CN212166984U - CO2Trapping system - Google Patents
CO2Trapping system Download PDFInfo
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- CN212166984U CN212166984U CN202020449456.7U CN202020449456U CN212166984U CN 212166984 U CN212166984 U CN 212166984U CN 202020449456 U CN202020449456 U CN 202020449456U CN 212166984 U CN212166984 U CN 212166984U
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- 230000008929 regeneration Effects 0.000 claims abstract description 115
- 238000011069 regeneration method Methods 0.000 claims abstract description 115
- 238000010521 absorption reaction Methods 0.000 claims abstract description 69
- 239000007788 liquid Substances 0.000 claims abstract description 68
- 239000007789 gas Substances 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 52
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 39
- 239000003546 flue gas Substances 0.000 claims description 38
- 238000005406 washing Methods 0.000 claims description 24
- 230000001172 regenerating effect Effects 0.000 claims description 18
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 239000004568 cement Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 239000002912 waste gas Substances 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 16
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 10
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 10
- 239000012535 impurity Substances 0.000 description 8
- 230000002745 absorbent Effects 0.000 description 7
- 239000002250 absorbent Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 150000001412 amines Chemical class 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 229940058020 2-amino-2-methyl-1-propanol Drugs 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 2
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
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Abstract
The utility model provides a CO2The trapping system comprises an absorption tower, a regeneration heat exchanger and a lean-rich liquid heat exchanger, wherein a rich liquid outlet of the absorption tower is connected with a cold source inlet of the regeneration heat exchanger, a cold source outlet of the regeneration heat exchanger is connected with a cold source inlet of the lean-rich liquid heat exchanger, and a cold source outlet of the lean-rich liquid heat exchanger is connected with a rich liquid inlet of the regeneration tower; a regeneration mixed gas outlet of the regeneration tower is connected with a heat source inlet of the regeneration heat exchanger; and a barren solution outlet of the regeneration tower is connected with a heat source inlet of the barren and rich solution heat exchanger, and a heat source outlet of the barren and rich solution heat exchanger is connected with a regeneration barren solution inlet of the absorption tower. Compared with the prior artCompared with the prior art, the CO2The capture system can efficiently recover the latent heat of the regeneration gas and the sensible heat of the regeneration barren solution in the regeneration tower, effectively reduce the consumption of the regeneration steam, reduce the regeneration energy consumption of the system, and can be used for large-scale CO of flue waste gas of coal-fired power plants, chemical plants and cement plants2Trapping and has good application prospect.
Description
Technical Field
The utility model relates to a solvent absorbed gas and solvent regeneration technical field especially relate to a CO2A capture system.
Background
Carbon dioxide capture and sequestration (CCS) technology is currently one of the most effective means to achieve large-scale carbon abatement. Wherein, CO is obtained by solvent method2The trapping technology has the advantages of good separation effect, mature and reliable technology and the like, but is used for large-scale CO2Trapping, the cost is higher at present. Therefore, reducing energy consumption to reduce capture cost has become a solvent process CO2Research on trapping technology is hot.
CO2The regeneration heat of the regeneration tower in the capture system is mainly distributed in two parts: the first part is the regenerated barren liquor at the tower bottom of the regeneration tower, and the other part is the regenerated mixed gas at the tower top of the regeneration tower. Conventional CO2The trapping process only simply recovers the heat of the regeneration barren solution at the tower bottom of the regeneration tower, is used for heating the absorption rich solution entering the regeneration tower, does not consider the utilization of the latent heat of the regeneration mixed gas at the tower top of the regeneration tower, and can cause a large amount of energy consumption loss.
SUMMERY OF THE UTILITY MODEL
To overcome the disadvantages of the prior art, an object of the present invention is to provide a CO gas generator2The trapping system can effectively utilize the latent heat of the regenerated mixed gas at the top of the regeneration tower and reduce the energy consumption loss of the system.
The utility model provides a pair of CO2The capture system is provided with an absorption tower and a regeneration tower, and further comprises a regeneration heat exchanger and a lean-rich liquid heat exchanger, a rich liquid outlet at the bottom of the absorption tower is connected with a cold source inlet of the regeneration heat exchanger, and a cold source outlet of the regeneration heat exchanger is connected with the lean-rich liquid heat exchangeA cold source inlet of the device is connected, and a cold source outlet of the lean-rich liquid heat exchanger is connected with a rich liquid inlet at the top of the regeneration tower; a regeneration mixed gas outlet at the top of the regeneration tower is connected with a heat source inlet of the regeneration heat exchanger; and a barren solution outlet at the bottom of the regeneration tower is connected with a heat source inlet of the barren and rich solution heat exchanger, and a heat source outlet of the barren and rich solution heat exchanger is connected with a regeneration barren solution inlet at the top of the absorption tower.
Preferably, the system further comprises a regenerative cooler and a gas-liquid separator, wherein an inlet of the regenerative cooler is connected with a heat source outlet of the regenerative heat exchanger, and an outlet of the regenerative cooler is connected with an inlet of the gas-liquid separator.
Preferably, the liquid phase outlet of the gas-liquid separator is connected with the regeneration condensed water inlet of the regeneration tower.
Preferably, the device further comprises a pretreatment unit, and an outlet of the pretreatment unit is connected with a flue gas inlet of the absorption tower.
Preferably, the absorption tower further comprises a circulating water washing device, and the circulating water washing device is communicated with the top of the absorption tower.
Preferably, the circulation washing device includes washing unit, circulating water pump and circulating water cooler, the washing unit circulating water pump with the circulating water cooler passes through the pipeline and connects gradually and forms closed return circuit.
Compared with the prior art, the utility model provides a CO2The trapping system can efficiently recover the latent heat of the regeneration gas and the sensible heat of the regeneration barren solution in the regeneration tower. The system preheats the absorption rich solution by using the latent heat of the regenerated mixed gas, so that all effective heat of the regenerated gas can be effectively recovered, and the preheated absorption rich solution is secondarily heated by the lean rich solution heat exchanger, so that the temperature of the absorption rich solution entering the regeneration tower is further increased, the consumption of regenerated steam is effectively reduced, and the regeneration energy consumption of the system is greatly reduced. The utility model discloses can be used to the extensive CO of coal fired power plant, chemical plant, cement plant flue waste gas2Trapping and has good application prospect.
The above-mentioned technical characteristics can be combined in various suitable ways or replaced by equivalent technical characteristics as long as the purpose of the invention can be achieved.
Drawings
The invention will be described in more detail hereinafter on the basis of non-limiting examples only and with reference to the accompanying drawings. Wherein:
FIG. 1 shows CO provided by the present invention2The structure of the trapping system is shown schematically.
Description of reference numerals:
1. an induced draft fan; 2. a pre-processing unit; 3. an absorption tower; 4. a water circulating pump; 5. a circulating water cooler; 6. A rich liquor pump; 7. a regeneration gas heat exchanger; 8. a lean-rich liquid heat exchanger; 9. a regeneration tower; 10. a reboiler; 11. a circulating pump of the tower kettle; 12. a regenerative cooler; 13. a gas-liquid separator;
I. flue gas; II. Regenerating the barren solution; III, discharging flue gas; IV, absorbing the rich liquid; v, regenerating mixed gas; VI, CO2Producing gas; VII, regenerating condensed water; VIII, adding circulating water.
Detailed Description
For making the purpose, technical solution and advantages of the present invention clearer, it will be right below that the technical solution of the present invention is clearly and completely described, based on the specific embodiments of the present invention, all other embodiments obtained by the ordinary skilled person in the art without creative work belong to the scope protected by the present invention.
The utility model provides a CO2The trapping system can efficiently recover the latent heat of the regeneration gas and the sensible heat of the regeneration barren solution II in the regeneration system. This system utilizes the latent heat of regeneration gas mixture V to preheat absorption pregnant solution IV earlier, can effectively retrieve whole effective heat of regeneration gas like this, and absorption pregnant solution IV after preheating carries out the secondary heating through lean solution rich solution heat exchanger 8 again for the temperature that absorption pregnant solution IV got into regenerator 9 further improves, and the consumption of regeneration steam has effectively been reduced to this system, greatly reduced regeneration energy consumption.
As shown in FIG. 1, CO is provided in this example2The trapping system mainly comprises an induced draft fan 1, a pretreatment unit 2, an absorption tower 3, a regenerative heat exchanger, a lean rich liquor heat exchanger 8, a regeneration tower 9, a reboiler 10, a regenerative cooler 12 and a gas-liquid separator 13. An outlet of the induced draft fan 1 is connected with an inlet of the pretreatment unit 2, and an outlet of the pretreatment unit 2 is connected with a flue gas inlet of the absorption tower 3; a rich liquid outlet at the bottom of the absorption tower 3 is connected with a cold source inlet of the regeneration heat exchanger, a rich liquid pump 6 is arranged on a connecting pipeline of the absorption tower and the regeneration heat exchanger, and an absorption rich liquid IV discharged from the bottom of the absorption tower 3 is conveyed to a regeneration gas heat exchanger 7 through the rich liquid pump 6; a cold source outlet of the regeneration heat exchanger is connected with a cold source inlet of the lean and rich liquid heat exchanger 8, and a cold source outlet of the lean and rich liquid heat exchanger 8 is connected with a rich liquid inlet at the top of the regeneration tower 9; a regeneration mixed gas V outlet at the top of the regeneration tower 9 is connected with a heat source inlet of the regeneration heat exchanger; a heat source outlet of the regenerative heat exchanger is connected with an inlet of a regenerative cooler 12, an outlet of the regenerative cooler 12 is connected with an inlet of a gas-liquid separator, and a liquid phase outlet of the gas-liquid separator 13 is connected with a regenerative condensate VII inlet at the top of the regeneration tower 9; a barren solution outlet at the bottom of the regeneration tower 9 is connected with a heat source inlet of the barren and rich solution heat exchanger 8, a tower kettle circulating pump 11 is arranged on a connecting pipeline of the barren solution outlet and the rich solution outlet, and a regenerated barren solution II discharged from the bottom of the regeneration tower 9 is conveyed into the barren and rich solution heat exchanger 8 through the tower kettle circulating pump 11; and a heat source outlet of the lean-rich liquid heat exchanger 8 is connected with a regenerated lean liquid II inlet at the top of the absorption tower 3. The reboiler 10 is used for heating the absorption rich liquid IV in the regeneration tower 9 to make the CO in the absorption rich liquid IV2And (4) desorbing.
In order to further reduce the pollution of the discharged flue gas III to the atmosphere, the capture system further comprises a circulating water washing device, wherein the circulating water washing device at least comprises a water washing unit (not shown in the figure) and a circulating water pump 4, and the circulating water washing device is communicated with the top of the absorption tower 3. And the decarbonized flue gas I in the absorption tower 3 enters a circulating water washing device, and organic amine and part of residual gas impurities carried by the flue gas I are removed and then discharged into the atmosphere. Because the water temperature is too high to be unfavorable for removing organic amine and partial residual gas impurities in the flue gas I, the circulating water in the circulating water washing device needs to be cooled, and a circulating water cooler 5 can be additionally arranged, and a water washing unit, a circulating water pump 4 and the circulating water are arrangedThe coolers 5 are sequentially connected through pipelines to form a closed loop, so that cooling and cyclic utilization of circulating water can be realized. The water washing unit can be arranged in the absorption tower 3 or outside the absorption tower 3, in the embodiment, the water washing unit is arranged at the top of the absorption tower 3, the washing liquid obtained after water washing enters the top of the regeneration tower 9 through the circulating water pump 4 and the circulating water cooler 5, and the CO provided by the invention can be kept2The trapping method and the device keep water balance during operation, are favorable for reducing water consumption and the long-term operation of the trapping device, and can also stabilize the concentration of the absorbent in the absorption liquid for a long time.
CO2Capture system for capturing CO2The process flow is as follows:
the method comprises the following steps that flue gas I is introduced into a pretreatment unit 2 through an induced draft fan 1 for pretreatment, sulfur dioxide and partial gas impurities in the flue gas I are removed, and the pretreatment method comprises the following steps: contacting a sodium hydroxide solution with the mass concentration of 5-10% or circulating water with the flue gas I; wherein, CO in the flue gas I2The volume concentration is 8-13%, the concentration of sulfur dioxide in the flue gas I is more than 100ppm, and the concentration of sulfur dioxide in the pretreated flue gas I is less than 1 ppm. The pretreated clean flue gas I enters the absorption tower 3 from the bottom, the absorbent enters the absorption tower 3 from the top and is in countercurrent contact with the flue gas I, and CO in the flue gas I2Trapped in absorbent at 20-50 deg.C and absorption pressure of 1-1.3 bar; the absorbent is one or more of ethanolamine MEA, methyldiethanolamine MDEA, piperazine PZ and sterically hindered amine AMP (2-amino-2-methyl-1-propanol), and the concentration of the absorbent is 5% -50%, preferably 20% -40%. The decarbonized flue gas I continuously goes upward to enter a circulating washing device at the top of the absorption tower 3, and organic amine and part of residual gas impurities carried by the flue gas I are removed and then discharged into the atmosphere. The absorption rich liquid IV coming out from the bottom of the absorption tower 3 is preheated by a regeneration gas heat exchanger 7, and the preheated absorption rich liquid IV enters a regeneration tower 9 after being secondarily heated by a lean rich liquid heat exchanger 8. The absorption rich liquid IV is heated by a reboiler 10 in the regeneration tower 9 to absorb CO in the rich liquid IV2Desorbing at the regeneration temperature of 110-The absorption barren solution after being regenerated at 0.15-0.25MPa is discharged from the bottom of the regeneration tower 9, exchanges heat with the absorption rich solution IV, and then returns to the top of the absorption tower 3 for recycling. In the regeneration column 9, part of the water is vaporized and the CO is desorbed2The product gas VI is mixed into a regenerated mixed gas V, the regenerated mixed gas V is discharged from the top of the regeneration tower 9, exchanges heat with the absorption rich liquid IV through a regenerated gas heat exchanger 7, is cooled through a regeneration cooler 12 and then enters a gas-liquid separator 13, and CO is discharged into a gas-liquid separator2Separating from the top of the gas-liquid separator 13 to obtain a product gas VI; the regenerated condensed water VII is separated from the bottom of the gas-liquid separator 13 and returned to the regeneration tower 9, thereby maintaining the water balance of the system.
The CO provided by the present application will be further illustrated with reference to the following examples2A capture system.
Example 1
The absorbent adopts 30 percent of ethanolamine MEA, and the specific implementation steps are as follows:
1) the flue gas I enters a pretreatment unit 2 from a Flue Gas Desulfurization (FGD) outlet through a draught fan 1 for pretreatment, sulfur dioxide and partial gas impurities are removed, and SO in the flue gas I2The concentration is reduced to below 1 ppm;
2) the clean flue gas I from the pretreatment device enters an absorption tower 3 from the bottom, a 30% ethanolamine MEA solution enters from the top of the absorption tower 3 and is in countercurrent contact with the flue gas I, and CO in the flue gas I2Trapped in a solvent;
3) the decarbonized flue gas I continuously goes upward to enter a circulating washing device at the top of the absorption tower 3, and organic amine carried by the flue gas I and part of residual gas impurities are removed and then discharged into the atmosphere;
4) and the absorption rich liquid IV coming out of the bottom of the absorption tower 3 is conveyed to a regeneration gas heat exchanger 7 through a rich liquid pump 6 for preheating, and then enters the top of a regeneration tower 9 for regeneration after being secondarily heated through a lean rich liquid heat exchanger 8. The CO in the absorption rich liquid IV is heated by a reboiler 10 in a regeneration tower 92Desorbing the solution; in the step, the temperature of the absorption rich liquid IV after being preheated by the regeneration gas heat exchanger 7 is 96 ℃, the temperature of the absorption rich liquid IV after being secondarily heated by the lean and rich liquid heat exchanger 8 is 116 ℃, the regeneration temperature of the regeneration tower 9 is 125 ℃, and the regeneration pressure is 0.2 MPa;
5) in the regeneration column 9, part of the water is vaporised with the desorbed CO2Enters a regeneration gas heat exchanger 7 from the top of a regeneration tower 9 for heat exchange, enters a gas-liquid separator 13 through a regeneration cooler 12, and CO2Separating from the top of the separator to obtain a product gas VI; the regenerated condensed water VII is returned to the regeneration tower 9 to maintain the water balance of the system.
6) The regenerated barren solution II is discharged from the bottom of the regeneration tower 9, exchanges heat with the absorption rich solution IV in the barren rich solution heat exchanger 8 through the tower kettle circulating pump 11, and returns to the top of the absorption tower 3 for recycling.
In this example, CO of flue gas I2The capture rate is 90 percent, and the capture energy consumption is 3.3GJ/tCO2Compared with the traditional process, the regeneration energy consumption can be reduced by 21%.
Example 2
The absorbent adopts 30 percent ethanolamine MEA, and the specific implementation steps are as follows:
1) the flue gas I enters a pretreatment device from a Flue Gas Desulfurization (FGD) outlet through a draught fan 1 for pretreatment, sulfur dioxide and partial gas impurities are removed, and SO in the flue gas I2The concentration is reduced to below 1 ppm;
2) the clean flue gas I from the pretreatment device enters an absorption tower 3 from the bottom, a 30% ethanolamine MEA solution enters from the top of the absorption tower 3 and is in countercurrent contact with the flue gas I, and CO in the flue gas I2Trapped in a solvent;
3) the decarbonized flue gas I continuously goes upward to enter a circulating washing device at the top of the absorption tower 3, and organic amine carried by the flue gas I and part of residual gas impurities are removed and then discharged into the atmosphere;
4) and the absorption rich liquid IV coming out of the bottom of the absorption tower 3 is conveyed to a regeneration gas heat exchanger 7 through a rich liquid pump 6 for preheating, and then enters the top of a regeneration tower 9 for regeneration after being secondarily heated through a lean rich liquid heat exchanger 8. The CO in the absorption rich liquid IV is heated by a reboiler 10 in a regeneration tower 92Desorbing the solution;
in the step, the temperature of the absorption rich liquid IV after being preheated by the regeneration gas heat exchanger 7 is 89 ℃, the temperature of the absorption rich liquid IV after being secondarily heated by the lean rich liquid heat exchanger 8 is 108 ℃, the regeneration temperature of the regeneration tower 9 is 115 ℃, and the regeneration pressure is 0.15 MPa;
5) in the regeneration column 9, part of the water is vaporised with the desorbed CO2Enters a regeneration gas heat exchanger 7 from the top of a regeneration tower 9 for heat exchange, enters a gas-liquid separator 13 through a regeneration cooler 12, and CO2Separating from the top of the separator to obtain a product gas VI; the regenerated condensed water VII is returned to the regeneration tower 9 to maintain the water balance of the system.
6) The regenerated barren solution II is discharged from the bottom of the regeneration tower 9, exchanges heat with the absorption rich solution IV in the barren rich solution heat exchanger 8 through the tower kettle circulating pump 11, and returns to the top of the absorption tower 3 for recycling.
In this example, CO of flue gas I2The capture rate is 90 percent, and the capture energy consumption is 3.8GJ/tCO2Compared with the traditional process, the regeneration energy consumption can be reduced by 10%.
Finally, it should be noted that: the above embodiments and examples are only used to illustrate the technical solution of the present invention, but not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments and examples, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments or examples may still be modified, or some of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the embodiments or examples of the present invention.
Claims (6)
1. CO (carbon monoxide)2The trapping system is provided with an absorption tower and a regeneration tower and is characterized by further comprising a regeneration heat exchanger and a lean-rich liquid heat exchanger, wherein a rich liquid outlet at the bottom of the absorption tower is connected with a cold source inlet of the regeneration heat exchanger, a cold source outlet of the regeneration heat exchanger is connected with a cold source inlet of the lean-rich liquid heat exchanger, and a cold source outlet of the lean-rich liquid heat exchanger is connected with a rich liquid inlet at the top of the regeneration tower; a regeneration mixed gas outlet at the top of the regeneration tower is connected with a heat source inlet of the regeneration heat exchanger; a barren solution outlet at the bottom of the regeneration tower and a heat source of the barren and rich solution heat exchangerThe heat source outlet of the lean-rich liquid heat exchanger is connected with the regenerated lean liquid inlet at the top of the absorption tower.
2. CO according to claim 12The trapping system is characterized by further comprising a regenerative cooler and a gas-liquid separator, wherein an inlet of the regenerative cooler is connected with a heat source outlet of the regenerative heat exchanger, and an outlet of the regenerative cooler is connected with an inlet of the gas-liquid separator.
3. CO according to claim 22The trapping system is characterized in that a liquid phase outlet of the gas-liquid separator is connected with a regeneration condensed water inlet of the regeneration tower.
4. CO according to claim 12The capture system is characterized by further comprising a pretreatment unit, wherein the outlet of the pretreatment unit is connected with the flue gas inlet of the absorption tower.
5. CO according to claim 12The capture system is characterized by further comprising a circulating water washing device, wherein the circulating water washing device is communicated with the top of the absorption tower.
6. CO according to claim 52The capture system is characterized in that the circulating water washing device comprises a water washing unit, a circulating water pump and a circulating water cooler, wherein the water washing unit, the circulating water pump and the circulating water cooler are sequentially connected through a pipeline to form a closed loop.
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| CN202020449456.7U CN212166984U (en) | 2020-03-31 | 2020-03-31 | CO2Trapping system |
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| CN202020449456.7U CN212166984U (en) | 2020-03-31 | 2020-03-31 | CO2Trapping system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114713003A (en) * | 2022-04-15 | 2022-07-08 | 江苏大学 | Method for utilizing heat in power plant flue gas CO2 capturing process based on chemical absorption method |
| CN115212708A (en) * | 2022-07-15 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Low-cost organic amine method flue gas carbon dioxide capture system and capture method thereof |
| CN115212709A (en) * | 2022-07-16 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Chemical method flue gas carbon dioxide capture system and capture method thereof |
| CN116747696A (en) * | 2023-07-12 | 2023-09-15 | 合肥万豪能源设备有限责任公司 | Carbon trapping system with waste heat recovery device |
-
2020
- 2020-03-31 CN CN202020449456.7U patent/CN212166984U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114713003A (en) * | 2022-04-15 | 2022-07-08 | 江苏大学 | Method for utilizing heat in power plant flue gas CO2 capturing process based on chemical absorption method |
| CN115212708A (en) * | 2022-07-15 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Low-cost organic amine method flue gas carbon dioxide capture system and capture method thereof |
| CN115212709A (en) * | 2022-07-16 | 2022-10-21 | 碳索(杭州)能源环境科技有限公司 | Chemical method flue gas carbon dioxide capture system and capture method thereof |
| CN116747696A (en) * | 2023-07-12 | 2023-09-15 | 合肥万豪能源设备有限责任公司 | Carbon trapping system with waste heat recovery device |
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