CN203648344U - Carbon dioxide capture experiment evaluation testing device - Google Patents
Carbon dioxide capture experiment evaluation testing device Download PDFInfo
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- CN203648344U CN203648344U CN201320749331.6U CN201320749331U CN203648344U CN 203648344 U CN203648344 U CN 203648344U CN 201320749331 U CN201320749331 U CN 201320749331U CN 203648344 U CN203648344 U CN 203648344U
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Abstract
The utility model relates to a carbon dioxide capture experiment evaluation testing device. The device comprises a carbon dioxide steel cylinder, a carbon dioxide buffer tank, an air compressor, an absorber, a heat pump system, a heater, a regenerator, gas-liquid separators and rich and poor liquid sample collection and treatment systems which are organically connected together; the traditional absorption and desorption technology is organically combined with an absorption type heat pump system and a vapor recompression heat recovery system; a double-heating way is adopted by the heater. The rich and poor liquid sample collection and treatment systems are respectively arranged at the bottoms of the absorber and the regenerator, so that pharmaceutical composition analysis and oxidative degradation measurement can be carried out; a tail gas outlet of the gas-liquid separator of the absorber is provided with a gas collection and treatment system, so that gas components can be rapidly analyzed. The regenerated gas produced by the gas-liquid separator of the regenerator is returned back into the absorber by the air compressor, so that the tail gas can be recycled, and carbon dioxide emission and resource waste are avoided. The carbon dioxide capture experiment evaluation testing device is an experimental facility which is energy-saving, efficient and convenient for drug evaluation and process optimization test.
Description
Technical field
The utility model relates to collecting carbonic anhydride purification process field, particularly coal-fired plant flue gas collecting carbonic anhydride test evaluation testing arrangement.
Background technology
Carbon dioxide is global warming, produces the one of the main reasons of extreme climate disaster.The purifying of the carbon of titanium dioxide trapping in recent years becomes hot research problem.Coal-burning power plant is main electric power and heat source of supply of China, is also maximum CO2 emission source.Trapping, carbon dioxide after purifying in order to the displacement of reservoir oil and sealed up for safekeeping in discarded oil reservoir, are had to important economic and social benefit.
Existing collecting carbonic anhydride purifying process mainly relies on monoethanolamine as absorbent, through absorbing and two processes of desorb, obtains the carbon dioxide of high concentration.These two processes are accompanied by repeatedly cooling and heat absorption, and capacity usage ratio is low.The energy consumption of chemical absorbing desorption process is owing to utilizing low-pressure steam to heat rich solution in reboiler, carbon dioxide is desorbed from solution, such heating mode makes the heat energy utilization of steam abundant not, integral energy utilization rate is lower, so it is particularly important to seek other high efficiency heating process patterns.Meanwhile, for the absorbent of collecting carbonic anhydride the performance test of running particularly its stability, corrosivity and degradation rate to investigate be also the important research content that collecting carbonic anhydride absorption technique amplifies.
Summary of the invention
The purpose of this utility model has been to provide a kind of collecting carbonic anhydride test evaluation testing arrangement, this device combines traditional absorption and desorption technique and absorption type heat pump system, steam recompression heat recovery system, the heater of this device adopts two mode of heatings, can effectively reduce flexibly the energy consumption of collecting carbonic anhydride purification system.This device can be used for powder performance evaluation and process optimization test, carries out medicament stability test, erosion test, degraded test and trapping system process optimization test experiments.
The technical solution of the utility model is achieved in the following ways:
The utility model comprises carbon dioxide steel cylinder, carbon dioxide buffer tank, moisturizing groove, liquid pool, air compressor, absorber, lean solution cooler, poor rich liquid heat exchanger, heat pump, heater, regenerator, flash vessel, vapour compression machine, gas-liquid separator and rich or poor liquid sample acquisition processing system, it is characterized in that carbon dioxide steel cylinder and carbon dioxide buffer filling import are connected, carbon dioxide buffer tank outlet export with the first air compressor and connect after be connected with absorber bottom import by gas flow regulating valve, the top gas outlet that absorber is deviate from after carbon dioxide is connected with the first gas-liquid separator import, the first gas-liquid separator top waste gas outlet is connected with tail gas switch valve, bottom lean solution outlet is connected with the lean solution import of absorber top, the outlet of absorber bottom rich solution is connected respectively with rich solution sample valve with rich solution pump inlet, rich solution pump discharge is connected with the heat pump import of poor rich liquid heat exchanger and heat pump by order, heat pump outlet enters to be respectively connected with heater middle part rich solution with the import of regenerator upper top rich solution, heater top is containing the outlet of rich solution steam and being connected containing rich solution steaming import of regenerator middle and lower part, heater is connected with the bottom filler lower end import of regenerator respectively containing the centre exit of rich solution steam, the upper end import of lower filler is connected with filler upper end import on top, the lean solution outlet of regenerator middle and lower part is connected with the bottom lean solution import of heater, the carbon dioxide outlet of regenerator top is connected with water cooler import, water cooler outlet is connected with the second gas-liquid separator upper inlet, the second gas-liquid separator top pure carbon dioxide exports by order and exhaust sampling valve, the 3rd gas-liquid separator, outlet is connected the second air compressor with carbon dioxide buffer tank, the outlet of regenerator bottoms lean solution is connected with lean solution sample valve with the import of flash vessel lean solution respectively, flash vessel top steam (vapor) outlet is connected with regenerator bottom steam inlet with vapour compression machine by frequency-variable controller, the lean solution outlet of flash vessel bottom is passed through poor rich liquid heat exchanger by order, lean pump, the vaporization chamber of heat pump, lean solution cooler is connected with the top lean solution import of absorber, moisturizing storage tank exports with dosing storage tank and connects afterwards and is connected with top absorption liquid import at the bottom of regenerator by fluid infusion pump.
Absorber, regenerator, heater and gas-liquid separator are made as vertical type cylinder shape, and absorber and regenerator are gone up separately low head and be connected with adopting separately flange between cylinder.
Upper and lower at absorber is provided with corrosion probe, detects online lean solution and the rich solution extent of corrosion to absorber.
Absorber bottom rich solution sample valve is connected with there being rich or poor liquid sample acquisition processing system separately with regenerator bottoms lean solution sample valve, adopts gas chromatography mass spectrometry chromatograph to analyze rich solution and lean solution component.
The first gas-liquid separator tail gas switch valve is connected with gas collecting treatment system, on-line analysis tail gas component.
The utlity model has following advantage:
1, this device is provided with regeneration gas cyclic utilization system, and the regenerating carbon dioxide gas that the second gas-liquid separator is produced is back to absorber by air compressor pressurization after the 3rd gas-liquid separator dewaters, is dried, and has realized recycling of tail gas, has avoided CO
2discharge and the wasting of resources.
2, the rich solution that has absorbed carbon dioxide was heated up before regeneration, improve desorption effect, the rich solution that absorber bottom produces, before entering regenerator, heats by poor rich liquid heat exchanger, heat pump and heater successively.The present invention is the absorption temperature that reduces lean solution, improves lean solution absorbability, and the lean solution bearing again at the bottom of regenerator is carried out cooling through flash vessel, poor rich liquid heat exchanger, heat pump and lean solution cooler successively.
3, use absorption type heat pump system, effectively utilize lean solution waste heat to heat rich solution, effectively utilize lean solution waste heat to heat rich solution, realize the reduction of lean solution temperature and the rising of rich solution temperature, reduced rich solution regeneration institute's calorific requirement and system energy consumption.
4, adopt two mode of heatings, the rich solution after heat pump enters regenerator, enters electric heater (boiling device) regenerate through tower bottom; Or directly entering heater heats.
5, the high-temperature barren liquor of regenerator bottoms is introduced flash vessel, and the flash-off steam of generation enters vapour compression machine and compresses after intensification, returns to regenerator bottoms, has realized steam heat recovery, has reduced system energy consumption.This device adopts frequency-changing control system for fluid flow and the control of equipment pressure, the 3rd gas-liquid separator is provided with gas flow and separator pressure frequency-changing control system, is provided with frequency-variable controller to realize flash vessel internal pressure and the interlock control that enters vapour compression machine steam flow between flash vessel and vapour compression machine.
6, the applicable pressure limit of this technique is 0.1-1MPa, can obtain CO
2purity reach more than 99.9%, CO
2capture rate reaches 90%, and the more traditional MEA system of system energy consumption reduces about 30-50%.
Brief description of the drawings
Accompanying drawing 1 is schematic flow sheet of the present invention.
Accompanying drawing 1 description of symbols: 1-carbon dioxide steel cylinder, 2-carbon dioxide buffer tank, the 3-the first air compressor 1, 4-tail gas switch valve 1, 5-the first gas-liquid separator, 6-filling absorber, 7-gas feed flow control valve, 8-rich solution sample valve, 9-moisturizing storage tank, 10-the second air compressor 2, 11-lean solution cooler, 12-dosing storage tank, 13-heat pump, 14-lean pump, 15-poor rich liquid heat exchanger, 16-rich solution pump, 17-fluid infusion pump, 18-regenerator, 19-heater, 20-water cooler, 21-lean solution sample valve, 22-gas frequency-changing control system, the 23-the three gas-liquid separator, the 24-the second gas-liquid separator, 25-exhaust sampling valve 2, 26-liquid switch valve, 27-vapour compression machine, 28-frequency-variable controller, 29-flash vessel.
Detailed description of the invention
For further disclosing the technical solution of the utility model, below in conjunction with accompanying drawing, by embodiment, the present invention is described in detail:
The utility model comprises carbon dioxide steel cylinder 1, carbon dioxide buffer tank 2, moisturizing storage tank 9, dosing storage tank 12, air compressor 3, 10, absorber 6, lean solution cooler 11, poor rich liquid heat exchanger 15, heat pump 13, heater 19, regenerator 18, flash vessel 29, vapour compression machine 27, gas- liquid separator 5, 24, 23 and rich or poor liquid sample acquisition processing system, it is characterized in that carbon dioxide steel cylinder and carbon dioxide buffer filling import are connected, carbon dioxide buffer tank outlet export with the first air compressor and connect after be connected with absorber bottom import by gas flow regulating valve 7, the top gas outlet that absorber is deviate from after carbon dioxide is connected with the first gas-liquid separator 5 imports, the first gas-liquid separator top waste gas outlet is connected with tail gas switch valve 4, bottom lean solution outlet is connected with the lean solution import of absorber top, the outlet of absorber bottom rich solution is connected respectively with rich solution sample valve 8 with 16 imports of rich solution pump, rich solution pump discharge is connected with the heat pump import of poor rich liquid heat exchanger 15 and heat pump 13 by order, heat pump outlet enters to be respectively connected with heater 19 middle part rich solutions with the import of regenerator upper top rich solution, heater top is containing the outlet of rich solution steam and being connected containing rich solution steaming import of regenerator middle and lower part, heater containing the centre exit of rich solution steam respectively with the bottom filler lower end import of regenerator, the upper end import of lower filler is connected with filler upper end import on top, the lean solution outlet of regenerator middle and lower part is connected with the bottom lean solution import of heater, the carbon dioxide outlet of regenerator top is connected with water cooler 20 imports, water cooler outlet is connected with the second gas-liquid separator 24 upper inlet, and the second gas-liquid separator top pure carbon dioxide exports by order and exhaust sampling valve 26, the 3rd gas-liquid separator 23, 2 outlets are connected the second air compressor 10 with carbon dioxide buffer tank, the outlet of regenerator bottoms lean solution is connected with lean solution sample valve 21 with flash vessel 29 lean solution imports respectively, flash vessel top steam (vapor) outlet is connected with regenerator bottom steam inlet with vapour compression machine 27 by frequency-variable controller 28, and the lean solution outlet of flash vessel bottom is passed through poor rich liquid heat exchanger 15 by order, lean pump 14, the vaporization chamber of heat pump 13, lean solution cooler 11 is connected with the top lean solution import of absorber, moisturizing storage tank 9 exports with dosing storage tank 12 and connects afterwards and is connected with top absorption liquid import at the bottom of regenerator by fluid infusion pump 17.
Carbon dioxide out enters carbon dioxide buffer tank from steel cylinder, after mixing, enters absorber 6 with from the air of the first air compressor 3.Mixed gas flow adopts inlet gas flow control valve 7 to control.Absorber overhead is deviate from tail gas after carbon dioxide and is entered the first gas-liquid separator 5 and carry out gas-liquid separation, the first gas-liquid separator bottom liquid is back to absorber top, gas after treatment is discharged by tail gas switch valve 4, or enters on-line analysis gas handling system and carry out gas component analysis.The rich solution that has absorbed carbon dioxide is drawn by absorber bottom, enters poor rich liquid heat exchanger 15 by rich solution pump 16, and rich solution also can enter online rich or poor liquid sample acquisition processing system by the control of rich solution sample valve 8.
The entrance lean solution of poor rich liquid heat exchanger is from flash vessel 29 bottoms, and the outlet lean solution of poor rich liquid heat exchanger enters the vaporization chamber of absorption type heat pump system 13, under low pressure utilizes lean solution heat to carry out heating evaporation to indoor moisture, realizes the reduction of lean solution temperature simultaneously.Rich solution after poor rich liquid heat exchanger heats up enters absorption heat pump.
Rich solution after heat pump enters regenerator 18, enters heater 19(boiling device through bottom) regenerate; Or directly enter heater and heat, two circuits are respectively arranged with valve control.In the time that rich solution directly enters regenerator, heater plays the effect of the boiling device of regenerator, for regenerator provides heat; In the time that rich solution directly enters heater, the high-temperature steam that heater produces is introduced regenerator bottom from its top, for regenerator provides steam source, the high temperature rich solution that heater produces can be respectively from regenerator top and middle part introduce regenerator.
After the palingenesis of regenerator, the CO that rich solution produces
2lower the temperature by water cooler 20 successively, enter the second gas-liquid separator 24 and remove liquid.The liquid that the second gas-liquid separator bottom produces imports dosing storage tank by liquid switch valve.The second gas-liquid separator 24 gas out can recycle, and gas is introduced to the 3rd gas-liquid separator 23 and further remove after liquid, under the effect of the second air compressor 10, enters absorption tower as unstripped gas, forms gas circulation.The 3rd gas-liquid separator 23 is provided with gas flow and separator pressure frequency-changing control system 22.
The liquid that comes self-water replenishing storage tank 9 and dosing storage tank 12 enters regenerator bottoms by the effect of fluid infusion pump 17.The regeneration lean solution that regenerator bottoms produces enters flash vessel 29, after compressing by vapour compression machine 27, the steam that under low pressure flash vessel produces enters regenerator bottoms, the lean solution that flash vessel bottom produces enters poor rich liquid heat exchanger 15 and carries out exchange heat with rich solution, to reduce temperature.Between flash vessel and vapour compression machine, be provided with frequency-variable controller 28 to realize flash vessel internal pressure and the interlock control that enters vapour compression machine steam flow.The regeneration lean solution of regenerator bottoms can be carried out on-line analysis by lean solution sample valve.
For improving rich solution regeneration effect, absorber bottom rich solution, before entering regenerator, heats by poor rich liquid heat exchanger, heat pump 13 and heater successively.For improving lean solution absorbability, the lean solution that bear at 18 ends of regenerator is again carried out cooling through flash vessel 29, poor rich liquid heat exchanger 15, lean pump 14, heat pump 13 and lean solution cooler 11 successively.
Embodiment: smoke carbon dioxide capture recovery experiment device
Gas composition: 15%CO
2, 80%N
2, 5%O
2
Air inflow: 10Nm
3/ h
MEA solution circulation amount: 100L/h;
Absorption type heat pump system COP:1.65
Both vapor compression acc power: 3.5KW
Absorber lean solution inlet temperature: 40 DEG C
Regenerator bottoms temperature: 110 DEG C;
Regenerator pressure: 0.9MPa
The second gas-liquid separator outlet CO
2purity: 99.95%;
CO
2capture rate: 91.5%;
More traditional MEA process system saving energy: 36.5%.
The applicable pressure limit of this experimental provision is 0.1-1MPa, can obtain CO
2purity reach more than 99.9%, collecting carbonic anhydride rate reaches 90%, the more traditional MEA process system of experimental system energy consumption saving energy 30-50%.That a kind of energy consumption is low, decarburization is effective, is convenient to the Novel experimental testing arrangement of evaluating powder performance, carrying out process optimization.
Claims (5)
1. a collecting carbonic anhydride test evaluation testing arrangement, comprise carbon dioxide steel cylinder, carbon dioxide buffer tank, moisturizing groove, liquid pool, air compressor, absorber, lean solution cooler, poor rich liquid heat exchanger, heat pump, heater, regenerator, flash vessel, vapour compression machine, gas-liquid separator and rich or poor liquid sample acquisition processing system, it is characterized in that: carbon dioxide steel cylinder is filled with import with carbon dioxide buffer and is connected, carbon dioxide buffer tank outlet export with the first air compressor and connect after be connected with absorber bottom import by gas flow regulating valve, the top gas outlet that absorber is deviate from after carbon dioxide is connected with the first gas-liquid separator import, the first gas-liquid separator top waste gas outlet is connected with tail gas switch valve, bottom lean solution outlet is connected with the lean solution import of absorber top, the outlet of absorber bottom rich solution is connected respectively with rich solution sample valve with rich solution pump inlet, rich solution pump discharge is connected with the heat pump import of poor rich liquid heat exchanger and heat pump by order, heat pump outlet enters to be respectively connected with heater middle part rich solution with the import of regenerator upper top rich solution, heater top is containing the outlet of rich solution steam and being connected containing rich solution steaming import of regenerator middle and lower part, heater is connected with the bottom filler lower end import of regenerator respectively containing the centre exit of rich solution steam, the upper end import of lower filler is connected with filler upper end import on top, the lean solution outlet of regenerator middle and lower part is connected with the bottom lean solution import of heater, the carbon dioxide outlet of regenerator top is connected with water cooler import, water cooler outlet is connected with the second gas-liquid separator upper inlet, the second gas-liquid separator top pure carbon dioxide exports by order and exhaust sampling valve, the 3rd gas-liquid separator, outlet is connected the second air compressor with carbon dioxide buffer tank, the outlet of regenerator bottoms lean solution is connected with lean solution sample valve with the import of flash vessel lean solution respectively, flash vessel top steam (vapor) outlet is connected with regenerator bottom steam inlet with vapour compression machine by frequency-variable controller, the lean solution outlet of flash vessel bottom is passed through poor rich liquid heat exchanger by order, lean pump, the vaporization chamber of heat pump, lean solution cooler is connected with the top lean solution import of absorber, moisturizing storage tank exports with dosing storage tank and connects afterwards and is connected with top absorption liquid import at the bottom of regenerator by fluid infusion pump.
2. collecting carbonic anhydride test evaluation testing arrangement according to claim 1, it is characterized in that: absorber, regenerator, heater and gas-liquid separator are made as vertical type cylinder shape, absorber and regenerator are gone up separately low head and are connected with adopting separately flange between cylinder.
3. collecting carbonic anhydride test evaluation testing arrangement according to claim 1, is characterized in that: the upper and lower at absorber is provided with corrosion probe, detects online lean solution and the rich solution extent of corrosion to absorber.
4. collecting carbonic anhydride test evaluation testing arrangement according to claim 1, it is characterized in that: absorber bottom rich solution sample valve is connected with there being rich or poor liquid sample acquisition processing system separately with regenerator bottoms lean solution sample valve, adopt gas chromatography mass spectrometry chromatograph to analyze rich solution and lean solution component.
5. according to the collecting carbonic anhydride test evaluation testing arrangement described in claim 1, it is characterized in that: the first gas-liquid separator tail gas switch valve is connected with gas collecting treatment system, on-line analysis tail gas component.
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| CN201320749331.6U CN203648344U (en) | 2013-11-25 | 2013-11-25 | Carbon dioxide capture experiment evaluation testing device |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399356A (en) * | 2014-11-05 | 2015-03-11 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture system |
| 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 |
| CN107567351A (en) * | 2015-04-08 | 2018-01-09 | 太阳火有限公司 | For preparing the preparation method and preparation facilities of methane/gaseous state and/or liquid hydrocarbon |
| CN108778440A (en) * | 2015-03-18 | 2018-11-09 | 弗朗索伊斯·帕尔曼蒂耶 | The chromatography separating method of high effect |
| CN110873777A (en) * | 2019-12-17 | 2020-03-10 | 兰州金润宏成石油化工科技有限公司 | A pilot test device for evaluating low carbon hydrocarbon oxidation catalyst performance |
| CN111252979A (en) * | 2020-01-14 | 2020-06-09 | 自然资源部天津海水淡化与综合利用研究所 | Thermal method seawater desalination water post-treatment system for municipal water supply |
| CN111500331A (en) * | 2020-04-27 | 2020-08-07 | 中海石油气电集团有限责任公司 | Natural gas decarburization experimental device with semi-barren solution logistics |
| CN115501739A (en) * | 2022-11-22 | 2022-12-23 | 广东捷玛节能科技股份有限公司 | Flue gas CO 2 Desorption device of trapping system |
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2013
- 2013-11-25 CN CN201320749331.6U patent/CN203648344U/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399356A (en) * | 2014-11-05 | 2015-03-11 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture system |
| CN108778440A (en) * | 2015-03-18 | 2018-11-09 | 弗朗索伊斯·帕尔曼蒂耶 | The chromatography separating method of high effect |
| CN108778440B (en) * | 2015-03-18 | 2021-06-08 | 弗朗索伊斯·帕尔曼蒂耶 | High performance chromatographic separation process |
| CN107567351A (en) * | 2015-04-08 | 2018-01-09 | 太阳火有限公司 | For preparing the preparation method and preparation facilities of methane/gaseous state and/or liquid hydrocarbon |
| CN107567351B (en) * | 2015-04-08 | 2021-09-07 | 太阳火有限公司 | Method and device for producing methane/gaseous and/or liquid hydrocarbons |
| 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 |
| CN110873777A (en) * | 2019-12-17 | 2020-03-10 | 兰州金润宏成石油化工科技有限公司 | A pilot test device for evaluating low carbon hydrocarbon oxidation catalyst performance |
| CN111252979A (en) * | 2020-01-14 | 2020-06-09 | 自然资源部天津海水淡化与综合利用研究所 | Thermal method seawater desalination water post-treatment system for municipal water supply |
| CN111500331A (en) * | 2020-04-27 | 2020-08-07 | 中海石油气电集团有限责任公司 | Natural gas decarburization experimental device with semi-barren solution logistics |
| CN115501739A (en) * | 2022-11-22 | 2022-12-23 | 广东捷玛节能科技股份有限公司 | Flue gas CO 2 Desorption device of trapping system |
| CN115501739B (en) * | 2022-11-22 | 2023-03-24 | 广东捷玛节能科技股份有限公司 | Flue gas CO 2 Desorption device of trapping system |
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Effective date of registration: 20151203 Address after: 100029 Beijing Chaoyang District Hui Xin a No. twelve layer 6 Patentee after: SINOPEC OILFIELD SERVICE CORPORATION Patentee after: SINOPEC PETROLEUM ENGINEERING DESIGN CO., LTD. Patentee after: Shandong Sairui Petroleum Science & Technology Development Co., Ltd. Address before: 257026 No. 49, Ji'nan Road, Dongying District, Shandong, Dongying Patentee before: SINOPEC PETROLEUM ENGINEERING DESIGN CO., LTD. Patentee before: Shandong Sairui Petroleum Science & Technology Development Co., Ltd. |
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