A carbon dioxide capture system

Abstract

The present invention discloses a carbon dioxide capture system, comprising: a catalytic desorption reactor; a catalytic desorption unit disposed within the catalytic desorption reactor, the catalytic desorption unit comprising a plurality of trays and a liquid accumulation tray arranged sequentially along a first direction, the trays being loaded with a solid catalyst; hollow regions extending through the trays along the first direction, the orthographic projections of the hollow regions of the odd-numbered trays and the orthographic projections of the hollow regions of the even-numbered trays being at least partially non-overlapping along the first direction; the first direction being from the top of the catalytic desorption reactor toward the bottom of the catalytic desorption reactor. A rich liquid formed after an organic amine solution absorbs carbon dioxide enters the catalytic desorption reactor for desorption. The desorption reactor is equipped with a plurality of trays loaded with catalyst, thereby increasing the desorption rate of the rich liquid and reducing the desorption temperature, thereby reducing the energy consumption for regenerating the rich liquid in the carbon dioxide capture system.

Description

Technical Field

[0001] The present invention relates to the technical field of flue gas treatment, and more particularly, to a carbon dioxide capture system. Background Art

[0002] Currently, carbon dioxide is captured from flue gas using an organic amine solution to absorb the carbon dioxide in the flue gas, generating carbamate. The absorbed solution becomes a rich liquid, which is discharged from the bottom of the absorption tower. After heat exchange, it enters a desorption tower. Under certain temperature and pressure conditions, the carbon dioxide in the rich liquid is desorbed and the absorbent is regenerated to produce a lean liquid. After heat exchange, the lean liquid returns to the absorption tower to continue absorbing carbon dioxide from the flue gas, completing the cycle of the organic amine solution. In existing technologies, the desorption tower is a packed tower, and externally supplied steam is used as the heat source for desorption of the rich liquid in the desorption tower. This results in high energy consumption for absorbent regeneration throughout the entire process.

[0003] Therefore, there is an urgent need to provide a carbon dioxide capture system that can reduce the energy consumption of absorbent regeneration. Summary of the Invention

[0004] The purpose of the present invention is to overcome the above-mentioned defects in the prior art and provide a carbon dioxide capture system.

[0005] To achieve the above object, the technical solution of the present invention is as follows:

[0006] A carbon dioxide capture system comprises: a catalytic desorption reactor;

[0007] The catalytic desorption reactor is provided with a catalytic desorption unit, the catalytic desorption unit comprising a plurality of tower plates and a liquid accumulation tray sequentially arranged along a first direction, the tower plates being loaded with a solid catalyst;

[0008] The edge of the tower plate is provided with a hollow area running through the tower plate along a first direction. Along the first direction, the orthographic projection of the hollow area of ​​the odd-numbered tower plate and the orthographic projection of the hollow area of ​​the even-numbered tower plate at least partially do not overlap; the first direction is the direction from the top of the catalytic desorption reactor to the bottom of the catalytic desorption reactor.

[0009] Optionally, an overflow plate is provided on the edge of the tower plate near the hollow area, and the overflow plate is arranged to intersect with the plane where the tower plate is located.

[0010] Optionally, a downcomer is further provided at the bottom of the tower plate, and along the first direction, the orthographic projection of the hollow area at least partially overlaps with the orthographic projection of the downcomer.

[0011] Optionally, the tower plate includes a plurality of through holes penetrating the tower plate along the first direction; and the diameter of the catalyst is greater than the diameter of the through holes.

[0012] Optionally, the carbon dioxide capture system further comprises a heater;

[0013] The heater includes a second rich liquid inlet and a third rich liquid outlet, and the catalytic desorption reactor includes a third rich liquid inlet and a second rich liquid outlet; the second rich liquid outlet is connected to the liquid accumulation tray, and the second rich liquid outlet is connected to the second rich liquid inlet; the third rich liquid inlet is located below the liquid accumulation tray, and the third rich liquid inlet is connected to the third rich liquid outlet.

[0014] Optionally, an air guide cylinder is provided on the liquid accumulation tray; an umbrella-shaped cap is provided on the top of the air guide cylinder, and an upper air guide hole is provided at the connection between the air guide cylinder and the umbrella-shaped cap; the bottom of the air guide cylinder is connected to the liquid accumulation tray, and a lower air guide hole is provided at the connection between the air guide cylinder and the liquid accumulation tray.

[0015] Optionally, the carbon dioxide capture system further comprises an absorption tower;

[0016] A first rich liquid outlet is provided at the bottom of the absorption tower, and a first rich liquid inlet is provided at the top of the catalytic desorption reactor, wherein the first rich liquid outlet is connected to the first rich liquid inlet;

[0017] A lean liquid inlet is provided at the top of the absorption tower, and a lean liquid outlet is provided at the bottom of the catalytic desorption reactor, and the lean liquid inlet is communicated with the lean liquid outlet.

[0018] Optionally, the carbon dioxide capture system further comprises a heat exchanger;

[0019] The heat exchanger includes a first channel and a second channel; both ends of the first channel are respectively connected to the first rich liquid outlet and the first rich liquid inlet, and both ends of the second channel are respectively connected to the lean liquid outlet and the lean liquid inlet.

[0020] Optionally, the carbon dioxide capture system further includes a cooling component, wherein the cooling component is connected to the lean liquid inlet and the second channel.

[0021] Optionally, the catalytic desorption reactor is provided with a plurality of catalytic desorption units sequentially arranged along the first direction.

[0022] The implementation of the present invention will have the following beneficial effects:

[0023] The carbon dioxide capture system provided by an embodiment of the present invention includes: a catalytic desorption reactor; a catalytic desorption unit disposed within the catalytic desorption reactor, the catalytic desorption unit comprising a plurality of trays and a liquid accumulation tray arranged sequentially along a first direction, the trays being loaded with a solid catalyst; hollow regions extending through the trays along the first direction, wherein the orthographic projections of the hollow regions of the odd-numbered trays and the orthographic projections of the hollow regions of the even-numbered trays in the first direction at least partially do not overlap; the first direction being from the top of the catalytic desorption reactor toward the bottom of the catalytic desorption reactor. A rich liquid formed after an organic amine solution absorbs carbon dioxide enters the catalytic desorption reactor for desorption. The desorption reactor is equipped with a plurality of trays loaded with catalyst, which increases the desorption rate of the rich liquid and reduces the desorption temperature, thereby reducing the energy consumption for regenerating the rich liquid in the carbon dioxide capture system. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0025] in:

[0026] Figure 1 This is a schematic diagram of the carbon dioxide capture system provided by the present invention.

[0027] Figure 2 yes Figure 1 A schematic diagram of a middle tower plate.

[0028] Figure 3 yes Figure 1 Another schematic diagram of the middle tower plate

[0029] Figure 4 yes Figure 1 An enlarged schematic diagram of area A in the middle.

[0030] Figure 5 This is a schematic diagram of a desorption reactor in the carbon dioxide capture system provided by the present invention. DETAILED DESCRIPTION

[0031] The following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. All other embodiments obtained by ordinary technicians in this field based on the embodiments of the present invention without making any creative efforts shall fall within the scope of protection of the present invention.

[0032] Reference Figure 1 、 Figure 2 , a carbon dioxide capture system, comprising: a catalytic desorption reactor 1;

[0033] A catalytic desorption unit 11 is provided in the catalytic desorption reactor 1. The catalytic desorption unit 11 includes a plurality of trays 111 and a liquid accumulation tray 112 sequentially arranged along a first direction X. The trays 111 are loaded with a solid catalyst.

[0034] The edge of the tower plate 111 is provided with a hollow area 110 that penetrates the tower plate 111 along the first direction X. Along the first direction X, the orthographic projection of the hollow area 110 of the odd-numbered tower plate and the orthographic projection of the hollow area 110 of the even-numbered tower plate at least partially do not overlap; the first direction X is the direction from the top of the catalytic desorption reactor 1 to the bottom of the catalytic desorption reactor 1.

[0035] It should be noted that Figure 2 In the figure, only the catalytic desorption unit 11 includes three tower plates 111 arranged in sequence along the first direction X as an example, and the tower plates 111 are respectively a first tower plate 111-1, a second tower plate 111-2 and a third tower plate 111-3 arranged in sequence along the first direction X. The first tower plate 111-1 is arranged close to the top of the catalytic desorption reactor 1, and the third tower plate 111-3 is arranged away from the top of the catalytic desorption reactor 1. A first rich liquid inlet 12 is provided above the first tray 111-1. The first rich liquid inlet 12 is arranged at one end of the hollow area 110-1 away from the first tray 111-1. A rich organic amine liquid containing carbon dioxide flows into the first tray 111-1 from the first rich liquid inlet 12, fully contacts the catalyst loaded on the first tray 111-1, and then flows into the second tray 111-2 through the hollow area 110-1 of the first tray 111-1; the rich liquid then fully contacts the catalyst on the second tray 111-2, and then flows into the third tray 111-3 through the hollow area 110-2 of the second tray 111-2; the rich liquid then fully contacts the catalyst on the third tray 111-3, and finally flows into the liquid accumulation tray 112 through the hollow area 110-3 of the third tray 111-3; thereby, under high temperature conditions, carbon dioxide is desorbed from the rich liquid as it passes through each tray 111.

[0036] Furthermore, the hollow areas 110 of the odd-numbered trays and the hollow areas 110 of the even-numbered trays are arranged opposite to each other along the second direction Y, and the second direction Y intersects with the first direction X. For example, Figure 2The hollow area 110-1 of the first tower plate 111-1 and the hollow area 110-2 of the second tower plate 111-2 are arranged relative to each other along the second direction Y. In the process of the rich liquid flowing through the first tower plate 111-1 into the second tower plate 111-2, the path on the first tower plate 111-1 is the longest, that is, the contact time with the catalyst is long, which improves the decomposition rate of the rich liquid; similarly, the hollow area 110-3 of the third tower plate 111-3 and the hollow area 110-2 of the second tower plate 111-2 are arranged relative to each other along the second direction Y.

[0037] It is understood that in the prior art, the rich liquid is desorbed through a packed tower. However, in this embodiment, by loading a highly active, high-specific-surface-area granular solid catalyst within the catalytic desorption reactor 1, the desorption reactor, combined with the catalytic desorption process, can increase the desorption rate of the carbon dioxide-rich organic amine rich liquid and reduce the desorption temperature, thereby reducing the energy consumption for regenerating the organic amine rich liquid. Optionally, the catalytic desorption reactor 1 may be provided with multiple groups of catalytic desorption units 11 arranged sequentially along the first direction X. Figure 5 In the figure, only two groups of catalytic desorption units 11 are provided as an example, and two groups of heaters 2 are provided to ensure the complete desorption of the rich liquid.

[0038] In some optional embodiments, referring to Figure 3 An overflow plate 113 is provided at the edge of the tower plate 111 near the hollow area 110 , and the overflow plate 113 is arranged to intersect with the plane where the tower plate 111 is located.

[0039] It can be understood that the overflow plate 113 is arranged to intersect with the plane where the tower plate 111 is located, that is, the height of the overflow plate 113 is higher than the plane where the tower plate 111 is located. The overflow plate 113 blocks the rich liquid from flowing into the tower plate 111. When the rich liquid level is higher than the height of the overflow plate 113, the rich liquid flows into the next tower plate 111; the setting of the overflow plate 113 prevents the rich liquid from flowing away quickly but forms a liquid seal on the surface of the tower plate 111, so that the rich liquid is in full contact with the catalyst on the tower plate 111, thereby improving the decomposition rate.

[0040] Furthermore, a downcomer 117 is provided at the bottom of tray 111. Along the first direction X, the orthographic projection of the hollowed-out area 110 at least partially overlaps with the orthographic projection of downcomer 117. Downcomer 117 drains the rich liquid, allowing it to flow into tray 111 from the end of tray 111 away from the hollowed-out area 110. Preferably, the orthographic projection of the hollowed-out area 110 overlaps with the orthographic projection of downcomer 117.

[0041] In some optional embodiments, referring to Figure 1The carbon dioxide capture system also includes a heater 2; the heater 2 includes a second rich liquid inlet 21 and a third rich liquid outlet 22, and the catalytic desorption reactor 1 includes a second rich liquid outlet 13 and a third rich liquid inlet 14; the second rich liquid outlet 13 is connected to the liquid accumulation tray 112, and the second rich liquid outlet 13 is communicated with the second rich liquid inlet 21; the third rich liquid inlet 14 is located below the liquid accumulation tray 112, and the third rich liquid inlet 14 is communicated with the third rich liquid outlet 22.

[0042] It should be noted that, referring to Figure 2 The tower plate 111 includes a plurality of through holes 1112 that pass through the tower plate 111 along the first direction X; the diameter of the catalyst is larger than the diameter of the through holes 1112 to ensure that the catalyst does not fall. Optionally, the catalytic desorption reactor 1 is filled with a carbon dioxide desorption catalyst to reduce the desorption temperature of the rich liquid. The catalyst type is selected from one or more of metal oxide catalysts, molecular sieve catalysts, solid superacid catalysts, and composite catalysts; the catalyst shape is spherical, cylindrical, etc. After the rich liquid flows into the liquid accumulation tray 112, it enters the heater 2 through the second rich liquid outlet 13. After being heated, it returns to the catalytic desorption reactor 1 through the third rich liquid inlet 14. The high-temperature gas rises through the through holes 1112 of the tower plate 111, disturbing the catalyst so that the gas, liquid and catalyst solids on the tower plate 111 are fully in contact. The high-temperature gas transfers heat to the rich liquid on the tower plate 111. Under the catalytic action, the carbon dioxide in the rich liquid is initially desorbed.

[0043] Specifically, heater 2 is equipped with a steam inlet 23 and a steam condensate outlet 24. Externally supplied steam heats the rich liquid, vaporizing some of the water vapor and further desorbing some of the carbon dioxide. The steam within heater 2 is isolated from the rich liquid, providing heat only without coming into contact with it. The heated rich liquid returns to the bottom of the desorption reactor. The desorbed carbon dioxide gas and vaporized water vapor flow upward through the through-holes 1112 of tray 111 until they are discharged through the regeneration gas outlet 16 at the top of the catalytic desorption reactor 1. The remaining liquid forms the lean liquid and flows to the bottom of the catalytic desorption reactor. In practice, the number of trays 111 and the height of the liquid layer accumulated on each tray 111 are determined by the rising gas pressure. The total resistance of the liquid layer on each tray 111 is less than the rising gas pressure, ensuring that the gas can pass through to the liquid layer on the topmost tray 111. Furthermore, the inner walls of the through-holes 1112 have a rough surface, such as a sawtooth or other irregular shape, which disperses the rising gas into small bubbles, increasing the contact area between the gas and the rich liquid on tray 111 and improving heat transfer.

[0044] In some optional embodiments, combined with Figure 1 、 Figure 4An air guide tube 114 is provided on the liquid collection tray 112; an umbrella-shaped cap 115 is provided on the top of the air guide tube 114, and an upper air guide hole 116 is provided at the connection between the air guide tube 114 and the umbrella-shaped cap 115; the bottom of the air guide tube 114 is connected to the liquid collection tray 112, and a lower air guide hole 1141 is provided at the connection between the air guide tube 114 and the liquid collection tray 112.

[0045] It should be noted that the heated rich liquid returns to the catalytic desorption reactor 1 through the third rich liquid inlet 14, and the vaporized water vapor and further desorbed carbon dioxide gas rise, sequentially passing through the lower gas guide holes 1141 and the upper gas guide holes 116 on the liquid accumulation tray 112, and then rise upward through the through holes 1112 of the tower plate 111 until it is discharged through the regeneration gas outlet 16 at the top of the catalytic desorption reactor 1. The carbon dioxide capture system provided in this embodiment also includes a carbon dioxide separator 6, and the regeneration gas outlet 16 is connected to the carbon dioxide separator 6. The gas discharged from the catalytic desorption reactor 1 is cooled and then separated into gas and liquid by the carbon dioxide separator 6 to obtain gaseous carbon dioxide product gas.

[0046] Furthermore, along the first direction X, the orthographic projection of the air guide cylinder 114 lies within the orthographic projection of the umbrella cap 115. That is, the edge of the umbrella cap 115 extends beyond the edge of the air guide cylinder 114. The edge of the umbrella cap 115 is connected to the air guide cylinder 114, and an upper air guide hole 116 is provided at the connection. The umbrella cap 115 can prevent rich liquid flowing down from the tray 111 from entering the air guide cylinder 114. The inclined design facilitates the flow of rich liquid that lands on the umbrella cap 115 down to the liquid collection tray 112.

[0047] In some optional embodiments, referring to Figure 1 The carbon dioxide capture system also includes an absorption tower 3; a first rich liquid outlet 31 is provided at the bottom of the absorption tower 3, and a first rich liquid inlet 12 is provided at the top of the catalytic desorption reactor 1, and the first rich liquid outlet 31 is connected to the first rich liquid inlet 12; a lean liquid inlet 32 ​​is provided at the top of the absorption tower 3, and a lean liquid outlet 15 is provided at the bottom of the catalytic desorption reactor 1, and the lean liquid inlet 32 ​​is connected to the lean liquid outlet 15.

[0048] It should be noted that the flue gas enters the absorption tower 3 and mixes with the organic amine solution in the absorption tower 3 to obtain a rich liquid and purified gas. Specifically, the organic amine solution can be one or more of primary amines, secondary amines, tertiary amines, and sterically hindered amines. In this embodiment, a flue gas inlet 33 is provided at the bottom of the absorption tower 3. The flue gas inlet 33 is connected to a flue gas source. The flue gas is flue gas with a carbon dioxide concentration of 5-40% (v / v) emitted from industries such as electricity, cement, steel, and chemicals. The absorption tower 3 is a packed tower, with a liquid distributor at the top, tower plates or packing in the middle, and a gas distributor at the bottom. The packing can be a random packing represented by ball rings, other high-performance packing represented by saddle packing, ring-saddle packing, spherical packing, etc., or a structured packing represented by Stedman wire mesh, Mellapak corrugated mesh, etc. Absorption tower 3 is filled with an organic amine solution, which absorbs carbon dioxide from the flue gas to form carbamate, resulting in a rich liquid. A purified gas outlet 34 is provided at the top of absorption tower 3, through which purified gas (i.e., the purified flue gas) is discharged. The rich liquid enters catalytic desorption reactor 1 for desorption, resulting in a lean liquid. The lean liquid then returns to absorption tower 3 to continue absorbing carbon dioxide, completing the absorption solution cycle.

[0049] In some optional embodiments, referring to Figure 1 The carbon dioxide capture system further includes a heat exchanger 4; the heat exchanger 4 includes a first channel 41 and a second channel 42; the two ends of the first channel 41 are respectively connected to the first rich liquid outlet 31 and the first rich liquid inlet 12, and the two ends of the second channel 42 are respectively connected to the lean liquid outlet 15 and the lean liquid inlet 32.

[0050] It can be understood that the rich liquid is a low-temperature absorption solution, and the lean liquid is an absorption solution after heating and decomposition. By setting up the heat exchanger 4 to exchange heat between the rich liquid and the lean liquid, the temperature of the low-temperature rich liquid is initially increased and the temperature of the high-temperature lean liquid is initially decreased, thereby reducing the energy consumption of subsequent reheating of the rich liquid and cooling of the lean liquid.

[0051] In some optional embodiments, referring to Figure 1 The carbon dioxide capture system further includes a cooling component 5 , which is connected to the lean liquid inlet 32 ​​and the second channel 42 .

[0052] It is understandable that carbon dioxide gas in the absorption solution is easy to precipitate at high temperature, which will reduce the carbon dioxide absorption rate of the absorption solution. Therefore, a cooling component 5 is set, and the lean liquid after heat exchange is cooled again and enters the absorption tower 3 to continue absorbing carbon dioxide, completing the circulation of the absorption solution. Specific embodiment:

[0054] Coal-fired flue gas is used as raw gas with a carbon dioxide concentration of 11.9% (v), an oxygen content of 4.5% (v), a nitrogen content of 75% (v), and other components being water and trace amounts of sulfur dioxide and nitrogen oxides. A 30% (wt) monoethanolamine aqueous solution is used as the absorption solution to absorb carbon dioxide from the coal-fired flue gas at 40°C and normal pressure to obtain a carbon dioxide-rich liquid.

[0055] Comparative Example:

[0056] In the comparative example, the rich liquid is desorbed by a regeneration tower in the prior art, which is a packed tower. The carbon dioxide regeneration process includes the following steps:

[0057] In the first step, the rich liquid is sent to the upper part of the regeneration tower after heat exchange. Two layers of 4-meter-high structured packing are set inside the regeneration tower. A liquid distributor is set on each layer of packing to ensure that the solution is evenly distributed in the packing.

[0058] In the second step, a liquid accumulation tray is set at the bottom of the lower packing, and the solution after preliminary desorption is collected. Under the action of gravity, it enters the heater outside the desorption reactor through a pipeline for heating and regeneration. The heating steam is 0.3MPa saturated steam, the tower top pressure is 30kPa, the tower bottom temperature is 108℃, and the tower top temperature is 91℃.

[0059] In the third step, the heated solution enters the bottom of the regeneration tower, the regeneration gas rises, transfers heat to the solution on the filler, and is finally discharged from the regeneration gas outlet at the top of the regeneration tower. After cooling and gas-liquid separation, the gaseous carbon dioxide product is obtained.

[0060] In the fourth step, the solution at the bottom of the regeneration tower is fully desorbed to obtain lean liquid, which is then sent to the absorption tower after heat exchange.

[0061] Example:

[0062] In the embodiment, the rich liquid is desorbed by the catalytic desorption reactor of the present invention, and the carbon dioxide regeneration process includes the following steps:

[0063] In the first step, the rich liquid is sent to the upper part of the desorption reactor after heat exchange. Three horizontal tower plates are set inside the regeneration tower. The tower plates are evenly opened with holes of 2mm diameter. A layer of granular solid acid carbon dioxide desorption catalyst with a diameter of 2-4mm is arranged on the tower plates. The rich liquid coming down from the upper part of the desorption reactor is fully in contact with the catalyst on the tower plates, and the rich liquid is desorbed for the first time.

[0064] In the second step, the solution after the first desorption descends to the second and third tower plates through the downcomer, and is further desorbed on the tower plates to improve the desorption effect of the solution.

[0065] Step 3: A liquid accumulation tray is set at the bottom of the tower, and the desorbed solution is collected. Under the action of gravity, it enters the heater outside the desorption reactor through a pipeline for heating and regeneration. The heating steam is 0.3MPa saturated steam, the tower top pressure is 30kPa, the tower bottom temperature is 100℃, and the tower top temperature is 70℃.

[0066] In the fourth step, the heated solution enters the bottom of the desorption reactor, the regeneration gas rises, transfers heat to the solution on the tower plate, and is finally discharged from the regeneration gas outlet at the top of the desorption reactor. After cooling and gas-liquid separation, the gaseous carbon dioxide product is obtained.

[0067] In the fifth step, the solution at the bottom of the desorption reactor is fully desorbed to obtain lean liquid, which is then sent to the absorption tower after heat exchange.

[0068] Table 1 Comparison of regeneration effects and energy consumption of the embodiments

[0069] Rich liquid acid gas loading Lean liquid acid gas loading Renewable energy consumption Comparative Example <![CDATA[39.6LCO2 / L]]> <![CDATA[25.4LCO2 / L]]> <![CDATA[3.98GJ / tCO2]]> Example <![CDATA[40.2LCO2 / L]]> <![CDATA[23.8LCO2 / L]]> <![CDATA[3.16GJ / tCO2]]>

[0070] Table 1 shows that the energy consumption of carbon dioxide desorption of the present invention is much lower than that of the prior art.

[0071] The above-described embodiments merely represent several implementation methods of the present invention. While the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the patent application. It should be noted that a person skilled in the art would be able to make various modifications and improvements without departing from the spirit of the present invention, all of which fall within the scope of protection of the present invention. Therefore, the scope of protection of the patent for this invention shall be determined by the appended claims.

Claims

1. A carbon dioxide capture system comprising: catalytic desorption reactor; The catalytic desorption reactor is provided with a catalytic desorption unit, the catalytic desorption unit comprising a plurality of tower plates and a liquid accumulation tray sequentially arranged along a first direction, the tower plates being loaded with a solid catalyst; The tray edge is provided with a hollow area penetrating the tray along a first direction, and along the first direction, the orthographic projection of the hollow area of ​​the odd-numbered tray and the orthographic projection of the hollow area of ​​the even-numbered tray at least partially do not overlap; the first direction is the direction from the top of the catalytic desorption reactor to the bottom of the catalytic desorption reactor; An overflow plate is provided on the edge of the tower plate near the hollow area, and the overflow plate is arranged to intersect with the plane where the tower plate is located; A downcomer is further provided at the bottom of the tray, and along the first direction, the orthographic projection of the hollow area at least partially overlaps with the orthographic projection of the downcomer; The tower plate includes a plurality of through holes penetrating the tower plate along a first direction; the diameter of the catalyst is greater than the diameter of the through holes.

2. The carbon dioxide capture system according to claim 1, characterized in that Also includes heater; The heater includes a second rich liquid inlet and a third rich liquid outlet, and the catalytic desorption reactor includes a second rich liquid outlet and a third rich liquid inlet; the second rich liquid outlet is connected to the liquid accumulation tray, and the second rich liquid outlet is connected to the second rich liquid inlet; the third rich liquid inlet is located below the liquid accumulation tray, and the third rich liquid inlet is connected to the third rich liquid outlet.

3. The carbon dioxide capture system according to claim 1, wherein: An air guide cylinder is provided on the liquid accumulation tray; an umbrella-shaped cap is provided on the top of the air guide cylinder, and an upper air guide hole is provided at the connection between the air guide cylinder and the umbrella-shaped cap; the bottom of the air guide cylinder is connected to the liquid accumulation tray, and a lower air guide hole is provided at the connection between the air guide cylinder and the liquid accumulation tray.

4. The carbon dioxide capture system according to claim 1, wherein: Including absorption tower; A first rich liquid outlet is provided at the bottom of the absorption tower, and a first rich liquid inlet is provided at the top of the catalytic desorption reactor, wherein the first rich liquid outlet is connected to the first rich liquid inlet; A lean liquid inlet is provided at the top of the absorption tower, and a lean liquid outlet is provided at the bottom of the catalytic desorption reactor, and the lean liquid inlet is communicated with the lean liquid outlet.

5. The carbon dioxide capture system according to claim 4, characterized in that Also includes heat exchanger; The heat exchanger includes a first channel and a second channel; both ends of the first channel are respectively connected to the first rich liquid outlet and the first rich liquid inlet, and both ends of the second channel are respectively connected to the lean liquid outlet and the lean liquid inlet.

6. The carbon dioxide capture system according to claim 5, characterized in that A cooling assembly is also included, wherein the cooling assembly connects the lean liquid inlet and the second channel.

7. The carbon dioxide capture system according to claim 1, wherein: The catalytic desorption reactor is provided with a plurality of catalytic desorption units sequentially arranged along the first direction.

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