CN219630976U - Carbon dioxide collecting system - Google Patents
Carbon dioxide collecting system Download PDFInfo
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- CN219630976U CN219630976U CN202320468646.7U CN202320468646U CN219630976U CN 219630976 U CN219630976 U CN 219630976U CN 202320468646 U CN202320468646 U CN 202320468646U CN 219630976 U CN219630976 U CN 219630976U
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- liquid
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- carbon dioxide
- outlet
- absorption tower
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 99
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 50
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 205
- 150000001412 amines Chemical class 0.000 claims abstract description 60
- 238000010521 absorption reaction Methods 0.000 claims abstract description 55
- 238000003795 desorption Methods 0.000 claims abstract description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000003546 flue gas Substances 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 230000006835 compression Effects 0.000 claims description 9
- 238000007906 compression Methods 0.000 claims description 9
- 238000000034 method Methods 0.000 abstract description 7
- 238000001816 cooling Methods 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract 1
- 239000000428 dust Substances 0.000 abstract 1
- 229910052717 sulfur Inorganic materials 0.000 abstract 1
- 239000011593 sulfur Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- -1 carbon dioxide amine Chemical class 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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 utility model discloses a carbon dioxide collecting system and method, comprising a flue gas pretreatment device, an absorption tower, a desorption tower and a recovery device which are sequentially communicated; the flue gas pretreatment device comprises a dust remover, a sulfur removal tower and a cooling tower which are sequentially communicated, wherein an air outlet of the cooling tower is communicated with an air inlet at the bottom of the absorption tower; the absorption tower absorbs carbon dioxide in the flue gas by utilizing amine liquid, an air outlet at the top of the absorption tower is communicated with a chimney, a liquid outlet at the bottom of the absorption tower is also communicated with a flow divider, a liquid outlet at the upper part of the flow divider is communicated with a liquid inlet at the top of the absorption tower, a liquid outlet at the lower part of the flow divider is communicated with a liquid inlet at the bottom of the desorption tower, and a liquid outlet at the bottom of the desorption tower is communicated with a liquid inlet at the top of the absorption tower; the desorption tower is used for separating amine liquid after absorbing carbon dioxide; the recovery device collects the carbon dioxide separated from the amine liquid. The utility model improves the utilization rate of amine liquid in the system and reduces the production cost.
Description
Technical Field
The utility model relates to the field of carbon dioxide collection, in particular to a carbon dioxide collection system.
Background
Carbon capture, utilization and sealing technology, abbreviated as CCUS, is used for purifying carbon dioxide generated and discharged in industrial production, and then the carbon dioxide is put into a new production process for recycling. The CCUS technology development and application have gaps, and a large gap exists between the existing emission reduction technology system and the actual demand.
The current CCUS industrial application is mainly an exemplary project of a large enterprise, and the investment cost is too high for small and medium enterprises. The existing trapping method mainly comprises an adsorption method, a chemical absorption method and a membrane separation method, heat energy at each stage cannot be effectively utilized in the application process, and in the amine liquid carbon dioxide absorption method, absorbed carbon dioxide amine liquid is not subjected to refined collection, most of amine liquid is recovered under the condition of not contacting carbon dioxide, and the heat energy released in the amine liquid recovery process is not recycled, so that the operation cost is too high.
Disclosure of Invention
Aiming at the defects that the prior art does not carry out zone recovery and waste heat utilization on the amine liquid which absorbs the carbon dioxide amine liquid, the utility model provides a carbon dioxide collecting system.
A carbon dioxide collecting system comprises an absorption tower, a desorption tower and a recovery device which are sequentially communicated; the absorption tower is used for absorbing carbon dioxide in the flue gas by utilizing amine liquid, an air outlet at the top of the absorption tower is communicated with a chimney, the absorption tower is also communicated with a flow divider, a liquid outlet at the bottom of the absorption tower is communicated with a liquid inlet of the flow divider, a liquid outlet at the upper part of the flow divider is communicated with a liquid inlet at the top of the absorption tower, a liquid outlet at the bottom of the flow divider is communicated with a liquid inlet at the bottom of the desorption tower, a liquid outlet at the bottom of the desorption tower is communicated with a liquid inlet at the top of the absorption tower, the desorption tower is used for separating the amine liquid after absorbing the carbon dioxide, and the recovery device is used for collecting the carbon dioxide separated by the amine liquid; the device comprises an absorption tower, a first liquid inlet of the absorption tower is communicated with a liquid inlet at the top of the absorption tower, and a second liquid inlet of the absorption tower is communicated with a liquid outlet at the bottom of the absorption tower; the second liquid inlet of the lean-rich liquid heat exchanger is communicated with the lower liquid outlet of the flow divider, the second liquid outlet of the lean-rich liquid heat exchanger is communicated with the first liquid inlet of the desorption tower, and a rich liquid pump is arranged in the middle of the second liquid inlet.
Further, the evaporator further comprises an evaporation tank, wherein the evaporation tank comprises a first liquid inlet, a second liquid inlet and a liquid outlet, the first liquid inlet is communicated with the upper liquid outlet of the flow divider, and the second liquid inlet is communicated with the first liquid outlet of the desorption tower; and a liquid outlet of the evaporation tank is communicated with a first liquid inlet of the lean-rich liquid heat exchanger.
Further, the device also comprises a reboiler and a steam generator, wherein the liquid inlet of the reboiler is communicated with the second liquid outlet at the bottom of the desorption tower, the liquid outlet of the reboiler is communicated with the second liquid inlet of the desorption tower, and the reboiler is supplied with heat by the steam generator.
Further, the cooling tower is internally divided into three layers along the axial direction, and heat exchange pipelines are arranged between each two layers.
Further, the recovery device comprises a heat exchanger, a gas-liquid separator and a compression fan which are sequentially communicated; the air inlet of the heat exchanger is communicated with the top air outlet of the desorption tower, the outlet of the heat exchanger is communicated with the air inlet of the gas-liquid separator, the top air outlet of the gas-liquid separator is communicated with the compression fan, and the bottom liquid outlet of the gas-liquid separator is communicated with the third liquid inlet of the desorption tower.
Compared with the prior art, the utility model has the advantages that:
1. the density layering is utilized to divide the amine liquid absorbed with carbon dioxide into low-saturation amine liquid and high-saturation amine liquid, and the low-saturation amine liquid is directly put into a flow for absorbing carbon dioxide in flue gas, so that the amine liquid which is not absorbed and saturated can be effectively prevented from directly entering a desorption tower to be discharged, and is regenerated and recycled together with the high-saturation amine liquid, thereby effectively reducing cost;
2. the heat energy released by the low-saturation amine liquid cooling is utilized to preheat the high-saturation amine liquid, so that the desorption process of the high-saturation amine liquid is effectively shortened, and the desorption efficiency is improved.
Drawings
FIG. 1 is a schematic diagram of a carbon dioxide collection system of the present utility model.
In the figure: 1. An absorption tower; 2. a shunt; 3. a lean rich liquid heat exchanger; 4. an evaporation tank; 5. a rich liquid pump; 6. a lean liquid pump; 7. a desorption tower; 8. a reboiler; 9. a heat exchanger; 10. a gas-liquid separator; 11. a compression fan.
Detailed Description
The present utility model provides a carbon dioxide collection system comprising:
the pretreated flue gas enters an air inlet at the bottom of the absorption tower 1 for communication; the air outlet at the top of the absorption tower 1 is communicated with a chimney, amine liquid flows in from the liquid inlet at the top of the absorption tower 1 and flows out from the liquid outlet at the bottom of the absorption tower 1, the inside of the absorption tower 1 is divided into three layers along with the height reduction from bottom to top, and a heat exchange pipeline is arranged between each two layers.
The flue gas moves from bottom to top of the absorption tower 1, the amine liquid in the absorption tower 1 flows in from a liquid inlet at the top of the absorption tower 1, and flows out from top to bottom from a liquid outlet at the bottom of the absorption tower 1, so that the flue gas and the amine liquid in the absorption tower 1 are in reverse contact, and the combination of the amine liquid and carbon dioxide is accelerated; three layers are arranged in the absorption tower 1, so that the smoke is sequentially contacted with each layer of amine liquid in the rising process, and carbon dioxide is fixed in the amine liquid to the greatest extent; through setting up heat exchange pipeline between every layer, guarantee that the inside temperature of absorption tower 1 remains unanimous throughout, improve the binding efficiency of carbon dioxide and amine liquid.
The liquid outlet at the bottom of the absorption tower 1 is communicated with the liquid inlet of the flow divider 2, the flow divider is divided into an upper part and a lower part, the liquid outlet at the upper part of the flow divider 2 is communicated with a first liquid inlet of the evaporation tank 4, a second liquid inlet of the evaporation tank 4 is communicated with a first liquid inlet of the desorption tower 7, the evaporation tank 4 is also connected with a lean-rich liquid heat exchanger 3, the lean-rich liquid heat exchanger 3 comprises a first liquid inlet, a second liquid inlet, a first liquid outlet and a second liquid outlet, the first liquid outlet of the evaporation tank 4 is communicated with the first liquid inlet of the lean-rich liquid heat exchanger 3, the first liquid outlet of the lean-rich liquid heat exchanger 3 is communicated with the liquid inlet at the top of the absorption tower 1 through a pipeline, and a lean liquid pump 6 is arranged on the pipeline; the lower liquid outlet of the flow divider 2 is communicated with the second liquid inlet of the lean-rich liquid heat exchanger 3, the second liquid inlet of the lean-rich liquid heat exchanger 3 is communicated with the first liquid inlet of the absorption tower 1 through a pipeline, and a rich liquid pump 5 is arranged on the pipeline.
Because the concentration of carbon dioxide in the flue gas, the flow rate of the flue gas and the contact time of the amine liquid are different, the combination degree of the amine liquid and the carbon dioxide is greatly different, the generated saturated liquid density is different, and the amine liquid entering the liquid separator is low-saturation amine liquid and high-saturation amine liquid according to the density difference atmosphere.
The low-saturation amine liquid in the flow divider 2 and the low-saturation amine liquid generated by desorbing the high-saturation amine liquid in the absorption tower 1 enter the evaporation tank 4 together and then enter the lean-rich liquid heat exchanger 3, the low-saturation amine liquid in the lean-rich liquid heat exchanger 3 is cooled to be lower than 42 ℃, the cooled low-saturation amine liquid enters the absorption tower 1 through the lean liquid pump 6 to absorb and combine carbon dioxide in the flue gas, and the combination efficiency of the low-temperature amine liquid and the carbon dioxide can be accelerated; the lean rich liquid heat exchanger 3 preheats the high-saturation amine liquid from the lower part of the separator 2 to more than 85 ℃ by utilizing the heat energy released by the steam and the low-saturation amine liquid generated by the evaporation tank 4, so that the heating time for the high-saturation amine liquid to enter the desorption tower 7 is reduced, and the desorption flow is shortened.
And a reboiler 8 is further arranged in the desorption tower 7, a liquid inlet of the reboiler 8 is communicated with a second liquid outlet at the bottom of the desorption tower 7, and a liquid outlet of the reboiler 8 is communicated with a second liquid inlet of the desorption tower 7, and is heated by the steam generator.
The preheated high-saturation amine liquid is further heated by a reboiler 8, so that the preheated high-saturation amine liquid meets the temperature requirement during desorption.
The gas outlet of the absorption tower 1 is communicated with a recovery device, the recovery device comprises a heat exchanger 9, a gas-liquid separator 10 and a compression fan 11, the gas inlet of the heat exchanger 9 is communicated with the top gas outlet of the desorption tower 7, the outlet of the heat exchanger 9 is communicated with the gas inlet of the gas-liquid separator 10, the top gas outlet of the gas-liquid separator 10 is communicated with the compression fan 11, and the bottom liquid outlet of the gas-liquid separator 10 is communicated with the third liquid inlet of the desorption tower 7.
The gas generated after the desorption of the high-saturation amine liquid firstly enters a heat exchanger 9 to be condensed, the condensed gas is separated by carbon dioxide and desorption liquid under the action of a gas-liquid separator 10, the desorption liquid enters a desorption tower 7 through a liquid outlet at the bottom of the gas-liquid separator 10, and the carbon dioxide gas is compressed by a compression fan 11 and then bottled for standby.
The workflow of the system is as follows:
after the pretreated flue gas enters the absorption tower 1, carbon dioxide in the flue gas is contacted and combined with amine liquid in the absorption tower 1, the pretreated flue gas moves upwards from the bottom of the absorption tower 1, the amine liquid moves downwards from the top of the absorption tower 1, at the moment, the carbon dioxide is reversely contacted with the amine liquid, so that the combination of the amine liquid and the carbon dioxide is quickened, the amine liquid containing the carbon dioxide is formed, and the flue gas after absorbing the carbon dioxide is discharged into a chimney through an air outlet at the top of the cooling tower.
The amine liquid containing the absorbed carbon dioxide forms low-saturation amine liquid and high-saturation amine liquid in the flow divider 2 under the action of gravity separation, the low-saturation amine liquid is cooled and then is input into the absorption tower 1 to continuously combine and absorb the carbon dioxide, and the high-saturation amine liquid is input into the desorption tower 7 to be desorbed.
The high-saturation amine liquid is desorbed into low-saturation amine liquid and carbon dioxide in the desorption tower 7, the low-saturation amine liquid is cooled and then is input into the absorption tower 1 to continuously combine and absorb the carbon dioxide, and carbon dioxide gas obtained by desorption enters the compression fan 11 to be compressed and collected.
In this document, terms such as front, rear, upper, lower, etc. are defined with respect to the positions of the components in the drawings and with respect to each other, for clarity and convenience in expressing the technical solution. It should be understood that the use of such orientation terms should not limit the scope of the claimed utility model.
The embodiments described above and features of the embodiments herein may be combined with each other without conflict.
The foregoing description of the preferred embodiments of the utility model is not intended to limit the utility model to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the utility model are intended to be included within the scope of the utility model.
Claims (6)
1. A carbon dioxide collection system, characterized by: comprises an absorption tower (1), a desorption tower (7) and a recovery device which are communicated in sequence;
the absorption tower (1) utilizes amine liquid to absorb carbon dioxide in flue gas, an air outlet at the top of the absorption tower (1) is communicated with a chimney, the absorption tower (1) is also communicated with a flow divider (2), a liquid outlet at the bottom of the absorption tower (1) is communicated with a liquid inlet of the flow divider (2), a liquid outlet at the upper part of the flow divider (2) is communicated with a liquid inlet at the top of the absorption tower (1), a liquid outlet at the lower part of the flow divider (2) is communicated with a liquid inlet at the bottom of the desorption tower (7), and a liquid outlet at the bottom of the desorption tower (7) is communicated with a liquid inlet at the top of the absorption tower (1);
the desorption tower (7) is used for separating amine liquid after absorbing carbon dioxide;
the recovery device collects the carbon dioxide separated from the amine liquid.
2. A carbon dioxide collection system as recited in claim 1, wherein:
the device further comprises a lean and rich liquid heat exchanger (3), wherein a first liquid inlet of the lean and rich liquid heat exchanger (3) is communicated with an upper liquid outlet of the flow divider (2), a first liquid outlet of the lean and rich liquid heat exchanger (3) is communicated with a liquid inlet at the top of the absorption tower (1) through a pipeline, and a lean liquid pump (6) is arranged on the pipeline;
the second liquid inlet of the lean-rich liquid heat exchanger (3) is communicated with the lower liquid outlet of the flow divider (2), the second liquid outlet of the lean-rich liquid heat exchanger (3) is communicated with the first liquid inlet of the desorption tower (7) through a pipeline, and a rich liquid pump (5) is arranged on the pipeline.
3. A carbon dioxide collection system as recited in claim 2, wherein: the evaporator further comprises an evaporation tank (4) which comprises a first liquid inlet, a second liquid inlet and a liquid outlet, wherein the first liquid inlet is communicated with the upper liquid outlet of the flow divider (2), and the second liquid inlet is communicated with the first liquid outlet of the desorption tower (7);
the liquid outlet of the evaporation tank (4) is communicated with the first liquid inlet of the lean-rich liquid heat exchanger (3).
4. A carbon dioxide collection system as recited in claim 3, wherein: still include reboiler (8), the inlet intercommunication of reboiler (8) the second liquid outlet of desorber (7) bottom, the liquid outlet intercommunication of reboiler (8) the second liquid inlet of desorber (7), reboiler (8) are by steam generator heat supply.
5. A carbon dioxide collection system as recited in claim 1, wherein: the inside of the absorption tower (1) is divided into three layers along the axial direction, and heat exchange pipelines are arranged between each two layers.
6. A carbon dioxide collection system as recited in claim 1, wherein: the recovery device comprises a heat exchanger (9), a gas-liquid separator (10) and a compression fan (11) which are sequentially communicated;
the air inlet of the heat exchanger (9) is communicated with the top air outlet of the desorption tower (7), the outlet of the heat exchanger (9) is communicated with the air inlet of the gas-liquid separator (10), the top air outlet of the gas-liquid separator (10) is communicated with the compression fan (11), and the bottom liquid outlet of the gas-liquid separator (10) is communicated with the third liquid inlet of the desorption tower (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320468646.7U CN219630976U (en) | 2023-03-10 | 2023-03-10 | Carbon dioxide collecting system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320468646.7U CN219630976U (en) | 2023-03-10 | 2023-03-10 | Carbon dioxide collecting system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219630976U true CN219630976U (en) | 2023-09-05 |
Family
ID=87815896
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320468646.7U Active CN219630976U (en) | 2023-03-10 | 2023-03-10 | Carbon dioxide collecting system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219630976U (en) |
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2023
- 2023-03-10 CN CN202320468646.7U patent/CN219630976U/en active Active
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