CN217391998U - System for capturing carbon dioxide - Google Patents
System for capturing carbon dioxide Download PDFInfo
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- CN217391998U CN217391998U CN202221111183.0U CN202221111183U CN217391998U CN 217391998 U CN217391998 U CN 217391998U CN 202221111183 U CN202221111183 U CN 202221111183U CN 217391998 U CN217391998 U CN 217391998U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The invention relates to the technical field of carbon dioxide capture, and discloses a system for capturing carbon dioxide, which comprises an absorption tower, a regeneration tower, a jet vacuum pump, a flash tank and a barren solution cooler, wherein a barren solution pipeline is arranged between the bottom of the regeneration tower and the absorption tower, the barren solution pipeline is provided with the flash tank and the barren solution cooler, the flash tank is connected with the bottom of the regeneration tower, and the barren solution cooler is connected with the absorption tower; at least one rich liquid pipeline is arranged between the bottom of the absorption tower and the regeneration tower, at least one of the rich liquid pipelines is provided with a jet vacuum pump, the inlet of the jet vacuum pump is connected with the bottom of the absorption tower, and the outlet of the jet vacuum pump is connected with the regeneration tower; the jet vacuum pump is provided with an air suction port, and the top of the flash tank is communicated with the air suction port of the jet vacuum pump through an exhaust pipe.
Description
Technical Field
The invention relates to the technical field of carbon dioxide capture, in particular to a system for capturing carbon dioxide.
Background
With the increasing certainty of global warming, it is internationally assumed that CO is reduced by emission 2 Realize the control of the atmospheric temperatureHas been found to be very slow. For carbon dioxide capture of coal-fired flue gas, the organic amine absorption method gradually embodies technical advantages due to high efficiency and reliable process. Under the normal condition, the temperature of the organic amine absorption liquid needs to be reduced to about 50 ℃ before entering the absorption tower to fully absorb the carbon dioxide in the flue gas, and the temperature of the organic amine absorption liquid needs to be increased to about 104-.
Disclosure of Invention
The utility model aims at overcoming the problem that the energy consumption is high in the carbon dioxide of prior art existence catches, provide a system of entrapment carbon dioxide, this system combines jet vacuum pump and flash tank, the negative pressure that utilizes jet vacuum pump to produce makes the barren liquor (absorption liquid behind the desorption carbon dioxide) evaporation in the flash tank produce barren liquor steam, barren liquor steam mixes the back with rich liquor (absorption liquid behind the absorption carbon dioxide) in jet vacuum pump's exit, thereby barren liquor steam condenses the temperature of exothermic having improved the rich liquor, and then reduced the energy consumption.
In order to achieve the purpose, the utility model provides a system for catching carbon dioxide, the system comprises an absorption tower, a regeneration tower, a jet vacuum pump, a flash tank and a barren liquor cooler, a barren liquor pipeline is arranged between the bottom of the regeneration tower and the absorption tower, the barren liquor pipeline is provided with the flash tank and the barren liquor cooler, the flash tank is connected with the bottom of the regeneration tower, and the barren liquor cooler is connected with the absorption tower; at least one rich liquid pipeline is arranged between the bottom of the absorption tower and the regeneration tower, at least one of the rich liquid pipelines is provided with a jet vacuum pump, the inlet of the jet vacuum pump is connected with the bottom of the absorption tower, and the outlet of the jet vacuum pump is connected with the regeneration tower; the jet vacuum pump is provided with an air suction port, and the top of the flash tank is communicated with the air suction port of the jet vacuum pump through an exhaust pipe.
Through the technical scheme, the utility model discloses following beneficial effect has been obtained:
(1) the utility model discloses a system of entrapment carbon dioxide adopts the negative pressure that the efflux vacuum pump produced ingeniously to make the vaporization of the part barren solution in the flash tank, then utilizes the vaporization latent heat of barren solution to preheat the rich liquid in the efflux vacuum pump to the temperature of rich liquid has been improved, and then has reduced the energy consumption.
(2) The utility model discloses an among the preferred embodiment, still be provided with two rich liquid pipelines between the bottom of absorption tower and regeneration tower, first rich liquid pipeline utilizes the latent heat of vaporization of barren solution to realize that the rich solution preheats, and remaining barren solution and rich solution in the flash tank are directly carried out the heat exchange to second rich liquid pipeline utilization, and make full use of barren solution preheats the rich solution.
(3) The utility model discloses an among the preferred embodiment, still be provided with three rich liquid pipelines between the bottom of absorption tower and regenerator, first rich liquid pipeline utilizes the latent heat of vaporization barren solution to realize that the rich liquid preheats, second rich liquid pipeline utilizes remaining barren solution in the flash tank and rich liquid directly to carry out the heat exchange, make full use of barren solution preheats the rich liquid, third rich liquid pipeline is used for cooling down the material at regenerator top to the temperature that makes from regenerator top exhaust material satisfies the requirement.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
fig. 1 is a schematic configuration diagram of a system for capturing carbon dioxide according to a preferred embodiment of the present invention.
Description of the reference numerals
1 absorption tower, 2 regeneration tower and 3 jet vacuum pumps
4-flash tank 5-lean liquid cooler 6 ejector pump
7 lean-rich liquid heat exchanger 8 boiler 9 tail gas washing tank
10 tail gas washing liquid cooler 11 regeneration cooler 12 regeneration gas separator
Detailed Description
The following describes in detail embodiments of the present invention. It should be understood that the description herein is provided for illustration and explanation of the invention and is not intended to limit the invention.
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
In the description of the present invention, it is to be understood that the terms "bottom" and "top" refer to the bottom and top as shown in the drawings, relative to the corresponding parts themselves, merely for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular configuration and operation, and therefore should not be considered as limiting the invention.
The utility model provides a system for catching carbon dioxide, the system comprises an absorption tower 1, a regeneration tower 2, a jet vacuum pump 3, a flash tank 4 and a barren solution cooler 5, a barren solution pipeline is arranged between the bottom of the regeneration tower 2 and the absorption tower 1, the barren solution pipeline is provided with the flash tank 4 and the barren solution cooler 5, the flash tank 4 is connected with the bottom of the regeneration tower 2, and the barren solution cooler 5 is connected with the absorption tower 1; at least one rich liquid pipeline is arranged between the bottom of the absorption tower 1 and the regeneration tower 2, at least one of the rich liquid pipelines is provided with a jet vacuum pump 3, the inlet of the jet vacuum pump 3 is connected with the bottom of the absorption tower 1, and the outlet of the jet vacuum pump 3 is connected with the regeneration tower 2; the jet vacuum pump 3 is provided with an air suction port, and the top of the flash tank 4 is communicated with the air suction port of the jet vacuum pump 3 through an exhaust pipe.
According to the utility model discloses, the system still includes ejector pump 6, and ejector pump 6 sets up between absorption tower 1 and jet vacuum pump 3. The ejector pump 6 is used for increasing the fluid pressure and ensuring the flow velocity of the fluid at the inlet of the jet vacuum pump 3, so that vacuum is formed at the joint of the jet vacuum pump and the flash tank.
According to the utility model discloses, blast pipe and jet vacuum pump 3's induction port intercommunication is passed through at the top of flash tank 4, utilizes the negative pressure that jet vacuum pump 3 formed after spraying the rich liquid, causes the negative pressure environment in flash tank 4's top, because pressure reduces, the lean solution part evaporation that is basically in saturated condition in flash tank 4 forms lean solution steam to in being sucked jet vacuum pump 3, behind jet vacuum pump 3's diffusion section, thereby lean solution steam mixes and condenses with the rich liquid and improves the temperature of rich liquid.
According to the present invention, in the absorption tower 1, the flue gas containing carbon dioxide is brought into countercurrent contact with the lean solution (organic amine absorption liquid) at 40 ℃ to 50 ℃ to remove carbon dioxide from the flue gas. The absorption tower 1 comprises a rich liquid outlet and a lean liquid inlet, wherein the rich liquid outlet is arranged at the bottom of the absorption tower 1, and the lean liquid inlet is arranged at the upper part of the absorption tower 1.
In the present invention, the type of the organic amine absorbent is not particularly limited, and may be an organic amine absorbent commonly used in the art, for example, ethanolamine, 2-methylamino-ethanol, piperazine, 2-amino-2-methyl-1-propanol.
In the present invention, the description of "upper portion" and "lower portion" is introduced for the purpose of explaining the entering positions of the rich liquid, the lean liquid and the flue gas, and the "upper portion" and "lower portion" are relative terms and do not refer to a specific position point or area. For example, the bottom of the absorption column may be referred to as the lower portion of the top of the absorption column, and conversely, the bottom of the absorption column may be referred to as the upper portion of the top of the absorption column, and for example, a position at one-half the height of the absorption column may be referred to as the "lower portion" of the top of the absorption column, and may also be referred to as the "upper portion" of the bottom of the absorption column.
According to the present invention, in the regeneration tower 2, the rich liquid is heated to 104 ℃ to 110 ℃ to remove carbon dioxide from the rich liquid, so that the rich liquid becomes a lean liquid. The regeneration tower 2 includes a rich liquid inlet and a lean liquid outlet, and the rich liquid inlet is usually disposed at the upper part of the regeneration tower 2, and the lean liquid outlet is disposed at the bottom of the regeneration tower 2.
According to the utility model discloses, under the preferred condition, the entrance of efflux vacuum pump 3 is equipped with the nozzle.
According to the utility model discloses, under the preferred condition, the rich liquid pipeline is two, is equipped with jet vacuum pump 3 on the first rich liquid pipeline, is equipped with lean solution heat exchanger 7 between second rich liquid pipeline and the lean solution pipeline and makes the material in second rich liquid pipeline and the lean solution pipeline can carry out the heat transfer. More preferably, lean-rich liquid heat exchanger 7 is disposed between flash tank 4 and lean liquid cooler 5. Thus, the heat of the residual barren solution (the unevaporated barren solution) in the flash tank 4 can be fully utilized, and the energy consumption of the system is reduced.
According to the utility model discloses, the rich solution in two rich solution pipelines can get into regenerator tower 2's upper portion through same rich solution import, also can get into regenerator tower 2's upper portion through the rich solution import of difference, under the condition that each interval heat balance needs of comprehensive consideration, preferably, regenerator tower 2's upper portion is equipped with two rich solution imports, correspond respectively and connect a rich solution pipeline, wherein, the setting height difference of two rich solution imports (the rich solution import is apart from regenerator tower 2 top or bottom highly different), the rich solution import that links to each other with first rich solution pipeline sets up the height that highly is higher than the rich solution import that links to each other with second rich solution pipeline. The arrangement can send rich liquid with different temperatures to the optimal position of the regeneration tower, thereby further reducing the energy consumption of the system. The specific height of the two rich liquid inlets is determined according to the actual condition of the system.
According to the utility model discloses, under the preferred condition, the rich liquid pipeline is three, is equipped with jet vacuum pump 3 on the first rich liquid pipeline, is equipped with lean solution heat exchanger 7 between second rich liquid pipeline and the lean solution pipeline and makes the material in second rich liquid pipeline and the lean solution pipeline can carry out the heat transfer. The third rich liquid pipeline is connected with the regeneration tower 2 directly.
According to the utility model discloses, the rich solution in three rich solution pipelines can get into the upper portion of regenerator tower 2 through the import of same rich solution, also can get into the upper portion of regenerator tower 2 through the import of rich solution of difference, under the condition that each interval heat balance needs is being considered comprehensively, preferably, the upper portion of regenerator tower 2 is equipped with three rich solution import, correspond respectively and connect a rich solution pipeline, wherein, the setting height difference of three rich solution import (the rich solution import is apart from the 2 top of regenerator tower or the height difference of bottom promptly), first rich solution pipeline links to each other with the rich solution import of lower, second rich solution pipeline links to each other with the rich solution import of middle department, third rich solution pipeline links to each other with the rich solution import of highest department. The arrangement can send rich liquid with different temperatures to the optimal position of the regeneration tower, thereby further reducing the energy consumption of the system. The specific heights of the three rich liquid inlets are determined according to the actual condition of the system, generally, the rich liquid with lower temperature enters the higher part of the regeneration tower, and the rich liquid with higher temperature enters the lower part of the regeneration tower, and the position height of the rich liquid inlet is designed according to the specific heights.
According to the utility model discloses, under the preferred condition, be equipped with the filler in the absorption tower 1, the filler is arranged in the absorption tower 1.
In the present invention, the type of the filler may be a filler commonly used in the art, for example, a structured filler.
According to the present invention, the system preferably further comprises a boiler 8, wherein the boiler 8 is connected to the bottom of the regeneration tower 2. The boiler 8 is used for heating the liquid at the bottom of the regeneration tower 2 to evaporate part of the liquid to form gas, so that the evaporated gas is used for heating the rich liquid entering from the upper part of the regeneration tower 2 to remove carbon dioxide in the rich liquid.
According to the utility model discloses, the form of boiler 8 does not have special restriction, can be conventional electrical heating boiler, also can be steam heating boiler, and under the preferred circumstances, boiler 8 is steam heating boiler, utilizes the liquid heat transfer of external steam (the steam that produces in other workshop sections) and regenerator column 2's bottom to make partial liquid evaporation form gas, thereby utilize the gaseous rich liquid that gets into by regenerator column 2 upper portion of the heating of evaporating, the carbon dioxide in the rich liquid of desorption.
According to the utility model discloses, because flue gas behind the desorption carbon dioxide probably carries organic amine absorbent, under the preferred condition, the system still includes tail gas washing tank 9 and tail gas washing liquid cooler 10, the upper portion of absorption tower 1 communicates with tail gas washing tank 9 and tail gas washing liquid cooler 10 in proper order. The flue gas after carbon dioxide removal enters a tail gas washing tank 9 filled with demineralized water to remove the organic amine absorbent carried in the flue gas, then enters a tail gas washing liquid cooler 10 through a tail gas washing pump to be cooled, and can be directly discharged after being cooled, or can enter the top of the absorption tower 1 and be discharged from a flue gas outlet at the top.
According to the utility model discloses, preferably, the system still includes regeneration cooler 11 and regeneration gas separator 12, and the top of regenerator column 2 communicates with regeneration cooler 11 and regeneration gas separator 12 in proper order. And the carbon dioxide gas in the regeneration tower 2 sequentially enters the regeneration cooler 11, the regeneration gas separator 12 and the compressor through a carbon dioxide gas outlet at the top of the regeneration tower 2, and finally a liquid carbon dioxide product is obtained.
According to a particularly preferred embodiment of the present invention, as shown in fig. 1, the system includes an absorption tower 1, a regeneration tower 2, a jet vacuum pump 3, a flash tank 4, a lean liquid cooler 5, an ejector pump 6, a lean and rich liquid heat exchanger 7, a boiler 8, a tail gas washing tank 9, a tail gas washing liquid cooler 10, a regeneration cooler 11, and a regeneration gas separator 12; the bottom and the upper part of the absorption tower 1 are respectively provided with a rich liquid outlet and a lean liquid inlet, and the bottom and the upper part of the regeneration tower 2 are respectively provided with a lean liquid outlet and a rich liquid inlet. A barren liquor pipeline is arranged between a barren liquor outlet at the bottom of the regeneration tower 2 and a barren liquor inlet at the upper part of the absorption tower 1, and a flash tank 4, a barren and rich liquor heat exchanger 7 and a barren liquor cooler 5 are sequentially arranged on the barren liquor pipeline along the flow direction of barren liquor. Three rich liquid pipelines are arranged between the rich liquid outlet at the bottom of the absorption tower 1 and the rich liquid inlet at the upper part of the regeneration tower 2. Along the flow direction of rich liquid, be equipped with ejector pump 6 and efflux vacuum pump 3 on the first rich liquid pipeline in proper order, wherein, efflux vacuum pump 3 has the induction port, and the top of flash tank 4 is passed through the blast pipe and is communicate with the induction port of efflux vacuum pump 3. The second rich liquor line meets the lean liquor line at lean-rich liquor heat exchanger 7. The second rich liquid pipeline is directly connected with a rich liquid outlet at the bottom of the absorption tower 1 and a rich liquid inlet at the upper part of the regeneration tower 2. The upper part of the regeneration tower 2 is provided with three rich liquid inlets which are respectively and correspondingly connected with a rich liquid pipeline, wherein the three rich liquid inlets are arranged at different heights, the first rich liquid pipeline is connected with the lowest rich liquid inlet, the second rich liquid pipeline is connected with the middle rich liquid inlet, and the third rich liquid pipeline is connected with the highest rich liquid inlet. The bottom of the regeneration tower 2 is also connected with a boiler 8 through a steam pipeline in a closed loop. The top of the regeneration tower 2 is provided with a carbon dioxide gas outlet which is connected with a regeneration cooler 11, a regeneration gas separator 12 and a compressor in sequence. The lower part and the top of the absorption tower 1 are respectively provided with a flue gas inlet and a flue gas outlet, and the flue gas inlet is arranged above the rich liquid outlet. The upper part of the absorption tower 1 is also sequentially connected with a tail gas washing tank 9 and a tail gas washing liquid cooler 10, and the tail gas washing liquid cooler 10 is connected with the upper part of the absorption tower 1 to form a closed loop.
Methods of using the system of particularly preferred embodiments of the present invention may include: the method comprises the following steps that flue gas containing carbon dioxide enters an absorption tower 1 through a flue gas inlet at the lower part of the absorption tower 1, and is in countercurrent contact with lean liquid (organic amine absorbent) entering from a lean liquid inlet at the upper part of the absorption tower 1 to remove the carbon dioxide in the flue gas, the lean liquid absorbs the carbon dioxide and becomes rich liquid, the rich liquid is gathered at the bottom of the absorption tower 1, the flue gas after the carbon dioxide removal firstly enters a tail gas washing tank 9 filled with desalted water to remove the organic amine absorbent carried in the flue gas, then enters a tail gas washing liquid cooler 10 through a tail gas washing pump to be cooled, and enters the top of the absorption tower 1 after being cooled and is discharged from a flue gas outlet at the top; the rich liquid gathered at the bottom of the absorption tower 1 flows through a rich liquid pipeline and enters the upper part of the regeneration tower 2, in the regeneration tower 2, the rich liquid is in countercurrent contact with the bottom evaporation gas of the regeneration tower 2, the rich liquid is further heated, so that the carbon dioxide in the rich liquid is removed and changed into lean liquid, and the lean liquid is gathered at the bottom of the regeneration tower 2; carbon dioxide gas enters the regenerative cooler 11, the regenerative gas separator 12 and the compressor in sequence through a carbon dioxide gas outlet at the top of the regeneration tower 2, and finally a liquid carbon dioxide product is obtained. The barren solution gathered at the bottom of the regeneration tower 2 enters the upper part of the absorption tower 1 through a barren solution pipeline and is in countercurrent contact with the flue gas again, so that the organic amine absorbent is recycled. The rich liquid gathered at the bottom of the absorption tower 1 is divided into three parts which respectively enter a first rich liquid pipeline, a second rich liquid pipeline and a third rich liquid pipeline, and the mass ratio of the rich liquid entering the first rich liquid pipeline, the second rich liquid pipeline and the third rich liquid pipeline is controlled. The rich solution entering the first rich solution pipeline is pumped into the jet vacuum pump 3 through the ejector pump 6, partial lean solution in the flash tank 4 is evaporated by using negative pressure generated by the jet vacuum pump 3 to generate lean solution steam, the lean solution steam and the rich solution are mixed at an outlet of the jet vacuum pump, the lean solution steam is condensed to release latent heat of vaporization so as to increase the temperature of the rich solution, and then the rich solution enters the regeneration tower 2 through a rich solution inlet at the lowest part of the regeneration tower 2. And the rest barren solution in the flash tank 4 enters a barren and rich solution heat exchanger 7 through a barren solution pump, in the barren and rich solution heat exchanger 7, the rest barren solution exchanges heat with the rich solution in a second rich solution pipeline, the barren solution after heat exchange enters the absorption tower 1 through a barren solution cooler 5 and a barren solution inlet at the upper part of the absorption tower 1, and the rich solution after heat exchange enters the regeneration tower 2 through a rich solution inlet at the middle part of the regeneration tower 2. The rich liquid entering the third rich liquid pipeline directly enters the regeneration tower 2 through a rich liquid inlet at the highest part of the regeneration tower 2.
The above detailed description describes the preferred embodiments of the present invention, but the present invention is not limited to the details of the above embodiments, and the technical idea of the present invention can be within the scope of the present invention, and can be right to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the present invention does not separately describe various possible combinations.
In addition, various embodiments of the present invention can be combined arbitrarily, and the disclosed content should be regarded as the present invention as long as it does not violate the idea of the present invention.
Claims (10)
1. A system for capturing carbon dioxide is characterized by comprising an absorption tower (1), a regeneration tower (2), a jet vacuum pump (3), a flash tank (4) and a lean liquid cooler (5), wherein a lean liquid pipeline is arranged between the bottom of the regeneration tower (2) and the absorption tower (1), the flash tank (4) and the lean liquid cooler (5) are arranged on the lean liquid pipeline, the flash tank (4) is connected with the bottom of the regeneration tower (2), and the lean liquid cooler (5) is connected with the absorption tower (1); at least one rich liquid pipeline is arranged between the bottom of the absorption tower (1) and the regeneration tower (2), a jet vacuum pump (3) is arranged on at least one of the rich liquid pipelines, an inlet of the jet vacuum pump (3) is connected with the bottom of the absorption tower (1), and an outlet of the jet vacuum pump (3) is connected with the regeneration tower (2); the jet vacuum pump (3) is provided with an air suction port, and the top of the flash tank (4) is communicated with the air suction port of the jet vacuum pump (3) through an exhaust pipe.
2. System according to claim 1, characterized in that the inlet of the jet vacuum pump (3) is provided with a nozzle.
3. The system according to claim 1 or 2, wherein the number of the rich liquid pipelines is two, a jet vacuum pump (3) is arranged on the first rich liquid pipeline, and a lean rich liquid heat exchanger (7) is arranged between the second rich liquid pipeline and the lean liquid pipeline so that the second rich liquid pipeline and the materials in the lean liquid pipeline can exchange heat.
4. The system according to claim 3, characterized in that the upper part of the regeneration tower (2) is provided with two rich liquid inlets respectively connected with one rich liquid pipeline, wherein the two rich liquid inlets are arranged at different heights, and the rich liquid inlet connected with the first rich liquid pipeline is arranged at a higher height than the rich liquid inlet connected with the second rich liquid pipeline.
5. The system according to claim 1 or 2, wherein the number of the rich liquid pipelines is three, a jet vacuum pump (3) is arranged on the first rich liquid pipeline, a lean rich liquid heat exchanger (7) is arranged between the second rich liquid pipeline and the lean liquid pipeline to enable the second rich liquid pipeline and materials in the lean liquid pipeline to exchange heat, three rich liquid inlets are arranged at the upper part of the regeneration tower (2) and are respectively and correspondingly connected with one rich liquid pipeline, the three rich liquid inlets are arranged at different heights, the first rich liquid pipeline is connected with the lowest rich liquid inlet, the second rich liquid pipeline is connected with the middle rich liquid inlet, and the third rich liquid pipeline is connected with the highest rich liquid inlet.
6. The system according to claim 1 or 2, characterized in that the absorption column (1) is packed with packing, which is arranged in layers in the absorption column (1).
7. The system according to claim 1 or 2, characterized in that the system further comprises a boiler (8), the boiler (8) being connected to the bottom of the regeneration column (2).
8. A system according to claim 7, characterized in that the boiler (8) is a steam heating boiler.
9. The system according to claim 1 or 2, further comprising a tail gas washing tank (9) and a tail gas washing liquid cooler (10), wherein the upper part of the absorption tower (1) is further communicated with the tail gas washing tank (9) and the tail gas washing liquid cooler (10) in sequence.
10. The system according to claim 1 or 2, characterized in that the system further comprises a regenerative cooler (11) and a regenerative gas separator (12), and the top of the regeneration tower (2) is communicated with the regenerative cooler (11) and the regenerative gas separator (12) in sequence.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221111183.0U CN217391998U (en) | 2022-05-09 | 2022-05-09 | System for capturing carbon dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221111183.0U CN217391998U (en) | 2022-05-09 | 2022-05-09 | System for capturing carbon dioxide |
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| CN217391998U true CN217391998U (en) | 2022-09-09 |
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| CN202221111183.0U Active CN217391998U (en) | 2022-05-09 | 2022-05-09 | System for capturing carbon dioxide |
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- 2022-05-09 CN CN202221111183.0U patent/CN217391998U/en active Active
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