CN202605989U - Carbon dioxide capture and regeneration device - Google Patents
Carbon dioxide capture and regeneration device Download PDFInfo
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- CN202605989U CN202605989U CN2012202687429U CN201220268742U CN202605989U CN 202605989 U CN202605989 U CN 202605989U CN 2012202687429 U CN2012202687429 U CN 2012202687429U CN 201220268742 U CN201220268742 U CN 201220268742U CN 202605989 U CN202605989 U CN 202605989U
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The utility model discloses a carbon dioxide capture and regeneration device, which comprises an absorption device, wherein the absorption device is provided with two outputs, one output is communicated with a rich solution inlet of a rich and lean solution heat exchanger, and the other output is communicated with a first inlet of a regeneration tower; a rich solution inlet of a rich solution flash tank is communicated with a rich solution outlet of the rich and lean solution heat exchanger; a rich solution outlet of the rich solution flash tank is communicated with a second inlet of the regeneration tower; a lean solution outlet at the bottom of the regeneration tower is communicated with a lean solution inlet of the rich and lean solution heat exchanger; a gas outlet at the top of the regeneration tower is communicated with a gas outlet at the top of the rich solution flash tank and further communicated with a gas inlet of a regeneration gas separation device; and a liquid outlet of the regeneration gas separation device is communicated with a lean solution outlet of the rich and lean solution heat exchanger and further communicated with an inlet of the absorption device. The carbon dioxide capture and regeneration device improves the desorption rate of the carbon dioxide and the regeneration degree of a solution, and lowers the temperature of a lean solution entering the absorption device, thereby improving the carbon dioxide capture efficiency of the lean solution.
Description
Technical field
The utility model relates to flue gas collecting carbonic anhydride technical field, is specifically related to a kind of collecting carbonic anhydride regenerating unit.
Background technology
In recent years, the pressure that global warming brings for government and energy enterprise increases rapidly, and a lot of western countries have begun to promote substantial decarburization work.Along with the reinforcement of China's carbon emission amount above the U.S. and the international cry that reduces discharging, power plant's collecting carbonic anhydride probably becomes required technology China's a middle or short term.China is thermal power generation more than 3/4 in the existing power station, does not also have commercial off-the-shelf IGCC power station now.So exploitation is fit to the pure amine absorption process of traditional power plant and catches carbon technique, is the most urgent demand.
The technology of utilizing alkanolamine solution from flue gas, to carry out collecting carbonic anhydride is ripe in chemical industry.But, because that generating plant flue gas has is large-minded, divide characteristics such as force down, it is that energy consumption is high that this technology applies to the maximum problem in power station, steam consumption is big.Reduce consumption, raise the efficiency, the large-scale promotion property that need improve this technology through the system and the subsystem of development of new.
Experimental study finds that for traditional collecting carbonic anhydride technology, solution can consume a large amount of steam in regenerative process; Cause system energy consumption big; And because regeneration is single, influence carbon dioxide desorb degree, 40% the carbon dioxide of still having an appointment can not get discharging and along with solution entering absorption tower; Cause the solution absorption ability not enough, reduced the capture load of carbon dioxide and the capture steam consumption of unit carbon dioxide on the whole.Simultaneously, purifying gas is being sent into regeneration overhead through the liquid after often will separating through high lift pump after the gas-liquid separation in the traditional handicraft, and its effect is to keep systematic water balance, reduces tower top temperature simultaneously, but has consumed more pump merit.
Summary of the invention
In order to overcome the shortcoming that above-mentioned prior art exists; The purpose of the utility model is to provide a kind of collecting carbonic anhydride regenerating unit; Have the advantages that the cooling effect that makes full use of before the rich solution heat exchange and the carbon dioxide in the solution after the heat exchange are prone to separate out; Improve the desorption efficiency of carbon dioxide and the regeneration degree of solution, reduce getting into absorption plant lean solution temperature, improve the collecting carbonic anhydride efficient of lean solution.
In order to achieve the above object, the utility model adopts following technical scheme:
A kind of collecting carbonic anhydride regenerating unit; Comprise absorption plant 5; The output of absorption plant 5 is divided into two-way; One the tunnel is communicated with the rich solution entrance pipe of poor rich liquid heat exchanger 1, and first entrance pipe of another road and regenerator 3 is communicated with, and rich solution flash tank 2 rich solutions enter the mouth and are communicated with poor rich liquid heat exchanger 1 rich solution export pipeline; Second entrance pipe of outlet of rich solution flash tank 2 rich solutions and regenerator 3 is communicated with; The outlet of regenerator 3 bottom lean solutions is communicated with poor rich liquid heat exchanger 1 lean solution inlet ductwork, and the outlet of regenerator 3 top gas is communicated with the gas access pipeline of regeneration gas separator 4 after outlet is communicated with rich solution flash tank 2 top gas again, and the lean solution of the liquid outlet of regeneration gas separator 4 and poor rich liquid heat exchanger 1 exports after the connection entrance pipe connection with absorption plant 5 again.
Said poor rich liquid heat exchanger 1 is board-like or shell-and-tube liquid-liquid heat exchanger.
Said regenerator 3 is filler or plate tower.
Compared with prior art, the utlity model has following advantage:
1, from the rich solution separated into two parts of absorption plant 5, wherein a road of flow directly gets into regenerator 3 tops, because this rich solution does not pass through heat exchange; Temperature is about 50～60 ℃; Can reduce tower top temperature after getting into regenerator 3 tops, reduce water evaporates, simultaneously because this part rich solution amount is less from tower; Also can make full use of the cat head waste heat and realize fully regeneration, resolve carbon dioxide.
2, another part rich solution then fully reclaims the heat of lean solution through poor rich liquid heat exchanger 1;, entering regenerator 3 at first passes through rich solution flash tank 2 before carrying out solution regeneration; The heat that utilize the to reclaim partial CO 2 gas of in rich solution flash tank 2, regenerating; The carbon dioxide that this part parses directly converges the back discharge with the regeneration gas that regenerator 3 ejects mouthful; Reduce the partial pressure of carbon dioxide in the regenerator 3, helped the further parsing of the carbon dioxide of solution, improved the desorption efficiency of carbon dioxide and the regeneration degree of solution.
3, further regeneration in the regenerator 3 of the rich solution of partial regeneration entering in rich solution flash tank 2.
4, after the process of the gas after regeneration regeneration gas separator 4 refrigerated separation, liquid mixes with lean solution with the lean solution outlet of poor rich liquid heat exchanger 1 through the gravity flow mode, sends into absorption plant 5 subsequently; Both solved owing to the part rich solution directly gets into rich solution flash tank 2 and caused the not enough problem of poor rich liquid heat exchanger 1 cooling load, also further reduced the lean solution temperature, improved the collecting carbonic anhydride efficient of lean solution in absorption plant; Reduced simultaneously and will separate the pump merit that back liquid is sent into regenerator 3 tops.
Description of drawings
Accompanying drawing is the structural representation of the utility model.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is done more detailed explanation.
Shown in accompanying drawing; A kind of collecting carbonic anhydride regenerating unit; Comprise absorption plant 5, the output of absorption plant 5 is divided into two-way, and one the tunnel is communicated with the rich solution entrance pipe of poor rich liquid heat exchanger 1; First entrance pipe of another road and regenerator 3 is communicated with; Rich solution flash tank 2 rich solutions inlet is communicated with poor rich liquid heat exchanger 1 rich solution export pipeline, and second entrance pipe of outlet of rich solution flash tank 2 rich solutions and regenerator 3 is communicated with, and regenerator 3 bottom lean solution outlets and poor rich liquid heat exchanger 1 lean solution inlet ductwork are communicated with; Regenerator 3 top gas outlets is communicated with the gas access pipeline of regeneration gas separator 4 after outlet is communicated with rich solution flash tank 2 top gas again, after the lean solution outlet connection of the liquid outlet of regeneration gas separator 4 and poor rich liquid heat exchanger 1 again with the entrance pipe connection of absorption plant 5.
Said poor rich liquid heat exchanger 1 is board-like or shell-and-tube liquid-liquid heat exchanger.
Said regenerator 3 is filler or plate tower.
The operation principle of the utility model does;
From the rich solution separated into two parts of absorption plant 5, wherein one the tunnel directly get into regenerator 3 tops, because this rich solution does not pass through heat exchange; Temperature is about 50～60 ℃, and the entering regenerator can reduce tower top temperature behind 3 tops, reduces water evaporates from tower; Simultaneously because this part rich solution amount is less; Also can make full use of the cat head waste heat and realize fully regeneration, resolve carbon dioxide, another part rich solution then fully reclaims the heat of lean solution through poor rich liquid heat exchanger 1;, entering regenerator 3 at first passes through rich solution flash tank 2 before carrying out solution regeneration; The regeneration gas that the heat that utilize the to reclaim partial CO 2 gas of in rich solution flash tank 2, regenerating, the carbon dioxide that this part parses directly eject mouthful with regenerator 3 converges the back and discharges, and reduced the interior partial pressure of carbon dioxide of regenerator 3.The rich solution of partial regeneration gets into further regeneration in the regenerator 3 in rich solution flash tank 2.At last, after gas process regeneration gas separator 4 refrigerated separation after the regeneration, the lean solution outlet that liquid is admitted to poor rich liquid heat exchanger 1 mixes with lean solution, sends into absorption plant 5 subsequently; Both solved owing to the part rich solution directly gets into rich solution flash tank 2 and caused the not enough problem of poor rich liquid heat exchanger 1 cooling load, also further reduced the lean solution temperature, improved the collecting carbonic anhydride efficient of lean solution in absorption plant.
Claims (3)
1. collecting carbonic anhydride regenerating unit; Comprise absorption plant (5); It is characterized in that: the output of absorption plant (5) is divided into two-way; One the road and the rich solution entrance pipe of poor rich liquid heat exchanger (1) be communicated with; First entrance pipe of another road and regenerator (3) is communicated with; Rich solution flash tank (2) rich solution inlet is communicated with poor rich liquid heat exchanger (1) rich solution export pipeline, and second entrance pipe of outlet of rich solution flash tank (2) rich solution and regenerator (3) is communicated with, and lean solution outlet of regenerator (3) bottom and poor rich liquid heat exchanger (1) lean solution inlet ductwork are communicated with; Regenerator (3) top gas outlet is communicated with the gas access pipeline of regeneration gas separator (4) after outlet is communicated with rich solution flash tank (2) top gas again, after the lean solution outlet connection of the liquid outlet of regeneration gas separator (4) and poor rich liquid heat exchanger (1) again and the connection of the entrance pipe of absorption plant (5).
2. a kind of collecting carbonic anhydride regenerating unit according to claim 1 is characterized in that: said poor rich liquid heat exchanger (1) is board-like or shell-and-tube liquid-liquid heat exchanger.
3. a kind of collecting carbonic anhydride regenerating unit according to claim 1 is characterized in that: said regenerator (3) is filler or plate tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202687429U CN202605989U (en) | 2012-06-07 | 2012-06-07 | Carbon dioxide capture and regeneration device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202687429U CN202605989U (en) | 2012-06-07 | 2012-06-07 | Carbon dioxide capture and regeneration device |
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| Publication Number | Publication Date |
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| CN202605989U true CN202605989U (en) | 2012-12-19 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2012202687429U Expired - Lifetime CN202605989U (en) | 2012-06-07 | 2012-06-07 | Carbon dioxide capture and regeneration device |
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| CN (1) | CN202605989U (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102698568A (en) * | 2012-06-07 | 2012-10-03 | 中国华能集团清洁能源技术研究院有限公司 | Enhanced cooling and multistage regeneration carbon dioxide capture and regeneration system |
| CN103266230A (en) * | 2013-05-08 | 2013-08-28 | 北京神雾环境能源科技集团股份有限公司 | Vanadium-containing stone coal shaft furnace oxygen-rich roasting system and method thereof |
| CN103480244A (en) * | 2013-09-27 | 2014-01-01 | 南京华基塔业有限公司 | Large CO2 regeneration tower with novel structure |
| CN103961979A (en) * | 2014-04-28 | 2014-08-06 | 中国华能集团清洁能源技术研究院有限公司 | Multistage division regenerative carbon dioxide trapping system and technology |
| CN106693621A (en) * | 2017-01-19 | 2017-05-24 | 东南大学 | Device and method for efficiently separating and purifying carbon dioxide and helium |
| CN111672280A (en) * | 2020-05-20 | 2020-09-18 | 西安交通大学 | Solar-driven carbon dioxide capturing tower and operation method thereof |
| CN114669177A (en) * | 2022-03-09 | 2022-06-28 | 中国矿业大学 | Low-energy-consumption CO2Trapping and compression refining process |
| WO2024001062A1 (en) * | 2022-07-01 | 2024-01-04 | 中国石油天然气集团有限公司 | Carbon dioxide capture method and apparatus |
-
2012
- 2012-06-07 CN CN2012202687429U patent/CN202605989U/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102698568A (en) * | 2012-06-07 | 2012-10-03 | 中国华能集团清洁能源技术研究院有限公司 | Enhanced cooling and multistage regeneration carbon dioxide capture and regeneration system |
| CN103266230A (en) * | 2013-05-08 | 2013-08-28 | 北京神雾环境能源科技集团股份有限公司 | Vanadium-containing stone coal shaft furnace oxygen-rich roasting system and method thereof |
| CN103266230B (en) * | 2013-05-08 | 2015-04-22 | 北京神雾环境能源科技集团股份有限公司 | Vanadium-containing stone coal shaft furnace oxygen-rich roasting system and method thereof |
| CN103480244A (en) * | 2013-09-27 | 2014-01-01 | 南京华基塔业有限公司 | Large CO2 regeneration tower with novel structure |
| CN103480244B (en) * | 2013-09-27 | 2015-03-25 | 南京华基塔业有限公司 | Large CO2 regeneration tower with novel structure |
| CN103961979A (en) * | 2014-04-28 | 2014-08-06 | 中国华能集团清洁能源技术研究院有限公司 | Multistage division regenerative carbon dioxide trapping system and technology |
| CN106693621A (en) * | 2017-01-19 | 2017-05-24 | 东南大学 | Device and method for efficiently separating and purifying carbon dioxide and helium |
| CN111672280A (en) * | 2020-05-20 | 2020-09-18 | 西安交通大学 | Solar-driven carbon dioxide capturing tower and operation method thereof |
| CN114669177A (en) * | 2022-03-09 | 2022-06-28 | 中国矿业大学 | Low-energy-consumption CO2Trapping and compression refining process |
| CN114669177B (en) * | 2022-03-09 | 2024-01-26 | 中国矿业大学 | Low-energy-consumption CO 2 Trapping and compression refining process |
| WO2024001062A1 (en) * | 2022-07-01 | 2024-01-04 | 中国石油天然气集团有限公司 | Carbon dioxide capture method and apparatus |
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Granted publication date: 20121219 |