Multi-stage uniform-temperature phase change absorption tower for capturing high-concentration carbon dioxide

Abstract

The invention relates to the technical field of carbon dioxide emission reduction, and discloses a multi-stage uniform-temperature phase change absorption tower for capturing high-concentration carbon dioxide, the multi-stage uniform-temperature phase change absorption tower comprises an absorption tower, a plurality of inlets, filler layers and redistributors are distributed on the absorption tower from top to bottom, and the inlets are sequentially a fourth inlet, a third inlet, a second inlet and a first inlet from top to bottom; the bottom of the split-phase tank is communicated with the bottom of the absorption tower through a pipeline, and the top of the split-phase tank is communicated with the third inlet and the first inlet through pipelines; the heat exchanger is communicated with the bottom of the split-phase tank through a rich liquid pump, and the heat exchanger is communicated with the fourth inlet and the second inlet through pipelines; the desorption tower is connected with a reboiler, and the desorption tower is connected with the heat exchanger through a pipeline. An interstage cooling process is replaced by a multi-stage shunting process, and uniform temperature distribution in the whole absorption tower is realized by adjusting the shunting proportion, so that local hot spots are avoided.

Description

Technical Field

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

[0002] With the rapid development of industry and the use of a large number of fossil fuels, the content of greenhouse gases such as carbon dioxide in the atmosphere has continued to increase, and global warming, glacier melting and other problems have become increasingly serious. Among them, carbon dioxide is considered to be one of the main culprits of climate change. In order to mitigate the negative impact of climate change. Carbon capture, utilization and storage (CCUS) is considered to be a technology with industrial application potential. Among various CCUS technologies, the organic amine absorption method in the chemical absorption method is widely used due to its strong selectivity and wide range of applications. It has now become one of the mainstream technologies for capturing carbon dioxide after combustion.

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

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

[0005] The purpose of the present invention is to provide a multi-stage uniform temperature phase change absorption tower for capturing high-concentration carbon dioxide to solve the problems existing in the prior art. A multi-stage diversion process is adopted to replace the inter-stage cooling process. By adjusting the diversion ratio, a uniform temperature distribution in the entire absorption tower is achieved to avoid local hot spots.

[0006] To achieve the above-mentioned purpose, the present invention provides the following scheme: The present invention provides a multi-stage uniform temperature phase change absorption tower for capturing high-concentration carbon dioxide, comprising: an absorption tower, wherein the absorption tower is provided with a plurality of inlets, packing layers and redistributors from top to bottom, wherein the inlets are sequentially a fourth inlet, a third inlet, a second inlet and a first inlet from top to bottom, wherein the packing layers are sequentially a section I packing layer, a section II packing layer, a section III packing layer and a section IV packing layer from top to bottom, and wherein the redistributors are sequentially a first redistributor, a second redistributor and a third redistributor from top to bottom; a phase separation tank, wherein the bottom of the phase separation tank is connected to the bottom of the absorption tower through a pipeline, and the top of the phase separation tank is connected to the third inlet and the first inlet through a pipeline; a heat exchanger, wherein the heat exchanger is connected to the bottom of the phase separation tank through a rich liquid pump, and the heat exchanger is connected to the fourth inlet and the second inlet through a pipeline; a desorption tower, wherein the desorption tower is connected to a reboiler, and the desorption tower is connected to the heat exchanger through a pipeline.

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

[0008] According to a multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide provided by the present invention, the fourth inlet is located between the top of the absorption tower and the first stage packing layer, the third inlet is located between the first stage packing layer and the second stage packing layer, the second inlet is located between the second stage packing layer and the third stage packing layer, and the first inlet is located between the third stage packing layer and the fourth stage packing layer.

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

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

[0011] According to a multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide provided by the present invention, 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 by the lean liquid pump, the desorbed absorption liquid becomes lean liquid, and the lean liquid enters the absorption tower through the fourth inlet and the second inlet through a pipeline.

[0012] According to a multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide provided by the present invention, the proportion of the lean liquid entering the fourth inlet is in the range of 60%-80%, and the proportion of the lean liquid entering the second inlet is in the range of 20%-40%.

[0013] According to a multi-stage isothermal phase change absorption tower for capturing high-concentration carbon dioxide provided by the present invention, the proportion of the light phase entering the third inlet ranges from 80% to 90%, and the proportion of the light phase entering the first inlet ranges from 20% to 10%.

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

[0015] According to the present invention, a multi-stage uniform temperature phase change absorption tower for capturing high-concentration carbon dioxide is provided, wherein the height-to-diameter ratio of the absorption tower is in the range of 10-50.

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

[0017] By opening holes at specific positions between the packing layers and adopting a multi-stage diversion process instead of an interstage cooling process, the temperature in the entire absorption tower can be evenly distributed by adjusting the diversion ratio to avoid local hot spots. This can improve the absorption performance on the one hand, and reduce the degradation of the absorbent and the loss of organic amines on the other. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[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 DESCRIPTION

[0021] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0022] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments.

[0023] There is a problem in the existing technology that there is a lack of proper treatment of the heat released during the absorption of carbon dioxide by the absorbent. For example, the patent with publication number CN116036803A discloses an absorption tower for capturing flue gas carbon dioxide, the absorption tower includes a bottom recycling section, an absorption section and a water washing section arranged in sequence along the flue gas flow direction, the bottom recycling section includes a liquid distributor, a variable diameter packing layer, an absorption tower bottom, a liquid divider 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 the semi-rich liquid in the absorption liquid is transported to the semi-rich liquid cooler for cooling, and then returned to the liquid distributor; the invention adopts the bottom recycling process to replace the interstage cooling process. Although the storage tank equipment is reduced, the semi-rich liquid cooler is introduced, which increases additional costs.

[0024] The patent with publication number CN118236819A discloses a gas-liquid redistributor for an absorption tower, an absorption tower and a method, wherein the gas-liquid redistributor for an absorption tower comprises a distribution plate and at least one distribution mixer; the outer side wall of the distribution plate can fit closely with the inner side wall of the absorption tower; the distribution plate is provided with at least one vent hole; the distribution mixer is arranged above the vent hole and covers the vent hole; the distribution mixer comprises a plurality of groups of symmetrically cross-arranged inclined plates; the inclined plates are provided with a plurality of openings for dividing the flue gas passing through the distribution plate. Although the absorption tower improves the capture efficiency of harmful gases in the flue gas, it does not take into account that the heat release of the absorbent will also increase when the capture rate is increased.

[0025] The patent with the publication number of CN113648805A discloses a dual-zone dual-circulation flue gas carbon dioxide absorption tower, including an absorption tower body, a lower absorption packing layer, an upper absorption packing layer, a lower spray device, an upper spray device, an absorption tower demister, a tower kettle one, a tower kettle two and an absorption liquid preparation box; the absorption tower body is divided into an upper absorption tower and a lower absorption tower; the lower absorption tower is provided with a lower absorption packing layer, and a lower spray device is provided above the lower absorption packing layer; the upper absorption tower is provided with an upper absorption packing layer, and an upper spray device is provided above the upper absorption packing layer. The invention can reduce the height of the absorption tower under the premise of ensuring the carbon dioxide capture rate of the lower layer by increasing the liquid-gas ratio of the lower absorption tower, and effectively reduce the height of the absorption tower under the premise of ensuring the carbon dioxide capture rate of the upper layer by increasing the absorbent concentration of the upper absorption tower and increasing the absorption reaction intensity, and finally achieve a higher carbon dioxide capture rate of the whole tower while effectively reducing the height of the absorption tower, but while increasing the capture rate, the harm caused by the increase in the absorbent temperature is not considered.

[0026] In order to solve the problem of heat release when the absorbent absorbs carbon dioxide, this device adopts a multi-stage diversion process instead of an inter-stage cooling process, and achieves uniform temperature distribution in the entire absorption tower by adjusting the diversion ratio. The specific contents are as follows:

[0027] like Figure 1 As shown, the present invention provides a multi-stage isothermal phase-change absorption tower for capturing high-concentration carbon dioxide, comprising: 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 sequentially a fourth inlet 104, a third inlet 103, a second inlet 102 and a first inlet 101 from top to bottom, the packing layers are sequentially a first-stage packing layer 105, a second-stage packing layer 106, a third-stage packing layer 107 and a fourth-stage packing layer 108 from top to bottom, and the redistributors are sequentially a first redistributor from top to bottom. A distributor 109, a second redistributor 110 and a 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 the 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 to the 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, which control a certain proportion of lean liquid and light phase 201 to enter the tower. The packing layer is used to promote the contact between the flue gas and the absorbent, thereby increasing the CO 2The redistributor is used to evenly distribute the liquid, ensure that the absorbent is evenly distributed in the packing layer, avoid the generation of local hot spots, and open holes at specific positions between the packing layers without affecting the capture rate. The multi-stage diversion process is used instead of the interstage cooling process. By adjusting the diversion ratio, the temperature in the entire absorption tower 1 is evenly distributed to avoid 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] Flue gas enters absorption tower 1 from the bottom, and high concentration CO 2 The concentration range is between 20% and 40%, and the gas velocity range is between 0.2m / s and 3m / 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-stage packing layer 105 and the tower top, and is used to introduce lean liquid in a ratio range of 60%-80%. The third inlet 103 is located between the I-stage packing layer 105 and the II-stage packing layer 106, and is used to introduce the light phase 201 in a ratio range of 80%-90%. The second inlet 102 is located between the II-stage packing layer 106 and the III-stage packing layer 107, and is used to introduce lean liquid in a ratio range of 20%-40%. The first inlet 101 is located between the III-stage packing layer 107 and the IV-stage packing layer 108, and is used to introduce the light phase 201 in a ratio range of 20%-10%.

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

[0032] The following table is a comparison of data of different packing layer heights in this embodiment and a comparison of the temperature in the tower after introducing different proportions of lean liquid and light phase. According to the data in the table, it can be obtained that under the range of packing layer heights set in this embodiment and the proportion of lean liquid and light phase added, a uniform distribution of temperature in the tower 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 to 103 refers to the ratio of the light phase, and 102 and 104 refer to the ratio of the lean liquid.

[0035] 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. The regeneration distributor can be a disc-type, trough-type, tube-type, flower-type or combination-type liquid redistributor, which is used to evenly distribute the liquid to avoid the generation of local hot spots in the absorption tower 1.

[0036] The upper layer in the phase separation tank 2 is the light phase 201, and the lower layer is the rich phase 202. The light phase 201 is separated in the phase separation tank 2 and contains less CO 2 The light phase 201 is usually larger than the rich phase 202 (containing more CO 2 The absorbent solution) is light, so it will float on the top in the phase separation tank 2. The light phase 201 layer is connected to the light phase pump 8 through a pipeline. The pumping end of the light phase pump 8 is connected to the third inlet 103 and the first inlet 101 through a pipeline. 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 of the first stage and the packing layer 106 of the second stage, and the first inlet 101 is located between the packing layer 107 of the third stage and the packing layer 108 of the fourth stage. This design is helpful to introduce the light phase 201 in different parts of the tower to adjust the temperature in the tower and promote CO 2 The introduction of light phase 201 helps maintain the temperature balance in the absorption tower 1 because its inlet temperature is low, which can help absorb and transfer the heat in the tower, thereby avoiding local overheating. The inlet temperature of the light phase 201 liquid is lower than 40°C, and the multi-stage temperature-averaged absorption tower 1 can evenly control the temperature of the entire absorption tower 1 below 50°C.

[0037] The absorption tower 1 is connected to the phase separation tank 2 through a rich liquid pipeline. This connection method allows the absorbed rich liquid (containing a high concentration of CO 2 The absorbent solution) flows out from the bottom of the absorption tower 1 and then enters the phase separation tank 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 to the top of the desorption tower 7 through a pipeline. The desorption tower 7 is connected to the reboiler 6. The heat provided by the reboiler 6 is used to heat the rich liquid in the desorption tower 7 to promote CO 2 The desorption of carbon dioxide in the rich liquid is released through the desorption tower 7 and the reboiler 6 to form a lean liquid that can be used again. The lean liquid completes the cooling process in the desorption tower 7. The desorption tower 7 is provided with a cooling link. The regenerated lean liquid in the desorption tower 7 is pumped to the heat exchanger 4 through the lean liquid pump 5. 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 into different parts of the tower to achieve uniform temperature distribution and improve the absorption efficiency. The fourth inlet 104 is located near the top of the tower, and the second inlet 102 is located between the II-stage packing layer 106 and the III-stage packing layer 107. This design is conducive to forming countercurrent contact and improving CO2 absorption efficiency.

[0038] Embodiment 1:

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

[0040] Comparative Example 1:

[0041] The experiment introduced 0.3m / s, 25% CO from the bottom of the tower. 2 The flue gas in the tower contacts the absorbent in countercurrent to absorb CO 2 The absorbent is separated into light phase and rich phase in the phase separation tank. The rich phase is pumped to the desorption tower for desorption. The desorbed absorption liquid becomes lean liquid. The lean liquid and light phase are all sent to the top of the tower. It is obvious that the temperature at the top of the tower is the highest, and the temperature gradually decreases from top to bottom. The temperature at the top of the tower reaches 71°C and the temperature at the bottom of the tower is around 40°C.

[0042] In the description of the present invention, it should be understood that the terms "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside" and "outside" etc., indicating orientations or positional relationships, are based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention, and do not indicate or imply 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 understood as a limitation on the present invention.

[0043] The embodiments described above are only descriptions of the preferred modes of the present invention, and are not intended to limit the scope of the present invention. Without departing from the design spirit of the present invention, various modifications and improvements made to the technical solutions of the present invention by ordinary technicians in this field should all 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 sequentially a fourth inlet (104), a third inlet (103), a second inlet (102) and a first inlet (101) from top to bottom, the packing layers are sequentially a first-stage packing layer (105), a second-stage packing layer (106), a third-stage packing layer (107) and a fourth-stage packing layer (108) from top to bottom, and the redistributors are sequentially a first redistributor (109), a second redistributor (110) and a third redistributor (111) from top to bottom; 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 isothermal 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). The rich phase (202) is pumped to the desorption tower (7) for desorption by the lean liquid pump (5). The desorbed absorption liquid becomes lean liquid, and the lean liquid enters the absorption tower (1) through the fourth inlet (104) and the second inlet (102) through a pipeline.

7. The multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide according to claim 6, characterized in that: 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%.

8. The multi-stage uniform temperature phase change absorption tower for capturing high concentration carbon dioxide according to claim 7, characterized in that: 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%.

9. The multi-stage isothermal phase change absorption tower for capturing high-concentration carbon dioxide according to claim 1, characterized in that: The height range of the stage I packing layer (105) is 0.5-2.5 m, the height range of the stage II packing layer (106) is 1.5-3 m, the height range of the stage III packing layer (107) is 0.5-2 m, and the height range of the stage IV packing layer (108) is 1.5-3 m.

10. The multi-stage uniform temperature 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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