CN104399356B - A kind of carbon dioxide capture system - Google Patents
A kind of carbon dioxide capture system Download PDFInfo
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- CN104399356B CN104399356B CN201410637130.6A CN201410637130A CN104399356B CN 104399356 B CN104399356 B CN 104399356B CN 201410637130 A CN201410637130 A CN 201410637130A CN 104399356 B CN104399356 B CN 104399356B
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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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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
A kind of carbon dioxide capture system, heat pump is combined with carbon dioxide capture system, make full use of low-pressure steam heat, rich solution at the bottom of regenerator column is carried out after a heat release by rich solution reheater rich solution reheating by low-pressure steam, steam cooling fluid after heat release again is collected into condensation water tank, the vapor condensation water out of condensation water tank is connected with heat pump set one hot junction, again lean pump outlet is connected with heat pump set one cold junction, utilize heat pump set one heating steam water of condensation while lowering the temperature to lean solution, the hot junction outlet of heat pump set one again cold junction with heat pump set two be connected, the hot junction of heat pump set two is connected with bottom regenerator column, desorb rich solution is taken with the heat in heat pump set two hot junction, the present invention makes the tow taste heat of steam condensate efficiently be utilized, and the demand of low-pressure steam and the cooling load of lean solution can be reduced, reach rich solution desorb degree to increase, the object that the overall energy consumption of carbon dioxide capture system reduces.
Description
Technical field
The invention belongs to flue gases purification field, it is particularly useful for lower concentration CO in the flue gas of the generations such as coal firing boiler, internal combustion turbine and Industrial Stoves2Trapping, in particular to a kind of carbon dioxide capture system.
Background technology
Global climate change problem is increasingly serious, has become one of principal element of threat human kind sustainable development, cuts down the focus that greenhouse gas emission becomes current international community concern with mitigation of climate change. Correlative study shows, the Carbon emission of China more than 50% comes from the thermal power generation of coal-burning power plant. Coal-fired plant flue gas quantity discharged is big, and Relatively centralized, is one of the important channel of carbon dioxide discharge-reduction based on the carbon trapping technique of coal-burning power plant's exploitation.
Utilizing alkanolamine solution to carry out the technology of collecting carbonic anhydride from flue gas ripe in chemical industry industry, similar technology has launched multiple demonstration in coal-burning power plant. But, owing to generating plant flue gas has large-minded, the feature such as point force down, this Technology application problem maximum in power station is energy consumption height, and steam consumption is big. Reduce energy expenditure, it is to increase efficiency, it is necessary to cut operating costs by the carbon trapping system of development of new and subsystem, it is to increase the large-scale promotion of this technology.
Experimental study finds, for traditional collecting carbonic anhydride technology, carbonic acid gas is in regenerative process, owing to regeneration is thorough, have an appointment 40% carbonic acid gas can not get release and enter absorption tower along with solution, cause solution receptivity inadequate, to ensure identical carbonic acid gas output, solution circulated amount and steam consumption must be increased, not only increase the trapping steam hear rate that electricity consumption also add unit carbonic acid gas, cause the overall energy consumption of service system big; Meanwhile, prior art steam is to a solution only heat release, and heat utilizes insufficient, and is not used by the tow taste heat of part water coolant after high temperature heat exchange, is also one of reason that system energy consumption is higher.
Summary of the invention
In order to overcome the shortcoming that above-mentioned prior art exists, it is an object of the invention to provide a kind of carbon dioxide capture system, this system can be used for fire coal, gas-fired station stack gas and the trapping of chemical field low fractional pressure carbon dioxide, optimize the technique of hydramine absorption process capturing carbon dioxide, there is the tow taste heat after making full use of a steam heat release, regeneration of waste liquor is abundant, the features such as system energy consumption is low.
In order to achieve the above object, the present invention is by the following technical solutions:
A kind of carbon dioxide capture system, comprise the absorption tower 2 being connected with flue gas flow variable valve 1, through rich solution pump 3 bottom absorption tower 2, rich liquid stream adjustable valve 4, poor rich liquid heat exchanger 5, rich solution reheater 6, it is connected with rich solution flash tank 7, the pneumatic outlet at rich solution flash tank 7 top is connected with regenerator column 9 upper end, the rich solution of rich solution flash tank 7 times ends is connected with packing section on regenerator column 9, resurgent gases is connected with resurgent gases cooling heat exchanger 10 one end by regenerator column 9 top vent, resurgent gases cooling heat exchanger 10 the other end is connected resurgent gases separating tank 11, resurgent gases separating tank 11 top gas exports workshop section of liquefying with follow-up gas compression and is connected.
It is provided with reboiler 8 bottom described regenerator column 9, the steam-in of reboiler 8 is connected with the low-pressure steam from steam pipe system, the outlet of reboiler 8 is connected with the steam cooling vapour/liquid entrance of rich solution reheater 6, and the steam cooling liquid outlet of rich solution reheater 6 is connected with condensation water tank 17.
Described condensation water tank 17 condensate outlet is connected with heat pump set 1 hot-side inlet, the outlet of heat pump set 1 hot junction is connected heat pump set 2 12 cold junction entrance and is connected, heat pump set 2 12 cold side outlet is connected steam condensate pipe network, and heat pump set 2 12 hot junction is connected with bottom regenerator column 9.
Lean solution outlet bottom described regenerator column 9 is connected with the lean solution entrance pipe of poor rich liquid heat exchanger 5, the lean solution outlet of poor rich liquid heat exchanger 5 is connected with lean pump 13, lean pump 13 is exported and is connected with heat pump set 1 cold junction entrance by lean solution flow control valve 14, and heat pump set 1 cold side outlet is connected with absorption tower 2 lean solution entrance through lean solution water cooler 15.
Described heat pump set 1 is absorption heat pump with heat pump set 2 12.
Compared with prior art, heat pump is combined by the present invention with carbon dioxide capture system, make full use of low-pressure steam heat, rich solution at the bottom of regenerator column is carried out after a heat release by rich solution reheater rich solution reheating by low-pressure steam, steam cooling fluid after heat release again is collected into condensation water tank, the vapor condensation water out of condensation water tank is connected with heat pump set one hot junction, again lean pump outlet is connected with heat pump set one cold junction, utilize heat pump set one heating steam water of condensation while lowering the temperature to lean solution, the hot junction outlet of heat pump set one again cold junction with heat pump set two be connected, the hot junction of heat pump set two is connected with bottom regenerator column, desorb rich solution is taken with the heat in heat pump set two hot junction, the tow taste heat of steam condensate is efficiently utilized, and the demand of low-pressure steam and the cooling load of lean solution can be reduced, reach rich solution desorb degree to increase, the object that the overall energy consumption of carbon dioxide capture system reduces.
Accompanying drawing explanation
Accompanying drawing is the structural representation of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be described in more detail.
With reference to accompanying drawing, a kind of carbon dioxide capture system, comprise the absorption tower 2 being connected with flue gas flow variable valve 1, through rich solution pump 3 bottom absorption tower 2, rich liquid stream adjustable valve 4, poor rich liquid heat exchanger 5, rich solution reheater 6, it is connected with rich solution flash tank 7, by absorption tower 2 rich solution out through rich solution pump 3 rich solution, through flow control valve 4 again by poor rich liquid heat exchanger 5 heat exchange, rich solution reheater 6 reheating, finally enter rich solution flash tank 7, the pneumatic outlet at rich solution flash tank 7 top is connected with regenerator column 9 upper end, the rich solution of rich solution flash tank 7 times ends is connected with packing section on regenerator column 9, resurgent gases is connected with resurgent gases cooling heat exchanger 10 one end by regenerator column 9 top vent, resurgent gases cooling heat exchanger 10 the other end is connected resurgent gases separating tank 11, the resurgent gases that regenerator column 9 produces is discharged by regenerator column 9 top and is connected with resurgent gases cooling heat exchanger 10, gas enters resurgent gases separating tank 11 after heat exchange, resurgent gases separating tank 11 top gas exports workshop section of liquefying with follow-up gas compression and is connected.
It is provided with reboiler 8 bottom described regenerator column 9, the steam-in of reboiler 8 is connected with the low-pressure steam from steam pipe system, the outlet of reboiler 8 is connected with the steam cooling vapour/liquid entrance of rich solution reheater 6, and the steam cooling liquid outlet of rich solution reheater 6 is connected with condensation water tank 17.
Described condensation water tank 17 condensate outlet is connected with heat pump set 1 hot-side inlet, the outlet of heat pump set 1 hot junction is connected heat pump set 2 12 cold junction entrance and is connected, heat pump set 2 12 cold side outlet is connected steam condensate pipe network, and heat pump set 2 12 hot junction is connected with bottom regenerator column 9. Phlegma returns steam condensate pipe network again after heat pump set 1 after heat pump set 2 12 cold junction heat release, and heat pump set 2 12 hot junction is connected with bottom regenerator column 9.
Lean solution outlet bottom described regenerator column 9 is connected with the lean solution entrance pipe of poor rich liquid heat exchanger 5, the lean solution outlet of poor rich liquid heat exchanger 5 is connected with lean pump 13, lean pump 13 is exported and is connected with heat pump set 1 cold junction entrance by lean solution flow control valve 14, heat pump set 1 cold side outlet is connected with absorption tower 2 lean solution entrance through lean solution water cooler 15, and the lean solution after heat release enters absorption tower 2 lean solution entrance again after lean solution water cooler 15 heat exchange.
Described heat pump set 1 is absorption heat pump with heat pump set 2 12.
The technological process of the present invention and principle be:
Neat stress after desulphurization denitration regulates flow to enter absorption tower 2 by flue gas flow variable valve 1, flue gas drenches and lower absorption agent formation counter current contact with spray, the rich solution absorbing carbonic acid gas carries out reheating from entering rich solution reheater 6 after rich solution pump 3 dozens to poor rich liquid heat exchanger 5 and lean solution heat exchange bottom absorption tower 2, enter rich solution flash tank 7 again and reclaim heat, the outlet of rich solution flash tank 7 top gas is connected with regenerator column 9 top, together lower the temperature through re-generatively cooled interchanger 10 heat exchange with the resurgent gases at regenerator column 9 top, after resurgent gases separating tank 11 gas-liquid separation, finished product carbon dioxide gas enter subsequent compression liquefaction workshop section, rich solution bottom rich solution flash tank 7 enters regenerator column packing section upper end and carries out desorption and regeneration.
Bottom absorption tower 2, rich solution after absorbing carbon dioxide enters rich solution flash tank 7 recovered energy again through poor rich liquid heat exchanger 5 after rich solution reheater 6 reheating, rich solution flash tank 7 rich bottoms liquid enters regenerator column regeneration from regenerator column 9 packing section upper end, gas fraction enters regenerator column 9 top from rich solution flash tank 7 top and regenerator column 9 top resurgent gases is together lowered the temperature through re-generatively cooled interchanger 10 heat exchange, after resurgent gases separating tank 11 gas-liquid separation, finished product carbon dioxide gas enter subsequent compression liquefaction workshop section.
Lean solution bottom regenerator column 9 enters heat pump set 1 cold junction heat release through lean pump 13 after going to poor rich liquid heat exchanger 5 and rich solution heat exchange, then enters packing section upper end, absorption tower 2 after lean solution cooling heat exchanger 15 heat exchange, carries out carbon dioxide absorption.
Condensation water tank 17 condensate outlet is connected with heat pump set 1 hot junction, condensation water tank 17 is returned again after heat pump set 2 12 cold junction heat release, heat pump set 2 12 hot junction is connected with bottom regenerator column 9, utilize heat pump set 1 that lean solution is lowered the temperature, and make steam condensate be warming up to about 95 DEG C, recycling heat pump set two makes steam condensate release of heat, makes heat pump set two hot junction working medium be warming up to about 120 DEG C, thus reaches the object with heat pump set two hot junction working medium heat desorb rich solution.
Claims (2)
1. a carbon dioxide capture system, it is characterized in that, comprise the absorption tower (2) being connected with flue gas flow variable valve (1), through rich solution pump (3) bottom absorption tower 2, rich liquid stream adjustable valve (4), poor rich liquid heat exchanger (5), rich solution reheater (6), it is connected with rich solution flash tank (7), the pneumatic outlet at rich solution flash tank (7) top is connected with regenerator column (9) upper end, the rich solution of rich solution flash tank (7) lower end packing section upper with regenerator column (9) is connected, resurgent gases is connected with resurgent gases cooling heat exchanger (10) one end by regenerator column (9) top vent, resurgent gases cooling heat exchanger (10) the other end is connected resurgent gases separating tank (11), resurgent gases separating tank (11) top gas exports workshop section of liquefying with follow-up gas compression and is connected,
Described regenerator column (9) bottom is provided with reboiler (8), the steam-in of reboiler (8) is connected with the low-pressure steam from steam pipe system, the outlet of reboiler (8) is connected with the steam cooling vapour/liquid entrance of rich solution reheater (6), and the steam cooling liquid outlet of rich solution reheater (6) is connected with condensation water tank (17);
The lean solution outlet of described regenerator column (9) bottom is connected with the lean solution entrance pipe of poor rich liquid heat exchanger (5), the lean solution outlet of poor rich liquid heat exchanger (5) is connected with lean pump (13), lean pump (13) outlet is connected with heat pump set one (18) cold junction entrance by lean solution flow control valve (14), and heat pump set one (18) cold side outlet is connected with absorption tower (2) lean solution entrance through lean solution water cooler (15);
Described condensation water tank (17) condensate outlet is connected with heat pump set one (18) hot-side inlet, the outlet of heat pump set one (18) hot junction is connected heat pump set two (12) cold junction entrance and is connected, heat pump set two (12) cold side outlet is connected steam condensate pipe network, and heat pump set two (12) hot junction is connected with regenerator column (9) bottom.
2. a kind of carbon dioxide capture system according to claim 1, it is characterised in that, described heat pump set one (18) is absorption heat pump with heat pump set two (12).
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| CN201410637130.6A CN104399356B (en) | 2014-11-05 | 2014-11-05 | A kind of carbon dioxide capture system |
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| CN201410637130.6A CN104399356B (en) | 2014-11-05 | 2014-11-05 | A kind of carbon dioxide capture system |
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| CN104399356A CN104399356A (en) | 2015-03-11 |
| CN104399356B true CN104399356B (en) | 2016-06-01 |
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Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104815529A (en) * | 2015-04-21 | 2015-08-05 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture regeneration system |
| CN104785073A (en) * | 2015-04-30 | 2015-07-22 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture, power generation and sequestration system utilizing terrestrial heat |
| CN105903310A (en) * | 2016-06-02 | 2016-08-31 | 广东电网有限责任公司电力科学研究院 | CO2 trapping system and heating system for regenerating tower of CO2 trapping system |
| CN108096996B (en) * | 2016-11-25 | 2021-03-02 | 中国石油化工股份有限公司 | MDEA selective desulfurization process and system |
| CN106731600A (en) * | 2016-12-20 | 2017-05-31 | 新疆敦华石油技术股份有限公司 | A kind of collecting carbonic anhydride liquefying plant |
| CN107138024B (en) * | 2017-05-12 | 2020-03-10 | 东北电力大学 | Integrated particle fluidized carbon dioxide capture method and apparatus for power plants |
| CN108211671B (en) * | 2018-03-15 | 2023-07-11 | 中国华能集团清洁能源技术研究院有限公司 | Energy-saving carbon dioxide regeneration and compression system and method |
| CN110115910A (en) * | 2019-06-20 | 2019-08-13 | 中国华能集团清洁能源技术研究院有限公司 | A kind of energy-saving carbon dioxide capture system and method |
| CN114247272B (en) * | 2021-12-28 | 2023-01-31 | 北京华源泰盟节能设备有限公司 | Energy-saving system based on carbon dioxide capture technology |
| CN114788992A (en) * | 2022-03-09 | 2022-07-26 | 国家电投集团远达环保股份有限公司 | Carbon capture system and power plant boiler steam turbine system coupled with carbon capture system |
| CN114452779B (en) * | 2022-03-09 | 2022-09-27 | 清华大学 | Carbon dioxide capture system based on phase change absorbent |
| 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 |
| CN115138181A (en) * | 2022-05-31 | 2022-10-04 | 华能营口热电有限责任公司 | Energy-saving and water-saving carbon capture device and method |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203244905U (en) * | 2013-04-17 | 2013-10-23 | 北京工业大学 | Carbon dioxide capturing system based on second-class absorption heat pump |
| CN103657381B (en) * | 2013-11-25 | 2015-06-10 | 中石化石油工程设计有限公司 | Flue gas pretreatment and carbon dioxide collecting, purifying and recycling device |
| CN203648344U (en) * | 2013-11-25 | 2014-06-18 | 中石化石油工程设计有限公司 | Carbon dioxide capture experiment evaluation testing device |
| CN103961979B (en) * | 2014-04-28 | 2015-12-30 | 中国华能集团清洁能源技术研究院有限公司 | A kind of carbon dioxide capture system of multi-stage diffluence regeneration and technique |
| CN204337980U (en) * | 2014-11-05 | 2015-05-20 | 中国华能集团清洁能源技术研究院有限公司 | A kind of carbon dioxide capture device |
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