3, rich liquid mixer 4, rich liquid pump 5, first stripping column 6, second stripping column 7, CO2 mixer 8, first heat pump evaporator 9, first heat pump compressor 10, first heat pump cooler 11, first heat pump throttle valve 12, reboiler 13, lean liquid replenisher 14, lean liquid cooler 15, lean liquid distributor 16, first liquefaction separator 17, first liquefaction compressor 18, second heat pump first evaporator 19, second liquefaction compressor 20, second heat pump second evaporator 21, second heat pump compressor 22, second heat pump cooler 23, second heat pump throttle valve 24, second liquefaction separator 25, first liquefaction heat exchanger 26, third liquefaction compressor 27, first liquefaction cooler 28, fourth liquefaction compressor 29, third heat pump evaporator 30, second liquefaction heat exchanger 31, first liquefaction throttle valve 32, third liquefaction separator 33, liquefaction mixer 34, third heat pump compressor 35, third heat pump cooler 36, third heat pump throttle valve 37, first heat pump 38, second heat pump 39, third heat pump 40, Rich liquid inlet 601, rich liquid outlet 602, first gas outlet 603, lean liquid inlet 604, lean liquid outlet 605, heating coil 606, rich liquid inlet 701, second gas outlet 702, liquid outlet 703, packing layer 704. DETAILED DESCRIPTION

[0019] In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative work fall within the protection scope of the present application. Therefore, the following detailed description of the embodiments of the present application provided in the drawings is not intended to limit the scope of the claimed present application, but only represents selected embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative work fall within the protection scope of the present application.

[0020] EMBODIMENT In combination Figs. 1 to 3 As shown in the drawings, the embodiment provides a carbon dioxide capture liquefaction system. Specifically, comprising a first absorption column 1, a second absorption column 3, a first stripping column 6, a second stripping column 7, a first heat pump, a second heat pump; wherein: The lower inlet of the first absorption tower 1 is connected with the desulfurized flue gas source, and the upper inlet of the first absorption tower 1 is connected with the lean liquid distributor 16; so that the desulfurized flue gas is in countercurrent contact with the lean liquid absorbent sprayed from top to bottom to generate chemical reaction, and most of the CO2 in the flue gas is absorbed; the remaining flue gas flows out from the top of the first absorption tower 1 and is sent into the inter-tower cooler 2 to cool the flue gas, and then enters the second absorption tower 3 from the lower inlet of the second absorption tower 3 to perform secondary absorption; and after the CO2 in the desulfurized flue gas in the first absorption tower 1 is absorbed, the lean liquid becomes rich liquid, which flows out from the bottom outlet of the first absorption tower 1, enters the rich liquid mixer 4, and is sent into the first stripping tower 6 through the rich liquid pump 5.

[0021] Similarly, the upper inlet of the second absorption tower 3 is connected with the lean liquid distributor 16; so that the desulfurized flue gas is in countercurrent contact with the lean liquid absorbent sprayed from top to bottom to generate chemical reaction, and performs secondary absorption. After the CO2 in the desulfurized flue gas in the second absorption tower 3 is absorbed, the lean liquid becomes rich liquid, which flows out from the bottom outlet of the second absorption tower 3, enters the rich liquid mixer 4, and is sent into the first stripping tower 6 through the rich liquid pump 5.

[0022] The rich liquid produced by absorbing CO2 in the absorption tower is sent to the first desorption tower by the rich liquid pump 5, the cold rich liquid enters the first desorption tower from the rich liquid inlet 601, is heated and stripped by the heating coil 606 arranged on the first stripping tower 6, the hot lean liquid, i.e. the lean liquid vapor from the reboiler 13, enters the heating coil 606 to heat the first desorption tower, and then exits from the first lean liquid outlet 605, the CO2 gas produced after the rich liquid is stripped exits from the first gas outlet 603, and the liquid exits from the rich liquid outlet 602, enters the second stripping tower 7 through the rich liquid inlet 601 at the top of the second desorption tower, and then is further stripped in the second stripping tower 7. Similarly, the vapor from the reboiler 13 enters the second stripping tower 7 from the lower gas inlet, so that the rich liquid in countercurrent contact with the vapor from top to bottom, the CO2 in the rich liquid is separated from the absorbent, the CO2 with steam flows out from the second gas outlet 702 at the top of the tower, the rich liquid becomes lean liquid after the CO2 is separated from the absorbent, and flows out from the liquid outlet 703 at the bottom of the second desorption tower, and can enter the lean liquid inlet 604 of the first stripping tower 6, and finally exits from the lean liquid outlet 605 to enter the lean liquid replenisher 14, and is sent to the lean liquid distributor 16 through the lean liquid cooler 15 to form a lean liquid circulation.

[0023] The CO2-containing steam after being resolved by the first and second desorption towers enters a CO2 mixer 8, is mixed, and then enters a first heat pump evaporator 9 of a first heat pump 38 to transfer steam heat to a refrigeration working medium to recover tower top waste heat, so as to preheat the first heat pump 38. The refrigeration working medium is then changed into high-temperature and high-pressure high-quality heat by a first heat pump compressor 10, enters a first heat pump cooler 11 to release heat, and provides part of the required energy of the reboiler 13. The refrigeration working medium after being cooled by the first heat pump cooler 11 enters a first heat pump throttling valve 12, is depressurized, and enters the first heat pump evaporator 9 to complete a heat exchange cycle. The steam of the CO2 mixer 8 after being cooled by the first heat pump evaporator 9 is subjected to primary gas-liquid separation in a first liquefaction separator 17, and the separated gas enters a first liquefaction compressor 18 for pressurization.

[0024] The pressurized gas enters a second heat pump first evaporator 19 of a second heat pump 39, the cooled gas enters a second liquefaction compressor 20 for pressurization, and the pressurized gas enters a second heat pump second evaporator 21 of the second heat pump to transfer pressurization heat to the refrigeration working medium to recover waste heat generated after pressurization of the second liquefaction compressor 20, so as to preheat the second heat pump 39. The refrigeration working medium is then changed into high-temperature and high-pressure high-quality heat by a second heat pump compressor 22, enters a second heat pump cooler 23 to release heat, and provides part of the required energy of the reboiler 13. The refrigeration working medium after being cooled by the second heat pump cooler 23 enters a second heat pump throttling valve 24, is depressurized, and enters the second heat pump first evaporator 19 to complete a heat exchange cycle. The pressurized gas of the second liquefaction compressor 20 after being cooled by the second heat pump second evaporator 21 is subjected to secondary gas-liquid separation in a second liquefaction separator 25, and the separated gas enters a first liquefaction heat exchanger 26 for liquefaction and storage.

[0025] The coolant of the liquefaction system is compressed by a third liquefaction compressor 27, is cooled by a first liquefaction cooler 28 after compression, is compressed by a fourth liquefaction compressor 29, and is cooled by a third heat pump evaporator 30 of a third heat pump 40 after compression to recover heat released during CO2 liquefaction, so as to preheat the third heat pump 40. The coolant heat is transferred to the refrigeration working medium, the refrigeration working medium is changed into high-temperature and high-pressure high-quality heat by a third heat pump compressor 35, enters a third heat pump cooler 36 to release heat, and provides part of the required energy of the reboiler 13. The refrigeration working medium after being cooled by the third heat pump cooler 36 enters a third heat pump throttling valve 37, is depressurized, and enters the third heat pump evaporator 30 to complete a heat exchange cycle.

[0026] The pressurized vapor of the fourth liquefaction compressor 29 enters the third heat pump evaporator 30 and is cooled, enters the second liquefaction heat exchanger 31 for heat exchange, enters the third liquefaction separator 33 through the first liquefaction throttle valve 32, the liquid part enters the first liquefaction heat exchanger 26 for heat exchange, and then enters the liquefaction mixer 34; the gas part and the liquid part enter the second liquefaction heat exchanger 31 for heat exchange, then enter the liquefaction mixer 34 for mixing, and then enter the third liquefaction compressor 27 to complete the cycle.

[0027] The application adopts the scheme of absorption tower series grading absorption + analysis tower series grading analysis + heat pump system, reduces the total energy consumption of the system, and improves the capture efficiency. The absorption tower series grading absorption and the analysis tower series grading analysis are adopted to reduce the tower height and scale, reduce the initial construction cost of the absorption tower, and also reduce the regeneration energy consumption of the system. The multistage heat pump system is adopted to recover and utilize the heat of the vapor waste heat of the second analysis tower 7, the heat of the carbon dioxide at the outlet of the compressor, and the heat released in the liquefaction process, reduce the energy consumption of the reboiler 13, utilize the waste heat, reduce the temperature of the extracted gaseous carbon dioxide, reduce the energy consumption in the liquefaction process, effectively improve the liquefaction ratio, and increase the production efficiency of the liquefied carbon dioxide.

[0028] Further, in the embodiment, based on the integrated pry, the pry height is 2.3 m, the functions such as the absorption tower, the desorption tower, the compressor, and the heat exchanger are integrated on an overall base, the overall installation and movement are realized, the vehicle transportation is realized, the carbon dioxide is captured and recovered in different occasions, and a plurality of groups of devices can be connected and combined to work according to the demand of the captured flue gas.

[0029] The above is only the preferred embodiment of the application, and the protection scope of the application is not limited to the above-mentioned embodiments, and any technical scheme falling within the idea of the application belongs to the protection scope of the application.

[0030] In the description of the application, it should be understood that the terms "center", "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the application and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the application.

[0031] In addition, the terms "first", "second", etc. are used only for the purpose of description and do not imply or imply relative importance or imply the number of the technical features indicated. Therefore, the features defined as "first", "second" can explicitly or implicitly include one or more of the features. In the description of the present application, the meaning of "a plurality of" is two or more, unless otherwise explicitly specified and limited.

[0032] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting", "fixing" and the like should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the internal communication of two elements or the interaction relationship between two elements. For those skilled in the art, the specific meaning of the above-mentioned terms in the present application can be understood according to the specific circumstances.

[0033] In the present application, unless otherwise explicitly specified and limited, the first feature "on" or "under" the second feature can include that the first and second features are in direct contact, or that the first and second features are not in direct contact but are in contact through another feature between them. Moreover, the first feature "on", "above" and "above" the second feature includes that the first feature is directly above and obliquely above the second feature, or only indicates that the horizontal height of the first feature is higher than that of the second feature. The first feature "below", "below" and "below" the second feature includes that the first feature is directly below and obliquely below the second feature, or only indicates that the horizontal height of the first feature is less than that of the second feature.

Claims

1. A carbon dioxide capture and liquefaction system, comprising: The system comprises a first absorption tower (1), a second absorption tower (3), a first desorption tower (6), a second desorption tower (7), a first heat pump, and a second heat pump; wherein: the first absorption tower (1) and the second absorption tower (3) are used for absorbing CO2 in desulfurized flue gas by a lean liquid absorbent to form a rich liquid; The rich liquid inlet (601) of the first desorption tower (6) is connected with the bottom outlet of the absorption tower through a rich liquid pump (5); the lean liquid vapor from a reboiler (13) enters the lean liquid inlet (604) of the first desorption tower (6) and then exits from the lean liquid outlet (605) to enter the lean liquid distributor (16); the remaining rich liquid flows out from the rich liquid outlet (602); The upper inlet of the second desorption tower (7) is connected with the rich liquid outlet (602) of the first desorption tower (6); the lean liquid vapor from the reboiler (13) enters the gas inlet at the lower part of the second desorption tower (7); the bottom outlet of the second desorption tower (7) is connected with the reboiler (13); the lean liquid after desorption by the second desorption tower (7) flows out from the liquid outlet (703) at the bottom of the second desorption tower, enters the lean liquid inlet (604) of the first desorption tower (6), and finally enters the lean liquid distributor (16); The first heat pump evaporator (9) in the first heat pump 38 is connected with the top gas outlet of the desorption tower through a CO2 mixer (8); the heat generated by the first heat pump 38 is transmitted to the reboiler (13); the carbon dioxide vapor cooled by the first heat pump evaporator (9) enters the second heat pump first evaporator (19) in the second heat pump 39 through a first liquefaction separator (17) and a first liquefaction compressor (18), and then enters the second heat pump second evaporator (21) in the second heat pump through a second liquefaction compressor (20); the heat generated by the second heat pump 39 is transmitted to the reboiler (13); the carbon dioxide vapor cooled by the second heat pump second evaporator (21) enters a second liquefaction separator (25), and then the separated gas enters a liquefaction system for liquefaction and storage.

2. The carbon dioxide capture and liquefaction system of claim 1, wherein, The liquefaction system comprises a third heat pump 40; the heat generated by the third heat pump 40 is transmitted to the reboiler (13).

3. The carbon dioxide capture and liquefaction system of claim 2, wherein, The liquefaction system comprises a first liquefaction heat exchanger (26), a liquefaction mixer (34), a third liquefaction compressor (27), a first liquefaction cooler (28), a fourth liquefaction compressor (29), a third heat pump system, a second liquefaction heat exchanger (31), a first liquefaction throttle valve (32), and a third liquefaction separator (33) connected in a circulation manner. The coolant is cooled by the first liquefaction cooler (28) after being compressed by the third liquefaction compressor (27), compressed by the fourth liquefaction compressor (29), cooled by the third heat pump evaporator (30) of the third heat pump, exchanged heat in the second liquefaction heat exchanger (31), enters the third liquefaction separator (33) through the first liquefaction throttle valve (32), and the liquid part enters the first liquefaction heat exchanger (26) after heat exchange, and enters the liquefaction mixer (34); The gas part liquid part enters the second liquefaction heat exchanger (31) after heat exchange, enters the liquefaction mixer (34) for mixing, and then enters the third liquefaction compressor (27) to complete the cycle.

4. The carbon dioxide capture and liquefaction system of claim 1, wherein, The first heat pump comprises the first heat pump evaporator (9), the first heat pump compressor (10), the first heat pump cooler (11) and the first heat pump throttle valve (12) connected in a cycle; the heat released by the first heat pump cooler (11) is provided to the reboiler (13).

5. The carbon dioxide capture and liquefaction system of claim 1, wherein, The second heat pump comprises the second heat pump first evaporator (19), the second heat pump second evaporator (21), the second heat pump compressor (22), the second heat pump cooler (23) and the second heat pump throttle valve (24) connected in a cycle; the heat released by the second heat pump cooler (23) is provided to the reboiler (13).

6. The carbon dioxide capture and liquefaction system of claim 2, wherein, The third heat pump comprises the third heat pump evaporator (30), the third heat pump compressor (35), the third heat pump cooler (36) and the third heat pump throttle valve (37) connected in a cycle; the heat released by the third heat pump cooler (36) is provided to the reboiler (13).

7. The carbon dioxide capture and liquefaction system of any one of claims 1-6, wherein, The first stripping column (6) is provided with a heating coil (606) on the upper disc, the lean liquid inlet (604) is arranged at the lower part of the first stripping column (6), and the lean liquid outlet (605) is arranged at the upper part of the first stripping column (6).

8. The carbon dioxide capture and liquefaction system of any one of claims 1-6, wherein, The second stripping column (7) is provided with a filler layer (704).

9. The carbon dioxide capture and liquefaction system of any one of claims 1-6, wherein, The system further comprises a lean liquid supplement device (14) connected to the lean liquid outlet (605), and the lean liquid supplement device (14) is connected to the lean liquid distributor (16) through a lean liquid cooling device.

10. The carbon dioxide capture and liquefaction system of any one of claims 1-6, wherein, The system is integrated on an overall base in a pry mode.

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