CN203635055U - Flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device - Google Patents
Flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device Download PDFInfo
- Publication number
- CN203635055U CN203635055U CN201320748429.XU CN201320748429U CN203635055U CN 203635055 U CN203635055 U CN 203635055U CN 201320748429 U CN201320748429 U CN 201320748429U CN 203635055 U CN203635055 U CN 203635055U
- Authority
- CN
- China
- Prior art keywords
- regenerator
- enters
- flue gas
- rich
- carbon dioxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Classifications
-
- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
-
- 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
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The utility model relates to a flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device. The device comprises an absorber, a heat exchanger of a barren solution and a pregnant solution, a heat pump system, a heater, a regenerator, a flash evaporator, a vapour compressor and a cyclone separator, wherein an absorption-type heat pump is used for effectively converting reaction heat of the absorber into heat required by the regenerator; a vapour recompression heat recycling system can be used for decreasing the temperature of the barren solution; a generated flash-evaporating vapour is heated by the vapour compressor and then returned to the bottom of the regenerator; a high-temperature vapour generated by the heater is introduced into the bottom of the regenerator from the top of the heater; the generated high-temperature pregnant solution can be respectively introduced into the regenerator from the upper part and the middle of the regenerator. The device has the advantages of low energy consumption, good treatment effect, high CO2 capturing purity and high CO2 capturing efficiency. Thus, the device is a unique means for flue gas pretreatment and CO2 capturing purification. According to the device, the purity of the obtained CO2 can reach 99.9% in a pressure range being from 0.1MPa to 1MPa. Therefore, compared with the traditional process, the device provided by the utility model has the advantage that the energy consumption is saved by more than 30%.
Description
Technical field
The utility model relates to collecting carbonic anhydride and reclaims field, the particularly pretreatment of coal-fired plant flue gas and collecting carbonic anhydride purifying retracting device.
Background technology
Carbon dioxide is global warming, produces the one of the main reasons of extreme climate disaster.The carbon of carbon dioxide trapping in recent years becomes hot research problem with purifying.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 (MEA) as absorbent, through chemical absorbing desorption process, obtains the carbon dioxide of high concentration.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.
Simultaneously for common process flow process, after rich or poor liquid heat exchange, lean solution is entered lean solution water cooler and is cooled to suitable reaction temperature, and in lean solution cooling procedure, the heat water that is cooled is taken away greatly, does not realize the comprehensive utilization of heat energy.If interpolation heat pump, can, by lean solution heat recovery to rich solution, effectively reduce system energy consumption.
Summary of the invention
The purpose of this utility model provides a kind of pretreatment and trapping purifying retracting device of flue gas carbon dioxide.Overcome traditional carbon dioxide chemistry absorption and desorption technique and have the problems such as capacity usage ratio is low, energy consumption is large.The carbon dioxide trapping of the object of the invention is to reduce outside heat input, seeking energy-saving is reclaimed, and has effectively reduced the energy consumption of collecting carbonic anhydride purification system.
The utility model comprises absorber, poor rich liquid heat exchanger, heat pump, heater, regenerator, flash vessel, vapour compression machine, cyclone separator, it is characterized in that flue gas enters desulphurization denitration processor through smoke inlet Flow-rate adjustment valve regulation flue gas flow, the pretreated flue gas of desulphurization denitration enters absorbing carbon dioxide from absorber bottom, flue gas distributes and rises through absorber bottom barrier gas distributor, and carbon dioxide is absorbed by liquid absorption and becomes rich solution, the high density foam removal net foam removal that residual gas is provided with through top, enter cyclone separator, carry out gas-liquid separation, gas is gone out from cyclone separator top, enter follow-up processing flow, cyclone separator bottom liquid enters fluid infusion pond through cyclone separator fluid level control valve, and absorption liquid enters from absorber overhead continuously through lean pump, to the CO in flue gas
2absorb, absorb CO
2rich solution from absorber bottom out in absorber Liquid level adjusting valve carries out tower liquid level regulate and enter rich solution pump and pump into poor rich liquid heat exchanger, rich solution after poor rich liquid heat exchanger heats up enters absorption type heat pump system and heats, entering heater proceeds to heat up again, the rich solution of heater via heating becomes carbon dioxide and rich carbonated liquid, carbon dioxide out enters and regenerates from regenerator bottoms from heater top, rich carbonated liquid out divides two-way to regulate from the middle part of regenerator and top and enter and regenerate through rich liquid stream adjustable valve from heater base, the carbon dioxide of regeneration out enters water chiller cooling from regenerator top, after cooling, entering cyclone separator separates, carbon dioxide after separation out enters molecular sieve dehydrator from cyclone separator top and dewaters, carbon dioxide after dehydration out enters carbon dioxide storage tank from molecular sieve top, the water of cyclone separator bottom and molecular sieve bottom enters fluid infusion pond through cyclone separator fluid level control valve, the lean solution of regenerator bottoms enters by fluid infusion pond and fluid infusion pump to flash vessel water pipe, enters flash vessel by the control of regeneration Liquid level adjusting valve, the steam of flash vessel flash distillation enters from regenerator bottoms through frequency-variable controller control, vapour compression machine compression, heat to regenerator, the lean solution flashing off out enters the vaporization chamber of heat pump through poor rich liquid heat exchanger from flash vessel bottom, out enter lean solution cooler from steaming vaporization chamber, enter absorber top by lean pump supercharging and the valve regulation of lean solution Flow-rate adjustment after cooling carbon dioxide circulation in the flue gas flue gas of coming in is absorbed.
Heater is made as electric heater, rich solution is heated, the high-temperature steam that electric heater produces is introduced the lower surface of the filler of regenerator bottoms from top, for regenerator provides steam source, the high temperature rich solution that electric heater produces respectively from the upper surface of regenerator top filler and the upper surface of bottom filling introduce regenerator regenerate.
The applicable pressure limit of this device is 0.1-1MPa,
Absorber bottom rich solution temperature is 45 ℃-47 ℃, is upgraded to 65 ℃-68 ℃ after entering poor rich liquid heat exchanger heat exchange, and the temperature that enters heat pump rises to 85 ℃-88 ℃, and it is 105 ℃-108 ℃ that rich solution enters electric heater heating-up temperature.
Under the palingenesis of regenerator, the CO that rich solution produces
2successively by water cooler lower the temperature, cyclone separator is removed liquid and molecular sieve dehydrator is dry.The high-pureness carbon dioxide gas generating is gone out from molecular sieve dehydrator top, and enters follow-up processing flow.The liquid that cyclone separator and molecular sieve dehydrator bottom produce imports fluid infusion pond by cyclone separator fluid level control valve 2.
The regeneration lean solution that the liquid in fluid infusion pond produces by fluid infusion pump 16 regenerator bottoms together enters flash vessel 29, after compressing by vapour compression machine 26, 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 and rich solution carries out exchange heat, to reduce temperature.Between flash vessel and vapour compression machine, be provided with frequency-variable controller 27 to realize flash vessel internal pressure and the interlock control that enters vapour compression machine steam flow.
The utility model is that the rich solution that has absorbed carbon dioxide was heated up before regeneration, improves desorption effect, and 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.
In device, use absorption type heat pump system, effectively utilize lean solution waste heat to heat rich solution, the reaction heat of absorber is converted into regenerator institute calorific requirement, realize the reduction of lean solution temperature and the rising of rich solution temperature.
The high-temperature steam that heater produces is introduced regenerator bottoms from its top, for regenerator provides steam and thermal source, the high temperature rich solution that heater produces can be respectively from regenerator top and middle part introduce regenerator and regenerate.
The high-temperature barren liquor of regenerator bottoms is introduced flash vessel, under low pressure carries out flash distillation, and reduces temperature, and the flash-off steam of generation enters vapour compression machine and compresses after intensification, returns to regenerator bottoms.Between flash vessel and vapour compression machine, be provided with frequency-variable controller, to realize the interlock control of flash vessel pressure and outlet steam flow thereof.
The applicable pressure limit of this device is 0.1-1MPa, can obtain CO
2purity reach 99.9%, save energy consumption more than 30% compared with traditional handicraft.
The utility model has the advantages that: for improving rich solution regeneration effect, absorber bottom rich solution, before entering regenerator, heats by poor rich liquid heat exchanger, heat pump and heater successively.For improving lean solution absorbability, 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.Have energy consumption low, treatment effect is good, and the advantage that collecting carbonic anhydride purity is high and arresting efficiency is high is a kind of flue gas pretreatment and collecting carbonic anhydride and purifying mode of uniqueness.In pressure 0.1-1MPa pressure limit, can obtain CO
2purity reach 99.9%, save energy consumption more than 30% compared with traditional handicraft.
Accompanying drawing explanation
Accompanying drawing 1 is schematic flow sheet of the present utility model.
Accompanying drawing 1 description of symbols: 1-smoke inlet flow control valve, 2-desulphurization denitration preprocessor, 3-absorber, 4-absorber pressure control valve, 5-cyclone separator 1, 6-cyclone separator fluid level control valve 1, 7-lean solution absorbs temperature control valve (TCV), 8-lean solution cooler, 9-lean solution flow control valve, 10-lean pump, 11-absorber Liquid level adjusting valve, 12-rich solution pump, 13-fluid infusion pond, 14-heat pump, 15-poor rich liquid heat exchanger, 16-fluid infusion pump, 17-heater, 18-rich liquid stream adjustable valve 1, 19-rich liquid stream adjustable valve 2, 20-water cooler, 21-regenerator, 22-regenerator pressure-regulating valve, 23-molecular sieve dehydrator, 24-cyclone separator 2, 25-cyclone separator fluid level control valve 2, 26-vapour compression machine, 27-frequency-variable controller, 28-regenerator Liquid level adjusting valve, 29-flash vessel.
The specific embodiment
for further originally openutility model
technical scheme,below in conjunction with accompanying drawing and specific embodiments, the present invention will be described in more detail:
Flue gas, before entering absorber 3, is removed oxysulfide, the nitrogen oxide that may contain through desulphurization denitration processor 2, to reduce the poisoning of absorbent and degraded.After desulphurization denitration pretreatment unit, flue gas enters in absorber and absorbs from absorber 3 bottoms, adopts smoke inlet flow control valve 1 to regulate flue gas flow.Absorber bottom is provided with barrier gas distributor, to promote flue gas being uniformly distributed in absorber; Absorber top is provided with high density foam removal net, prevents that air-flow from taking liquid in absorber out of from top.Absorbent enters from absorber overhead under the effect of lean pump 10, to the CO in flue gas
2absorb.Remove CO
2flue gas draw from absorber overhead, enter cyclone separator 5 and carry out gas-liquid separation, gas is gone out from cyclone separator top, enters follow-up processing flow; Cyclone separator bottom liquid pipeline is provided with cyclone separator fluid level control valve 6, and liquid enters fluid infusion pond 13 thus.Absorb CO
2rich solution under the effect of rich solution pump 12, enter poor rich liquid heat exchanger 15, adopt absorber Liquid level adjusting valve 11 to carry out the liquid level in absorber to regulate.The entrance lean solution of poor rich liquid heat exchanger is from flash vessel 29 bottoms.The outlet lean solution of poor rich liquid heat exchanger 15 enters the vaporization chamber of absorption type heat pump system 14, 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 type heat pump system and heats, rich solution after heat pump heat temperature raising enters electric heater 17 and proceeds heating, add thermogenetic high-temperature steam and introduce regenerator 21 bottoms from 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 and regenerate.
The applicable pressure limit of this device is 0.1-1MPa,
Absorber bottom rich solution temperature is 45 ℃-47 ℃, is upgraded to 65 ℃-68 ℃ after entering poor rich liquid heat exchanger heat exchange, and the temperature that enters heat pump rises to 85 ℃-88 ℃, and it is 105 ℃-108 ℃ that rich solution enters electric heater heating-up temperature.
Under the palingenesis of regenerator, the CO that rich solution produces
2successively by water cooler 20 lower the temperature, cyclone separator 24 removes liquid, drier through molecular sieve dehydrator 23, the high-purity CO of generation
2gas is gone out from the regenerator control valve 22 at molecular sieve dehydrator top, enters carbon dioxide storage tank.The liquid that cyclone separator 24 and molecular sieve dehydrator 23 bottoms produce enters fluid infusion pond 13 by cyclone separator fluid level control valve 25.
The liquid in fluid infusion pond together enters flash vessel 29 by fluid infusion pump 16 and the regeneration lean solution that regenerator bottom produces, after compressing by vapour compression machine 26, 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 and rich solution carries out exchange heat, to reduce temperature.Between flash vessel and vapour compression machine, be provided with frequency-variable controller 27 to realize flash vessel internal pressure and the interlock control that enters vapour compression machine steam flow.
The utility model is that the rich solution that has absorbed carbon dioxide was heated up before regeneration, improves desorption effect, and 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.
In device, use absorption type heat pump system, effectively utilize lean solution waste heat to heat rich solution, the reaction heat of absorber is converted into regenerator institute calorific requirement, realize the reduction of lean solution temperature and the rising of rich solution temperature.
The high-temperature steam that heater produces is introduced regenerator bottoms 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 and regenerate.
The high-temperature barren liquor of regenerator bottoms is introduced flash vessel, carries out flash distillation, and reduce temperature under low pressure, and the flash-off steam of generation enters vapour compression machine and compresses after intensification, returns to regenerator bottoms.Between flash vessel and vapour compression machine, be provided with frequency-variable controller 27, to realize the interlock control of flash vessel pressure and outlet steam flow thereof.
Case study on implementation:
Device and scale: 10NM
3/ h smoke carbon dioxide capture recovery experiment device
Gas composition:
Table 1 air-intake component table
Air inflow: 10NM
3/ h intake air temperature: 40 ℃
Table 2 feed liquor component table
| Component | Mass number (%) |
| MEA | 20 |
| H 2O | 80 |
Solution circulation amount: 60-80L/h feed liquor temperature: 40 ℃
Absorber bottom rich solution temperature is 45 ℃, is upgraded to 65 ℃ after entering poor rich liquid heat exchanger heat exchange, carries out afterwards reclaiming tow taste heat in lean solution after absorption type heat pump system, and temperature rises to 85 ℃.Rich solution enters electric heater and heats to 105 ℃ afterwards, 105 ℃, electric heater top steam enters packing layer bottom, and the 105 ℃ of rich solutions in electric heater bottom enter regenerator packing layer upper end, both reverse contacts, steam plays air lift and dividing potential drop effect, is conducive to regeneration gas CO
2fast decoupled overflow.
The regenerator bottoms lean solution temperature of regenerating is 105 ℃, enters flash vessel and flashes off 85 ℃ of steam, and energy recovery rate reaches 29%, is forced into 110 ℃ (about 140KpaA) turns back to regenerator packing layer bottom through vapour compression machine; Flash vessel bottom lean solution temperature is 85 ℃, and this lean solution enters subsequently poor rich liquid heat exchanger and is cooled to 70 ℃.Regenerator top gas is cooled to 45 ℃ after water cooler is processed, and enters subsequently follow-up flow process.Lean solution is subsequently after absorption type heat pump system is processed, and temperature is down to 50 ℃, and continues to be down to 40 ℃ by lean solution heat exchanger, enters afterwards absorber and carries out absorption operation.
Table 3 flash-off steam amount and energy recovery rate table
Claims (3)
1. the pretreatment of a flue gas and collecting carbonic anhydride purifying retracting device, comprise absorber, poor rich liquid heat exchanger, heat pump, heater, regenerator, flash vessel, vapour compression machine, cyclone separator, it is characterized in that flue gas enters desulphurization denitration processor through smoke inlet Flow-rate adjustment valve regulation flue gas flow, the pretreated flue gas of desulphurization denitration enters absorbing carbon dioxide from absorber bottom, flue gas distributes and rises through absorber bottom barrier gas distributor, and carbon dioxide is absorbed by liquid absorption and becomes rich solution, the high density foam removal net foam removal that residual gas is provided with through top, enter cyclone separator, carry out gas-liquid separation, gas is gone out from cyclone separator top, enter follow-up processing flow, cyclone separator bottom liquid enters fluid infusion pond through cyclone separator fluid level control valve, and absorption liquid enters from absorber overhead continuously through lean pump, to the CO in flue gas
2absorb, absorb CO
2rich solution from absorber bottom out in absorber Liquid level adjusting valve carries out tower liquid level regulate and enter rich solution pump and pump into poor rich liquid heat exchanger, rich solution after poor rich liquid heat exchanger heats up enters absorption type heat pump system and heats, entering heater proceeds to heat up again, the rich solution of heater via heating becomes carbon dioxide and rich carbonated liquid, carbon dioxide out enters and regenerates from regenerator bottoms from heater top, rich carbonated liquid out divides two-way to regulate from the middle part of regenerator and top and enter and regenerate through rich liquid stream adjustable valve from heater base, the carbon dioxide of regeneration out enters water chiller cooling from regenerator top, after cooling, entering cyclone separator separates, carbon dioxide after separation out enters molecular sieve dehydrator from cyclone separator top and dewaters, carbon dioxide after dehydration out enters carbon dioxide storage tank from molecular sieve top, the water of cyclone separator bottom and molecular sieve bottom enters fluid infusion pond through cyclone separator fluid level control valve, the lean solution of regenerator bottoms enters by fluid infusion pond and fluid infusion pump to flash vessel water pipe, enters flash vessel by the control of regeneration Liquid level adjusting valve, the steam of flash vessel flash distillation enters from regenerator bottoms through frequency-variable controller control, vapour compression machine compression, heat to regenerator, the lean solution flashing off out enters the vaporization chamber of heat pump through poor rich liquid heat exchanger from flash vessel bottom, out enter lean solution cooler from steaming vaporization chamber, enter absorber top by lean pump supercharging and the valve regulation of lean solution Flow-rate adjustment after cooling carbon dioxide circulation in the flue gas flue gas of coming in is absorbed.
2. the pretreatment of flue gas according to claim 1 and collecting carbonic anhydride purifying retracting device, heater is made as electric heater, rich solution is heated, the high-temperature steam that electric heater produces is introduced the lower surface of the filler of regenerator bottoms from top, for regenerator provides steam source, the high temperature rich solution that electric heater produces is regenerated from the upper surface of regenerator top filler and the upper surface of bottom filling introducing regenerator respectively.
3. the pretreatment of flue gas according to claim 1 and collecting carbonic anhydride purifying retracting device, absorber bottom rich solution temperature is 45 ℃-47 ℃, after entering poor rich liquid heat exchanger heat exchange, be upgraded to 65 ℃-68 ℃, the temperature that enters heat pump rises to 85 ℃-88 ℃, and it is 105 ℃-108 ℃ that rich solution enters electric heater heating-up temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320748429.XU CN203635055U (en) | 2013-11-25 | 2013-11-25 | Flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320748429.XU CN203635055U (en) | 2013-11-25 | 2013-11-25 | Flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203635055U true CN203635055U (en) | 2014-06-11 |
Family
ID=50866339
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320748429.XU Expired - Fee Related CN203635055U (en) | 2013-11-25 | 2013-11-25 | Flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203635055U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103657381A (en) * | 2013-11-25 | 2014-03-26 | 中石化石油工程设计有限公司 | Flue gas pretreatment and carbon dioxide collecting, purifying and recycling device |
| CN113877365A (en) * | 2020-07-03 | 2022-01-04 | 中石化石油工程技术服务有限公司 | CO2Trapping system and process |
| 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 |
-
2013
- 2013-11-25 CN CN201320748429.XU patent/CN203635055U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103657381A (en) * | 2013-11-25 | 2014-03-26 | 中石化石油工程设计有限公司 | Flue gas pretreatment and carbon dioxide collecting, purifying and recycling device |
| 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 |
| CN113877365A (en) * | 2020-07-03 | 2022-01-04 | 中石化石油工程技术服务有限公司 | CO2Trapping system and process |
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103657381B (en) | Flue gas pretreatment and carbon dioxide collecting, purifying and recycling device | |
| CN101745288B (en) | Method for vacuum pressure and temperature varying coupling adsorbing and trapping carbon dioxide in flue gas | |
| CN203648344U (en) | Carbon dioxide capture experiment evaluation testing device | |
| CN110960956B (en) | CO in flue gas is absorbed to applicable phase transition absorbent 2 Method and system of (2) | |
| CN105032113B (en) | Process for capturing carbon dioxide in flue gas based on wet reclamation technology | |
| CN108187455B (en) | Flue gas carbon dioxide capture system based on two-phase absorbent | |
| CN101492616B (en) | Desulfurization and decarburization integrated absorption process for polyglycol dimethyl ether | |
| CN107754568B (en) | Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process | |
| CN212166984U (en) | CO2Trapping system | |
| CN109999618A (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN101822929B (en) | Method for capturing carbon dioxide by utilizing electrical desorption technology | |
| CN203635055U (en) | Flue gas pretreatment and carbon dioxide (CO2) capturing purification recycling device | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN218544490U (en) | Flue gas waste heat recovery device of coupling carbon entrapment | |
| CN106582200A (en) | Flue gas carbon capturing system for temperature swing adsorption power plant by virtue of intermediate steam extraction | |
| CN102489120A (en) | Low temperature methanol wash method and equipment | |
| KR102055976B1 (en) | A single compression system and process for capturing carbon dioxide | |
| CN202355997U (en) | CO2 absorption tower and low-temperature methanol washing equipment comprising same | |
| CN111054187A (en) | Recovery system and gas recovery method | |
| CN107866134B (en) | A kind of efficient CO using unit steam2Trapping solution regenerative system and method | |
| TWI466711B (en) | A low-energy consumption system for co2 adsorption, concentration and energy conversion | |
| CN203429147U (en) | Methane purifying system | |
| CN101518706B (en) | Adsorption device and adsorbent regeneration method | |
| CN102321676A (en) | Biogas engineering two gas one fertile complex method | |
| CN217526998U (en) | Carbon dioxide capture system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20160526 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. |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140611 Termination date: 20171125 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |