CN104399356A - Carbon dioxide capture system - Google Patents
Carbon dioxide capture system Download PDFInfo
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- CN104399356A CN104399356A CN201410637130.6A CN201410637130A CN104399356A CN 104399356 A CN104399356 A CN 104399356A CN 201410637130 A CN201410637130 A CN 201410637130A CN 104399356 A CN104399356 A CN 104399356A
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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 carbon dioxide capture system is disclosed. According to the invention, a heat pump system and a carbon dioxide capture system are combined. Low-pressure steam heat is fully utilized. After the low-pressure steam releases heat to rich liquor at the bottom of a regeneration tower, the rich liquor is reheated by a rich liquor reheater. A steam cooling liquid which releases heat again is collected in a condensation water tank. A steam condensate outlet of the condensation water tank is connected with a hot end of a first heat pump unit. Then, a barren liquor pump outlet is connected with a cold end of the first heat pump unit. A steam condensate is heated while the first heat pump unit cools barren liquor. The hot end outlet of the first heat pump unit is then connected with a cold end of a second heat pump unit, and a hot end of the second heat pump unit is communicated with the bottom of the regeneration tower. The rich liquor is desorbed by the use of heat from the hot end of the second heat pump unit. According to the invention, low-grade heat of the steam condensate is utilized efficiently, and demand of low-pressure steam and cooling load of the barren liquor can be reduced. The purpose of increasing desorption degree of the rich liquor and reducing energy consumption of the whole carbon dioxide capture system is achieved.
Description
Technical field
The invention belongs to flue gases purification field, be particularly useful for low concentration CO in the flue gas of the generations such as coal-burning boiler, gas turbine and Industrial Stoves
2trapping, particularly a kind of carbon dioxide capture system.
Background technology
Against Global Climate Changes is increasingly serious, has become one of principal element threatening human kind sustainable development, cuts down greenhouse gas emission becomes current international community concern focus with mitigation of climate change.Correlative study shows, the CO2 emission of China more than 50% comes from the thermal power generation of coal-burning power plant.Coal-fired plant flue gas discharge capacity is large, and Relatively centralized, the carbon trapping technique based on coal-burning power plant's exploitation is one of important channel of carbon dioxide discharge-reduction.
Utilize alkanolamine solution from flue gas, carry out the technology of collecting carbonic anhydride ripe in chemical industry, similar technology launches multiple demonstration in coal-burning power plant.But because generating plant flue gas has large-minded, the feature such as point to force down, this Technology application problem maximum in power station is that energy consumption is high, and steam consumption is large.Reduce energy ezpenditure, raise the efficiency, need to be cut operating costs by the carbon trapping system of development of new and subsystem, improve the large-scale promotion of this technology.
Experimental study finds, for traditional collecting carbonic anhydride technology, carbon dioxide is in regenerative process, because regeneration is thorough, have an appointment 40% carbon dioxide can not get release and enter absorption tower along with solution, cause solution absorbability inadequate, to ensure identical carbon dioxide produce, solution circulation amount and steam consumption must be increased, not only increase the trapped vapor hear rate that power consumption also add unit carbon dioxide, cause the overall energy consumption of service system large; Meanwhile, prior art steam is to solution for once heat release, and Btu utilization is insufficient, and is not used to the tow taste heat of part cooling water 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, the object of the present invention is to provide a kind of carbon dioxide capture system, this system can be used for the trapping of fire coal, gas-fired station flue gas and chemical field low fractional pressure carbon dioxide, optimize the technique of alcohol amine 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 be communicated with flue gas flow control 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, be communicated with rich solution flash tank 7, the gas vent at rich solution flash tank 7 top is communicated with regenerator 9 upper end, the rich solution of rich solution flash tank 7 lower end is communicated with packing section on regenerator 9, regeneration gas is communicated with regeneration gas cooling heat exchanger 10 one end by regenerator 9 top vent, regeneration gas cooling heat exchanger 10 other end is communicated with regeneration gas knockout drum 11, the outlet of regeneration gas knockout drum 11 top gas compresses and liquefies workshop section with subsequent gases and is communicated with.
Reboiler 8 is provided with bottom described regenerator 9, the steam inlet of reboiler 8 is communicated with the low-pressure steam from steam pipe system, the outlet of reboiler 8 is communicated with the steam cooling vapour/liquid entrance of rich solution reheater 6, and the steam cooling liquid outlet of rich solution reheater 6 is communicated with condensation water tank 17.
Described condensation water tank 17 condensate outlet is communicated with source pump 1 hot-side inlet, source pump 1 hot junction outlet source pump 2 12 cold-side inlet is connected, source pump 2 12 cold side outlet is communicated with steam-condensation grid, and source pump 2 12 hot junction is communicated with bottom regenerator 9.
Lean solution outlet bottom described regenerator 9 is communicated 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 communicated with lean pump 13, lean pump 13 is exported and is communicated with source pump 1 cold-side inlet by lean solution flow control valve 14, and source pump 1 cold side outlet is communicated with absorption tower 2 lean solution entrance through lean solution cooler 15.
Described source pump 1 is absorption heat pump with source pump 2 12.
Compared with prior art, heat pump combines with carbon dioxide capture system by the present invention, make full use of low-pressure steam heat, low-pressure steam to carry out after a heat release by rich solution reheater rich solution reheating the rich solution at the bottom of regenerator, steam cooling fluid after heat release is again collected into condensation water tank, the steam-condensation water out of condensation water tank is connected with source pump one hot junction, again lean pump outlet is connected with source pump one cold junction, utilize source pump one heating steam condensed water while lowering the temperature to lean solution, the hot junction outlet of source pump one is connected with the cold junction of source pump two again, the hot junction of source pump two is communicated with bottom regenerator, desorb rich solution is taken with the heat in source pump two hot junction, the tow taste heat of steam condensate is made to obtain efficiency utilization, 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 structural representation of the present invention.
Detailed description of the invention
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 be communicated with flue gas flow control 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, be communicated 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 gas vent at rich solution flash tank 7 top is communicated with regenerator 9 upper end, the rich solution of rich solution flash tank 7 lower end is communicated with packing section on regenerator 9, regeneration gas is communicated with regeneration gas cooling heat exchanger 10 one end by regenerator 9 top vent, regeneration gas cooling heat exchanger 10 other end is communicated with regeneration gas knockout drum 11, the regeneration gas that regenerator 9 produces is discharged by regenerator 9 top and is communicated with regeneration gas cooling heat exchanger 10, gas enters regeneration gas knockout drum 11 after heat exchange, the outlet of regeneration gas knockout drum 11 top gas compresses and liquefies workshop section with subsequent gases and is communicated with.
Reboiler 8 is provided with bottom described regenerator 9, the steam inlet of reboiler 8 is communicated with the low-pressure steam from steam pipe system, the outlet of reboiler 8 is communicated with the steam cooling vapour/liquid entrance of rich solution reheater 6, and the steam cooling liquid outlet of rich solution reheater 6 is communicated with condensation water tank 17.
Described condensation water tank 17 condensate outlet is communicated with source pump 1 hot-side inlet, source pump 1 hot junction outlet source pump 2 12 cold-side inlet is connected, source pump 2 12 cold side outlet is communicated with steam-condensation grid, and source pump 2 12 hot junction is communicated with bottom regenerator 9.Condensate liquid returns steam-condensation grid again after source pump 1 after the heat release of source pump 2 12 cold junction, and source pump 2 12 hot junction is communicated with bottom regenerator 9.
Lean solution outlet bottom described regenerator 9 is communicated 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 communicated with lean pump 13, lean pump 13 is exported and is communicated with source pump 1 cold-side inlet by lean solution flow control valve 14, source pump 1 cold side outlet is communicated with absorption tower 2 lean solution entrance through lean solution cooler 15, and the lean solution after heat release enters absorption tower 2 lean solution entrance again after lean solution cooler 15 heat exchange.
Described source pump 1 is absorption heat pump with source pump 2 12.
Technical process of the present invention and principle are:
Neat stress after desulphurization denitration enters absorption tower 2 by flue gas flow control valve 1 adjust flux, flue gas and spray and under absorbent form counter current contacting, the rich solution absorbing carbon dioxide carries out reheating from entering rich solution reheater 6 bottom absorption tower 2 after rich solution pump 3 dozens to poor rich liquid heat exchanger 5 and lean solution heat exchange, enter rich solution flash tank 7 again and reclaim heat, the outlet of rich solution flash tank 7 top gas is communicated with regenerator 9 top, together lower the temperature through re-generatively cooled heat exchanger 10 heat exchange with the regeneration gas at regenerator 9 top, after regeneration gas knockout drum 11 gas-liquid separation, finished product carbon dioxide gas enters subsequent compression liquefaction workshop section, rich solution bottom rich solution flash tank 7 enters regenerator packing section upper end and carries out desorption and regeneration.
After rich solution reheater 6 reheating, enter rich solution flash tank 7 from the rich solution after absorbing carbon dioxide bottom absorption tower 2 again through poor rich liquid heat exchanger 5 to recover energy, rich solution flash tank 7 rich bottoms liquid enters regenerator regeneration from regenerator 9 packing section upper end, gas fraction enters regenerator 9 top from rich solution flash tank 7 top and regenerator 9 top regeneration gas is together lowered the temperature through re-generatively cooled heat exchanger 10 heat exchange, after regeneration gas knockout drum 11 gas-liquid separation, finished product carbon dioxide gas enters subsequent compression liquefaction workshop section.
Lean solution bottom regenerator 9 enters the heat release of source pump 1 cold junction 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 communicated with source pump 1 hot junction, condensation water tank 17 is returned again after the heat release of source pump 2 12 cold junction, source pump 2 12 hot junction is communicated with bottom regenerator 9, utilize source pump 1 that lean solution is lowered the temperature, and make steam condensate be warming up to about 95 DEG C, recycling source pump two makes steam condensate release heat, makes source pump two hot junction working medium be warming up to about 120 DEG C, thus reaches the object with source pump two hot junction working medium heat desorb rich solution.
Claims (5)
1. a carbon dioxide capture system, it is characterized in that, comprise the absorption tower (2) be communicated with flue gas flow control 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), be communicated with rich solution flash tank (7), the gas vent at rich solution flash tank (7) top is communicated with regenerator (9) upper end, the rich solution of rich solution flash tank (7) lower end is communicated with the upper packing section of regenerator (9), regeneration gas is communicated with regeneration gas cooling heat exchanger (10) one end by regenerator (9) top vent, regeneration gas cooling heat exchanger (10) other end is communicated with regeneration gas knockout drum (11), the outlet of regeneration gas knockout drum (11) top gas compresses and liquefies workshop section with subsequent gases and is communicated with.
2. a kind of carbon dioxide capture system according to claim 1, it is characterized in that, described regenerator (9) bottom is provided with reboiler (8), the steam inlet of reboiler (8) is communicated with the low-pressure steam from steam pipe system, the outlet of reboiler (8) is communicated with the steam cooling vapour/liquid entrance of rich solution reheater (6), and the steam cooling liquid outlet of rich solution reheater (6) is communicated with condensation water tank (17).
3. a kind of carbon dioxide capture system according to claim 1, it is characterized in that, described condensation water tank (17) condensate outlet is communicated with source pump one (18) hot-side inlet, source pump one (18) hot junction outlet source pump two (12) cold-side inlet is connected, source pump two (12) cold side outlet is communicated with steam-condensation grid, and source pump two (12) hot junction is communicated with regenerator (9) bottom.
4. a kind of carbon dioxide capture system according to claim 1, it is characterized in that, the lean solution outlet of described regenerator (9) bottom is communicated 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 communicated with lean pump (13), lean pump (13) outlet is communicated with source pump one (18) cold-side inlet by lean solution flow control valve (14), and source pump one (18) cold side outlet is communicated with absorption tower (2) lean solution entrance through lean solution cooler (15).
5. a kind of carbon dioxide capture system according to claim 1, is characterized in that, described source pump one (18) is absorption heat pump with source pump 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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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| 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 |
| 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 |
| CN107138024A (en) * | 2017-05-12 | 2017-09-08 | 东北电力大学 | The grain fluidized collecting carbonic anhydride method and apparatus of integral type for power plant |
| CN108096996A (en) * | 2016-11-25 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of MDEA selective desulfurizations technique and system |
| CN108211671A (en) * | 2018-03-15 | 2018-06-29 | 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 regeneration and compressibility 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 |
| CN114247272A (en) * | 2021-12-28 | 2022-03-29 | 北京华源泰盟节能设备有限公司 | Energy-saving system based on carbon dioxide capture technology |
| 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 |
| 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 |
| 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 |
| CN116212593A (en) * | 2023-04-18 | 2023-06-06 | 河北正元氢能科技有限公司 | Cryogenic carbon dioxide trapping device for urea production |
| WO2023168925A1 (en) * | 2022-03-09 | 2023-09-14 | 清华大学 | Carbon dioxide capture system based on phase change absorbent |
| 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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Cited By (19)
| 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 |
| CN108096996A (en) * | 2016-11-25 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of MDEA selective desulfurizations technique 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 |
| CN107138024A (en) * | 2017-05-12 | 2017-09-08 | 东北电力大学 | The grain fluidized collecting carbonic anhydride method and apparatus of integral type for power plant |
| CN108211671A (en) * | 2018-03-15 | 2018-06-29 | 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 regeneration and compressibility and method |
| 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 |
| CN114247272A (en) * | 2021-12-28 | 2022-03-29 | 北京华源泰盟节能设备有限公司 | Energy-saving system based on carbon dioxide capture technology |
| 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 |
| WO2023168925A1 (en) * | 2022-03-09 | 2023-09-14 | 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 |
| CN116212593A (en) * | 2023-04-18 | 2023-06-06 | 河北正元氢能科技有限公司 | Cryogenic carbon dioxide trapping device for urea production |
| 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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