A multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture

Abstract

The present invention relates to the technical field of carbon dioxide emission reduction, and discloses a multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture, which comprises an absorption tower. The absorption tower is provided with a plurality of inlets, a packing layer and a redistributor from top to bottom. The inlets are, from top to bottom, the fourth inlet, the third inlet, the second inlet and the first inlet; a phase separation tank, the bottom of the phase separation tank is communicated with the bottom of the absorption tower through a pipeline, and the top of the phase separation tank is communicated with the third inlet and the first inlet through a pipeline; a heat exchanger, the heat exchanger is communicated with the bottom of the phase separation tank through a rich liquid pump, and the heat exchanger is communicated with the fourth inlet and the second inlet through a pipeline; a desorption tower, the desorption tower is connected with a reboiler, and the desorption tower is connected with the heat exchanger through a pipeline. A multi-stage shunt process is adopted to replace the inter-stage cooling process, and by adjusting the shunt ratio, the temperature is evenly distributed throughout the absorption tower, avoiding the occurrence of local hot spots.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon dioxide emission reduction, and more specifically, particularly relates to a multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture. Background Art

[0002] With the rapid development of industry and the use of a large amount of fossil fuels, the content of greenhouse gases such as carbon dioxide in the atmosphere is increasing continuously, and problems such as global warming and glacier melting are intensifying. Among them, carbon dioxide is considered to be one of the main culprits of climate change. To mitigate the negative impacts brought about by climate change, carbon capture, utilization and storage (CCUS) is considered a technology with industrial application potential. Among various CCUS technologies, the organic amine absorption method in chemical absorption method is widely used because of its strong selectivity and wide application range, and has now become one of the mainstream technologies for post-combustion carbon dioxide capture.

[0003] However, the traditional organic amine absorption method has the problem of high regeneration energy consumption. To further reduce the regeneration energy consumption, the phase change absorption method came into being, reducing the energy consumption from 4 GJ / tCO 2 to about 2.4 GJ / tCO 2 However, while the phase change absorption method reduces the energy consumption, it brings the problem of heat release. The process of the organic amine solution in the absorption tower absorbing CO 2 is an exothermic reaction, and the heat generated by the reaction is transferred to the absorption liquid, resulting in an increase in the temperature of the absorption liquid. The increase in the temperature of the absorption liquid limits the driving force of the absorption process and reduces the CO 2 loading capacity of the absorption liquid, and at the same time will also exacerbate the degradation of the organic amine.

[0004] The problem of serious heat release during the absorption process of the phase change absorption method has become an urgent problem to be solved in industry. Maintaining the solution in the absorption tower at a suitable temperature while maintaining the capture rate is an important key to promoting the development of this technology. Summary of the Invention

[0005] The purpose of the present invention is to provide a multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture to solve the problems existing in the prior art. By adopting a multi-stage shunt process instead of an inter-stage cooling process and adjusting the shunt ratio, the temperature distribution in the entire absorption tower is made uniform, and local hot spots are avoided.

[0006] To achieve the above object, the present invention provides the following solution: The present invention provides a multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture, including: an absorption tower, in which several inlets, a packing layer and redistributors are distributed from top to bottom. The inlets are, from top to bottom, the fourth inlet, the third inlet, the second inlet and the first inlet. The packing layer is, from top to bottom, the I-section packing layer, the II-section packing layer, the III-section packing layer and the IV-section packing layer. The redistributors are, from top to bottom, the first redistributor, the second redistributor and the third redistributor; a phase separation tank, the bottom of which is connected to the bottom of the absorption tower through a pipeline, and the top of which is connected to the third inlet and the first inlet through a pipeline; a heat exchanger, which is connected to the bottom of the phase separation tank through a rich liquid pump, and is connected to the fourth inlet and the second inlet through a pipeline; a desorption tower, which is connected with a reboiler and is connected to the heat exchanger through a pipeline.

[0007] According to the multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, the upper layer in the phase separation tank is the light phase, and the lower layer is the rich phase. The rich phase is connected to the bottom of the absorption tower through a pipeline, the light phase is connected to the third inlet and the first inlet through a pipeline, and the light phase is connected with a light phase pump. The light phase enters the third inlet and the first inlet through the light phase pump and a pipeline.

[0008] According to the multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, the fourth inlet is located between the top of the absorption tower and the I-section packing layer, the third inlet is located between the I-section packing layer and the II-section packing layer, the second inlet is located between the II-section packing layer and the III-section packing layer, and the first inlet is located between the III-section packing layer and the IV-section packing layer.

[0009] According to the multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, the first redistributor is located below the I-section packing layer, the second redistributor is located below the II-section packing layer, and the third redistributor is located below the III-section packing layer.

[0010] According to the multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, the rich phase is connected to the heat exchanger through a rich liquid pump.

[0011] A multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, wherein the heat exchanger is connected to the top of the desorption tower through a pipeline, the heat exchanger is connected to the bottom of the desorption tower through a lean liquid pump, the rich phase is pumped to the desorption tower for desorption through the lean liquid pump, and the absorbed liquid after desorption becomes lean liquid, and the lean liquid enters the absorption tower through the pipeline via the fourth inlet and the second inlet.

[0012] A multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, wherein the proportion range of the lean liquid entering the fourth inlet is 60%-80%, and the proportion range of the lean liquid entering the second inlet is 20%-40%.

[0013] A multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, wherein the proportion range of the light phase entering the third inlet is 80%-90%, and the proportion range of the light phase entering the first inlet is 20%-10%.

[0014] A multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, wherein the height range of the I-section packing layer is 0.5-2.5 m, the height range of the II-section packing layer is 1.5-3 m, the height range of the III-section packing layer is 0.5-2 m, and the height range of the IV-section packing layer is 1.5-3 m.

[0015] A multi-stage isothermal phase change absorption tower for high-concentration carbon dioxide capture provided by the present invention, wherein the aspect ratio range of the absorption tower is 10-50.

[0016] The present invention discloses the following technical effects:

[0017] Open holes at specific positions between the packing layers, adopt a multi-stage splitting process instead of an inter-stage cooling process, and adjust the splitting ratio to achieve uniform temperature distribution throughout the absorption tower, avoid the occurrence of local hot spots, improve the absorption performance on the one hand, and reduce the degradation of the absorbent and the loss of organic amine on the other hand. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings required for use in the embodiments. Obviously, the drawings in the following description are only some embodiments of the present invention, and those of ordinary skill in the art can also obtain other drawings based on these drawings without creative efforts.

[0019] Figure 1 It is a schematic diagram of the overall structure of the present invention;

[0020] Among them, 1. Absorption tower; 101. First inlet; 102. Second inlet; 103. Third inlet; 104. Fourth inlet; 105. Section I packing layer; 106. Section II packing layer; 107. Section III packing layer; 108. Section IV packing layer; 109. First redistributor; 110. Second redistributor; 111. Third redistributor; 2. Phase separation tank; 201. Light phase; 202. Rich phase; 3. Rich liquid pump; 4. Heat exchanger; 5. Lean liquid pump; 6. Reboiler; 7. Desorption tower; 8. Light phase pump. Detailed implementation manners

[0021] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.

[0022] To make the above objects, features, and advantages of the present invention more obvious and understandable, the present invention will be further described in detail below in conjunction with the accompanying drawings and specific implementation manners.

[0023] In the existing technology, there is a problem that the heat released during the process of the absorbent absorbing carbon dioxide is not properly handled. For example, the patent with the publication number CN116036803A discloses an absorption tower for flue gas carbon dioxide capture. The absorption tower includes a tower bottom recirculation section, an absorption section, and a water washing section arranged in sequence along the flue gas flow direction. The tower bottom recirculation section includes a liquid distributor, a variable-diameter packing layer, an absorption tower bottom, a liquid splitter, and a semi-rich liquid cooler; the absorption liquid in the absorption section enters the liquid distributor and the variable-diameter packing layer in sequence, enters the right side of the absorption tower bottom, and transports the semi-rich liquid in the absorption liquid to the semi-rich liquid cooler for cooling, and then returns to the liquid distributor; although this invention replaces the inter-stage cooling process with the tower bottom recirculation process, it reduces the storage tank equipment, but introduces a semi-rich liquid cooler, increasing additional costs.

[0024] The patent with the publication number CN118236819A discloses a gas-liquid redistribution device, an absorption tower, and a method for an absorption tower. The gas-liquid redistribution device for the absorption tower includes a distribution plate and at least one distribution mixer; the outer side wall of the distribution plate can be closely attached to the inner side wall of the absorption tower; at least one ventilation hole is provided on the distribution plate; the distribution mixer is arranged above the ventilation hole and covers the ventilation hole; the distribution mixer includes multiple groups of symmetrically cross-arranged inclined plates; multiple openings are provided on the inclined plates for dividing the flue gas passing through the distribution plate. Although this absorption tower improves the capture efficiency of harmful gases in the flue gas, it does not consider that while increasing the capture rate, it will also increase the heat release of the absorbent.

[0025] The patent with the publication number CN113648805A discloses a dual-zone double-circulation flue gas carbon dioxide absorption tower, which includes an absorption tower main body, a lower absorption packing layer, an upper absorption packing layer, a lower spray device, an upper spray device, an absorption tower demister, a first tower bottom, a second tower bottom, and an absorbent preparation tank; the absorption tower main body is divided into an upper absorption tower and a lower absorption tower; a lower absorption packing layer is provided in the lower absorption tower, and a lower spray device is provided above the lower absorption packing layer; an upper absorption packing layer is provided in the upper absorption tower, and an upper spray device is provided above the upper absorption packing layer. By increasing the liquid-gas ratio of the lower absorption tower, the height of the absorption tower can be reduced on the premise of ensuring the carbon dioxide capture rate of the lower layer. By increasing the absorbent concentration of the upper absorption tower and increasing the absorption reaction intensity, the height of the absorption tower can be effectively reduced on the premise of ensuring the carbon dioxide capture rate of the upper layer. Finally, while achieving a relatively high carbon dioxide capture rate of the whole tower, the height of the absorption tower can be effectively reduced. However, when improving the capture rate, the harm caused by the increase in absorbent temperature is not considered.

[0026] Regarding the problem that the absorbent releases heat during carbon dioxide absorption, this device adopts a multi-stage shunt process instead of an inter-stage cooling process, and by adjusting the shunt ratio, a uniform temperature distribution throughout the absorption tower is achieved. The specific content is as follows:

[0027] As Figure 1 shown, the present invention provides a multi-stage temperature-uniform phase-change absorption tower for high-concentration carbon dioxide capture, including: an absorption tower 1, where several inlets, packing layers, and redistributors are distributed from top to bottom in the absorption tower 1. The inlets are, from top to bottom, the fourth inlet 104, the third inlet 103, the second inlet 102, and the first inlet 101. The packing layers are, from top to bottom, the I-section packing layer 105, the II-section packing layer 106, the III-section packing layer 107, and the IV-section packing layer 108. The redistributors are, from top to bottom, the first redistributor 109, the second redistributor 110, and the third redistributor 111; a phase separation tank 2, the bottom of the phase separation tank 2 is connected to the bottom of the absorption tower 1 through a pipeline, and the top of the phase separation tank 2 is connected to the third inlet 103 and the first inlet 101 through a pipeline; a heat exchanger 4, the heat exchanger 4 is connected to the bottom of the phase separation tank 2 through a rich liquid pump 3, and the heat exchanger 4 is connected to the fourth inlet 104 and the second inlet 102 through a pipeline; a desorption tower 7, the desorption tower 7 is connected with a reboiler 6, and the desorption tower 7 is connected to the heat exchanger 4 through a pipeline.

[0028] The absorption tower 1 is provided with a fourth inlet 104, a third inlet 103, a second inlet 102, and a first inlet 101 from top to bottom. A certain proportion of lean liquid and light phase 201 are controlled to enter the tower. The packing layer is used to promote the contact between the flue gas and the absorbent and improve CO 2Absorption efficiency. The redistributor is used to evenly distribute the liquid, ensuring the uniform distribution of the absorbent in the packing layer, avoiding the generation of local hot spots. At specific positions between the packing layers, openings are made, and a multi-stage shunt process is adopted instead of the inter-stage cooling process. By adjusting the shunt ratio, the temperature distribution throughout the absorption tower 1 is made uniform, avoiding the emergence of local hot spots. On the one hand, it can improve the absorption performance, and on the other hand, it can reduce the degradation of the absorbent and reduce the loss of organic amines.

[0029] The flue gas enters the absorption tower 1 from the bottom, and the high-concentration CO 2 has a concentration range between 20% - 40%, and the gas velocity range is 0.2 m / s - 3 m / s. The absorbent selected for phase change capture is a liquid-liquid phase change absorbent, and the absorbent is located in the absorption tower 1.

[0030] The fourth inlet 104 is located between the I-section packing layer 105 and the tower top, and is used to introduce lean liquid, with a proportion range of 60% - 80%. The third inlet 103 is located between the I-section packing layer 105 and the II-section packing layer 106, and is used to introduce the light phase 201, with a proportion range of 80% - 90%. The second inlet 102 is located between the II-section packing layer 106 and the III-section packing layer 107, and is used to introduce lean liquid, with a proportion range of 20% - 40%. The first inlet 101 is located between the III-section packing layer 107 and the IV-section packing layer 108, and is used to introduce the light phase 201, with a proportion range of 20% - 10%.

[0031] The height range of the I-section packing layer 105 is 0.5 - 2.5 m, the height range of the II-section packing layer 106 is 1.5 - 3 m, the height range of the III-section packing layer 107 is 0.5 - 2 m, and the height range of the IV-section packing layer 108 is 1.5 - 3 m. The height ranges of each section of the packing layer are different, which is used to promote the contact between the flue gas and the absorbent and improve the CO2 absorption efficiency. The height-diameter ratio of the absorption tower 1 ranges from 10 - 50.

[0032] The following table shows the comparison of different packing layer height data and the comparison of the tower internal temperature after introducing different proportions of lean liquid and light phase in this embodiment. According to the data in the table, within the set packing layer height range and the proportions of lean liquid and light phase added in this embodiment, the uniform distribution of the tower internal temperature can be achieved.

[0033]

[0034] Among them, 101100% in Comparative Example 1 means that both the lean liquid and the light phase enter from 101. The ratio of 101 and 103 refers to the proportion of the light phase, and 102 and 104 refer to the proportion of the lean liquid.

[0035] The first redistributor 109 is located below the packing layer 105 in section I, the second redistributor 110 is located below the packing layer 106 in section II, and the third redistributor 111 is located below the packing layer 107 in section III. The regeneration redistributor can be a disk type, trough type, pipe type, flower type or combined type liquid redistributor, which is used to evenly distribute the liquid and avoid the generation of local hot spots in the absorption tower 1.

[0036] In the phase separator 2, the upper layer is the light phase 201 and the lower layer is the rich phase 202. The light phase 201 refers to the absorbent solution separated in the phase separator 2, which contains less CO 2 and impurities. The light phase 201 is usually lighter than the rich phase 202 (the absorbent solution containing more CO 2 ), so it will float on the top in the phase separator 2. The light phase 201 layer is connected with a light phase pump 8 through a pipeline. The pumping end of the light phase pump 8 is connected with the third inlet 103 and the first inlet 101 through pipelines. The light phase 201 enters the absorption tower 1 from the third inlet 103 and the first inlet 101. The third inlet 103 is located between the packing layer 105 in section I and the packing layer 106 in section II, and the first inlet 101 is located between the packing layer 107 in section III and the packing layer 108 in section IV. Such a design helps to introduce the light phase 201 at different parts of the tower to adjust the temperature in the tower and promote the absorption of CO 2 The introduction of the light phase 201 helps to maintain the temperature balance in the absorption tower 1 because its inlet temperature is relatively low, which can help absorb and transfer the heat in the tower, thus avoiding local overheating. The inlet temperature of the light phase 201 liquid is lower than 40°C, and the multi-stage isothermal absorption tower 1 can evenly control the temperature of the entire absorption tower 1 below 50°C.

[0037] The absorption tower 1 is connected with the phase separator 2 through a rich liquid pipeline. This connection method allows the rich liquid after absorption (the absorbent solution containing a higher concentration of CO 2 ) to flow out from the bottom of the absorption tower 1 and then enter the phase separator 2 for separation. The separated rich phase 202 is pumped to the heat exchanger 4 by the rich liquid pump 3. The heat exchanger 4 is connected with the top of the desorption tower 7 through a pipeline. The desorption tower 7 is connected with a reboiler 6. The heat provided by the reboiler 6 is used to heat the rich liquid in the desorption tower 7 to promote the desorption of CO 2 The carbon dioxide in the rich liquid is released through the desorption tower 7 and the reboiler 6 to form lean liquid that can be used again. The lean liquid completes the cooling process in the desorption tower 7. There is a cooling link in the desorption tower 7. The regenerated lean liquid in the desorption tower 7 is pumped into the heat exchanger 4 by the lean liquid pump 5, and then the lean liquid enters the absorption tower 1 from the fourth inlet 104 and the second inlet 102. This is to introduce the lean liquid at different parts of the tower to achieve uniform temperature distribution and improve the absorption efficiency. The fourth inlet 104 is near the top of the tower, and the second inlet 102 is located between the packing layer 106 in section II and the packing layer 107 in section III. Such a design helps to form countercurrent contact and improve the absorption of CO2 Absorption efficiency.

[0038] Example 1:

[0039] In the experiment, flue gas with a concentration of 0.3 m / s and 25% CO 2 was introduced from the bottom of the tower. The gas in the tower was in countercurrent contact with the absorbent to absorb CO 2 The absorbent was phase-separated in the phase separation tank 2 into a light phase 201 and a rich phase 202. The rich phase 202 was pumped to the desorption tower 7 for desorption. After desorption, the absorbent liquid became the lean liquid. The lean liquid entered the absorption tower 1 from the fourth inlet 104 and the second inlet 102 respectively, with proportions of 60% and 40% respectively. The light phase 201 was pumped to the third inlet 103 and the first inlet 101 respectively, with proportions of 90% and 10% respectively. It can be found that the temperature of the tower is relatively uniform.

[0040] Comparative Example 1:

[0041] In the experiment, flue gas with a concentration of 0.3 m / s and 25% CO 2 was introduced from the bottom of the tower. The gas in the tower was in countercurrent contact with the absorbent to absorb CO 2 The absorbent was phase-separated in the phase separation tank into a light phase and a rich phase. The rich phase was pumped to the desorption tower for desorption. After desorption, the absorbent liquid became the lean liquid. The lean liquid and the light phase were all sent to the top of the tower. It was significantly found that the temperature at the top of the tower was the highest, and the temperature gradually decreased from top to bottom. The temperature at the top of the tower reached 71 °C, and the temperature at the bottom of the tower was about 40 °C.

[0042] In the description of the present invention, it should be understood that the orientation or positional relationship indicated by the terms "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present invention, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention.

[0043] The above-described embodiments are only descriptions of the preferred embodiments of the present invention, and do not limit the scope of the present invention. Without departing from the design spirit of the present invention, various deformations and improvements made by those of ordinary skill in the art to the technical solutions of the present invention should fall within the protection scope determined by the claims of the present invention.

Claims

1. A multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide, characterized in that: include: An absorption tower (1), wherein the absorption tower (1) is provided with a plurality of inlets, packing layers and redistributors from top to bottom, wherein the inlets are, from top to bottom, a fourth inlet (104), a third inlet (103), a second inlet (102) and a first inlet (101), wherein the rich phase (202) is pumped to a desorption tower (7) for desorption by a lean liquid pump (5), and the desorbed absorption liquid becomes lean liquid, which enters the absorption tower (1) through a pipeline via the fourth inlet (104) and the second inlet (102), wherein the proportion of the lean liquid entering the fourth inlet (104) is in the range of 60%-80%, and the proportion of the lean liquid entering the second inlet (102) is in the range of 20%-40%; the proportion of the light phase (201) entering the third inlet (103) is in the range of 80%-90%, and the proportion of the light phase (201) entering the first inlet (101) is in the range of 20%-10%; The packing layers are, from top to bottom, a stage I packing layer (105), a stage II packing layer (106), a stage III packing layer (107) and a stage IV packing layer (108); and the redistributors are, from top to bottom, a first redistributor (109), a second redistributor (110) and a third redistributor (111); The height of the packing layer (105) of stage I is in the range of 0.5-2.5 m, the height of the packing layer (106) of stage II is in the range of 1.5-3 m, the height of the packing layer (107) of stage III is in the range of 0.5-2 m, and the height of the packing layer (108) of stage IV is in the range of 1.5-3 m; A phase separation tank (2), wherein the bottom of the phase separation tank (2) is connected to the bottom of the absorption tower (1) through a pipeline, and the top of the phase separation tank (2) is connected to the third inlet (103) and the first inlet (101) through a pipeline; a heat exchanger (4), the heat exchanger (4) being connected to the bottom of the phase separation tank (2) via a rich liquid pump (3), and the heat exchanger (4) being connected to the fourth inlet (104) and the second inlet (102) via a pipeline; A desorption tower (7), wherein the desorption tower (7) is connected to a reboiler (6), and the desorption tower (7) is connected to the heat exchanger (4) via a pipeline.

2. The multi-stage uniform temperature phase change absorption tower for high concentration carbon dioxide capture according to claim 1, characterized in that: The upper layer in the phase separation tank (2) is a light phase (201), and the lower layer is a rich phase (202); the rich phase (202) is connected to the bottom of the absorption tower (1) through a pipeline; the light phase (201) is connected to the third inlet (103) and the first inlet (101) through a pipeline; the light phase (201) is connected to a light phase pump (8); the light phase (201) enters the third inlet (103) and the first inlet (101) through the light phase pump (8) and the pipeline.

3. The multi-stage uniform temperature phase change absorption tower for high concentration carbon dioxide capture according to claim 2, characterized in that: The fourth inlet (104) is located between the top of the absorption tower (1) and the section I packing layer (105), the third inlet (103) is located between the section I packing layer and the section II packing layer, the second inlet (102) is located between the section II packing layer and the section III packing layer, and the first inlet (101) is located between the section III packing layer and the section IV packing layer (108).

4. The multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide according to claim 3, characterized in that: The first redistributor (109) is located below the stage I packing layer (105), the second redistributor (110) is located below the stage II packing layer (106), and the third redistributor (111) is located below the stage III packing layer (107).

5. The multi-stage uniform temperature phase change absorption tower for high concentration carbon dioxide capture according to claim 2, characterized in that: The rich phase (202) is connected to the heat exchanger (4) via a rich liquid pump (3).

6. The multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide according to claim 5, characterized in that: The heat exchanger (4) is connected to the top of the desorption tower (7) through a pipeline, and the heat exchanger (4) is connected to the bottom of the desorption tower (7) through a lean liquid pump (5).

7. The multi-stage isotropic phase change absorption tower for capturing high concentration carbon dioxide according to claim 1, characterized in that: The aspect ratio of the absorption tower (1) is in the range of 10-50.

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