CN218011967U - Post-combustion CO based on waste heat utilization two-phase absorbent 2 Trapping device - Google Patents
Post-combustion CO based on waste heat utilization two-phase absorbent 2 Trapping device Download PDFInfo
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- CN218011967U CN218011967U CN202221086653.2U CN202221086653U CN218011967U CN 218011967 U CN218011967 U CN 218011967U CN 202221086653 U CN202221086653 U CN 202221086653U CN 218011967 U CN218011967 U CN 218011967U
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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
- 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
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- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Post-combustion CO based on waste heat utilization two-phase absorbent 2 A trapping apparatus comprising: the device comprises an absorption tower, a phase separator, a low-temperature multi-effect distillation reactor, a lean-rich liquid heat exchanger and a regeneration tower, wherein the low-temperature multi-effect distillation reactor comprises a plurality of distillation reactors connected end to end, each distillation reactor is provided with a reactor inlet, a dehydration outlet, a concentration outlet and a condensation outlet, and the device comprises a water-absorbing tower, a phase separator, a low-temperature multi-effect distillation reactor, a lean-rich liquid heat exchanger and a regeneration towerThe reactor inlet is communicated with a second rich liquid outlet of the phase separator; the lean-rich liquid heat exchanger comprises a heat exchanger inlet, a cooling outlet and a heating outlet, wherein the heat exchanger inlet is communicated with a concentration outlet of the last-effect distillation reactor, and the cooling outlet, a dehydration outlet of the distillation reactor and a lean liquid outlet of the phase separator are communicated with an A + B two-phase absorbent inlet. The utility model discloses can reduce flue gas CO by a wide margin 2 The energy consumption of trapping has wide application prospect.
Description
Technical Field
The utility model relates to a post-combustion chemical absorption CO method 2 Trapping device, in particular post-combustion CO based on a two-phase absorbent for waste heat utilization 2 A trapping device.
Background
With the higher dependence of the development of human socioeconomic energy, the wide utilization of fossil energy brings a series of environmental problems. With CO 2 Global climate change due to excessive emission of major greenhouse gases is becoming an important factor threatening human society. In recent years, CO in the atmosphere 2 The concentration reaches 400ppm level, which is increased by about 40 percent compared with the concentration before the industrial revolution, and the problems of sea level rise, global hydrological system disorder, frequent extreme weather events and the like caused by greenhouse effect lead the survival conditions of human beings to be severe day by day. How to deal with climate change caused by greenhouse effect becomes a major challenge which is necessary for sustainable development of human society.
Carbon dioxide capture and sequestration from industrial centralized emissions sources 2 The separation, the sealing and the long-term isolation from the atmosphere are important measures for solving the contradiction between the dependence of fossil energy and the coping with climate change. The development of CCS in the power industry will be in global CO 2 The weight of the Chinese herbal medicines is reduced and the Chinese herbal medicines are of great importance.
CO 2 The capture technology is mainly applied to large-scale CO 2 Fixing an emission source: fossil fuel power plants, fossil fuel processing, and other industrial processes. CO 2 2 Separation can be carried out at different stages of the fossil fuel utilization process, whereby carbon capture technologies can be broadly divided into three categories: post-combustion capture, pre-combustion capture, and oxycombustion capture.
Post combustion CO 2 Capturing and arranging at the tail end of an energy system, and separating CO from flue gas generated after combustion of fossil fuel 2 . Post combustion CO 2 The captured technology has high maturity, the requirements on the design and the technical transformation of an energy system are low, and the layout of main equipment of the power plant is hardly influenced, so that the device has high conformity with coal-fired and natural gas power plants. However, under the current technical conditions, the combustion system of a conventional power plant is operated by airIs an oxidant, and CO in the flue gas is diluted by nitrogen 2 The partial pressure is low (about 15vol-% of a coal-fired unit and about 4vol-% of a natural gas unit), the flue gas flow is large (about 320kg/s of a 300MW coal-fired unit and about 708.3kg/s of a 450MW natural gas unit), the energy consumption and the cost in the carbon capture process are relatively high, the net power generation efficiency of a power plant of the capture system after combustion is generally reduced by 8-12%, and the power generation cost is increased by 30-45%.
The most widely used absorbents for chemical absorption are the alcamines. The alcohol amine method is especially suitable for the low CO with complex components 2 Partial pressure and low CO 2 Decarbonizing the power plant flue gas with concentration. But now CO 2 The absorption pregnant solution mainly adopts a thermal desorption mode to realize the regeneration of the absorbent, the desorption energy consumption is too large, and the absorption pregnant solution accounts for the capture of CO 2 70-80% of the process, corresponding equipment corrosion will cause a further increase in capture costs.
Disclosure of Invention
In order to overcome the defects of the prior art, the utility model provides a post-combustion CO based on a waste heat utilization two-phase absorbent 2 A capture device which can greatly reduce the CO in the flue gas 2 The energy consumption of trapping has wide application prospect.
The utility model provides a technical scheme that its technical problem adopted is:
post-combustion CO based on waste heat utilization two-phase absorbent 2 A trapping apparatus comprising: absorption tower, phase separator, low temperature multi-effect distillation reactor, rich and lean solution heat exchanger and regenerator column, wherein:
the absorption tower comprises a flue gas inlet and a first rich liquid outlet which are arranged at the bottom of the tower and used for the entry of the flue gas after combustion, an A + B two-phase absorbent inlet and a flue gas outlet used for the discharge of the flue gas after decarburization, wherein the A + B two-phase absorbent inlet and the flue gas outlet are arranged at the top of the tower;
the phase separator comprises a phase separator inlet positioned at the upper part, a barren liquor outlet and a second rich liquor outlet positioned at the lower part, and the phase separator inlet is communicated with the first rich liquor outlet of the absorption tower;
the low-temperature multi-effect distillation reactor comprises a plurality of distillation reactors connected end to end, each distillation reactor is provided with a reactor inlet, a dehydration outlet, a concentration outlet and a condensation outlet, and the reactor inlet is communicated with a second rich liquid outlet of the phase separator;
the lean-rich liquid heat exchanger comprises a heat exchanger inlet, a cooling outlet and a heating outlet, wherein the heat exchanger inlet is communicated with a concentration outlet of the last-effect distillation reactor, and the cooling outlet, a dehydration outlet of the distillation reactor and a lean liquid outlet of the phase separator are communicated to an A + B two-phase absorbent inlet;
the regeneration tower comprises a regeneration tower first inlet and CO 2 And a first inlet of the regeneration tower is connected with a heating outlet of the lean-rich liquid heat exchanger.
Compared with the prior art, the utility model discloses a post-combustion CO based on double-phase absorbent of waste heat utilization 2 The trapping device uses a two-phase absorbent, a low-temperature multi-effect distillation device is additionally arranged in front of the regeneration tower, and a part of solvent is removed in advance through low-temperature multi-effect distillation before the rich solution enters the thermal desorption process, so that the rich solution is further concentrated, the water content of the solvent is reduced after concentration, and CO is generated 2 The equilibrium partial pressure is improved, and the driving force of mass transfer of pregnant solution regeneration is strengthened, thereby reducing the latent heat of vaporization and the sensible heat of evaporation of the solvent water in the regeneration process. Meanwhile, after the rich solution is further concentrated, the flow of the rich solution entering the regeneration tower is correspondingly reduced, the temperature of the rich solution at the inlet of the regeneration tower can be increased, and the waste heat recovery is enhanced. Therefore, on the premise of solving the problems of corrosion, degradation and the like of the high-concentration absorbent, the energy-saving absorbent has a remarkable energy-saving advantage.
Drawings
The present invention will be further described with reference to the accompanying drawings and examples.
Fig. 1 is a block diagram of an embodiment of the present invention.
Description of the reference numerals:
1. the absorption tower, 2, the phase separator, 3, the low-temperature multi-effect distillation reactor, 31, the distillation reactor, 4, the lean and rich liquor heat exchanger, 5, the regeneration tower, 6, the reboiler, 7, the first flash tank, 8, the second flash tank, 9, the compressor, 10, the environmental protection equipment, 11, the flue gas cooler, 12, the pump body, 121, the first rich liquor pump, 122, the second rich liquor pump, 123, the third rich liquor pump, 124, the first lean liquor pump, 125, the second lean liquor pump, 13, the pipeline/pipeline.
Detailed Description
To make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and obviously, the described embodiments are some, but not all, embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
FIG. 1 is a schematic diagram of a preferred embodiment of the present invention, a post-combustion CO-based waste heat utilization two-phase absorbent 2 A trapping apparatus comprising: absorption tower 1, phase separator 2, poor rich liquid heat exchanger 4, low temperature multiple effect distillation reactor 3 and regenerator column 5, wherein:
the absorption tower 1 comprises a flue gas inlet, a first rich solution outlet, an A + B two-phase absorbent inlet and a flue gas outlet, wherein the flue gas inlet is formed in the bottom of the tower and used for the entry of flue gas after combustion, the A + B two-phase absorbent inlet is formed in the top of the tower, and the flue gas outlet is used for the discharge of decarbonized flue gas;
the phase separator 2 comprises a phase separator inlet positioned at the upper part, a barren liquor outlet and a second rich liquor outlet positioned at the lower part, and the phase separator inlet is communicated with the first rich liquor outlet of the absorption tower 1;
the low-temperature multi-effect distillation reactor 3 comprises a plurality of distillation reactors 31 connected end to end, each distillation reactor 31 is provided with a reactor inlet, a dehydration outlet, a concentration outlet and a condensation outlet, and the reactor inlet is communicated with a second rich solution outlet of the phase separator 2;
the lean-rich liquid heat exchanger 4 comprises a heat exchanger inlet, a cooling outlet and a heating outlet, the heat exchanger inlet is communicated with the concentration outlet of the last-effect distillation reactor 31, and the cooling outlet, the dehydration outlet of the distillation reactor 31 and the lean liquid outlet of the phase separator 2 are communicated with an A + B two-phase absorbent inlet;
the regeneration column 5 includes regenerationFirst inlet of column and CO 2 And a first inlet of the regeneration tower is connected with a heating outlet of the lean-rich liquid heat exchanger 4.
Absorption column 1 of two-phase absorbent, absorbing CO 2 Post-generation liquid-liquid phase separation, upper and lower two-phase CO 2 The load difference is large, the absorbent is subjected to phase splitting in the phase separator 2, the barren solution is directly returned to the absorption tower 1, and only the rich solution is subjected to subsequent regeneration, so that the energy consumption can be reduced by 30-50% compared with the traditional MEA system.
Part of the solvent is removed in advance through the low-temperature multi-effect distillation reactor 3, so that the rich solution is further concentrated, and the energy consumption caused by solvent evaporation in the regeneration process can be reduced.
The low-quality barren solution is changed into high-quality steam through a flash evaporation compression process to provide heat for a desorption process, and the insufficient part is provided by the reboiler 6, so that the low-temperature waste heat can be recovered.
Therefore, in the embodiment, from the viewpoints of reducing the regeneration energy consumption of the absorbent and improving the regeneration thermal efficiency, the method for capturing CO in the flue gas by the traditional alkanolamine method is used 2 The equipment is optimized, and the CO in the flue gas can be greatly reduced 2 The energy consumption of the trapping process has wide application prospect.
The working process is as follows:
after passing through the environmental protection equipment 10 of the power plant and the flue gas cooler 11, the flue gas temperature is cooled to 40-60 ℃, enters from the bottom of the absorption tower 1, and is in countercurrent contact with A + B absorbent barren solution to realize CO 2 And (4) collecting, wherein the decarbonized flue gas is discharged from the top of the absorption tower 1. Absorption of CO 2 The rich solution of the absorbent A + B enters a phase separator 2.
After phase separation, CO 2 The lean solution A with low load is mixed with the desorption lean solution B again and then returns to the absorption tower 1 again; CO after phase separation 2 And B rich liquid with high load enters a low-temperature multi-effect distillation reactor through a rich liquid pump, is further dehydrated and concentrated and then respectively performs two-stage heat exchange with lean liquid flash evaporation liquid and regeneration gas of a regeneration tower 5, and the temperature of the B rich liquid is raised to 95 ℃ and then enters the regeneration tower 5 for desorption.
The desorbed B lean solution enters a second flash tank 8 for flash evaporation to generate a large amount of secondary steam, the secondary steam is pressurized by a compressor 9 and then becomes high-temperature and high-pressure gas, the high-temperature and high-pressure gas enters a desorption tower for heating and desorption of the B rich solution, and the load of a reboiler 6 is reduced.
In an alternative embodiment of this embodiment, the regenerator column 5 further comprises a regenerator column second inlet and a regenerator column first outlet, and the post-combustion CO 2 The capture equipment further comprises a reboiler 6; the reboiler 6 comprises a reboiler first inlet communicated with the second outlet of the regeneration tower, a reboiler first outlet communicated with the second inlet of the regeneration tower, a reboiler second inlet for steam from a unit pipe network to enter, and a reboiler second outlet communicated with the inlet of the first flash tank; the distillation reactor 31 further comprises a steam inlet, and a first outlet of the first flash tank 7 is respectively communicated to each steam inlet of the distillation reactor 31. The hydrophobic flash steam of the reboiler 6 is used as a driving heat source of the low-temperature multi-effect distillation reactor 3, so that co-production or deep utilization of waste heat can be realized.
In an optional implementation manner of this embodiment, the regeneration tower 5 further includes a third inlet of the regeneration tower and a second outlet of the regeneration tower, and the second outlet of the regeneration tower passes through the second flash tank 8 and the compressor 9 in sequence and then is communicated to the third inlet of the regeneration tower. Through the flash distillation compression process, can become high-quality steam with low-quality barren solution, provide the heat for the desorption process, the less than partial by reboiler 6 provides, can realize the recovery of low temperature waste heat, further optimize and improve regeneration thermal efficiency. The quality improvement and utilization of barren solution flash steam can be realized, heat is provided for the desorption process, and the desorption energy consumption is reduced.
In an alternative embodiment of the present embodiment, the lean-rich liquid heat exchanger 4 further comprises a lean liquid inlet for communicating with another outlet of the second flash drum 8. The absorbent lean solution after flashing by the second flash tank 8 enters the lean solution inlet of the lean-rich solution heat exchanger 4 through the second lean solution pump 125. And separating the saturated steam and the saturated liquid after flash evaporation in a second flash tank 8, introducing the saturated steam into a compressor 9 for compression, and introducing the saturated liquid, namely the desorbed barren liquid, into a barren and rich liquid heat exchanger 4 through a second barren liquid pump 125 for heat exchange and temperature reduction.
In a specific embodiment of this embodiment, the low-temperature multi-effect distillation reactor 3 is a three-effect low-temperature multi-effect distillation reactor, and consists of three low-temperature distillation reactors 31. Without being limited thereto, the specific effect stage of the low temperature multi-effect distillation reactor 3 may be specifically matched according to actual application conditions.
In a preferred embodiment of this embodiment, the system further comprises an environmental protection device 10 and a flue gas cooler 11, which are connected to the flue gas inlet of the absorption tower 1 in sequence. The flue gas previously treated by the environmental protection equipment 10 and the flue gas cooler 11 not only contains less impurities, but also is more beneficial to capture.
In a specific embodiment of the embodiment, the absorption tower 1, the phase separator 2, the lean-rich liquid heat exchanger 4, the low-temperature multi-effect distillation reactor 3 and the regeneration tower 5 are connected/communicated through a pipeline/pipe 13 and conveyed by a pump body 12. Wherein, the pump body 12 can be a high-pressure pump.
In a specific optional implementation manner of this embodiment, the pump body 12 includes a rich liquid pump and a lean liquid pump, the first rich liquid pump 121, the second rich liquid pump 122, and the third rich liquid pump 123 are respectively disposed between the first rich liquid outlet of the absorption tower 1, the phase separator 2, and the low-temperature multi-effect distillation reactor 3, and between the low-temperature multi-effect distillation reactor 3 and the lean-rich liquid heat exchanger 4, and the first lean liquid pump 124 and the second lean liquid pump 125 are respectively disposed between the a + B two-phase absorbent inlet of the absorption tower 1, and between the lean-rich liquid heat exchanger 4 and the second flash tank 8.
The working principle is as follows:
the utility model discloses the double-phase absorbent of A + B that equipment used is by the CO of two kinds of different grade types and ratio 2 The absorbent A and the absorbent B can be DEEA + BDA, DEEA + MAPA, DEEA + MEA, DMAC + DETA and the like. Assuming absorption of CO 2 After then, CO 2 One phase with large load mainly consists of absorbent B and is called as pregnant solution; CO 2 2 The phase with the smaller loading is mainly composed of absorbent A and is called barren liquor.
After passing through the environmental protection equipment 10 of the power plant, the flue gas burned by the thermal power plant passes through the flue gas cooler 11, the temperature of the flue gas is cooled to 40-60 ℃, and then the flue gas enters the absorption tower 1 from the bottom and is in countercurrent contact with the lean solution of the A + B absorbent entering from the top of the absorption tower 1. The pressure in the absorption tower 1 is normal pressure, and the initial temperature of the absorbent can be set to 40 ℃. CO 2 2 Dissolved in the absorbent, and the decarbonized flue gas is discharged from the top of the absorption tower 1.
Absorption of CO 2 The post-A + B absorbent rich liquid is drawn out from the bottom of the absorption tower 1 by the first rich liquid pump 121 and enters the phase separator 2. The rich solution of the A + B absorbent is subjected to phase separation in a phase separator 2, and CO 2 The lean solution A with small load capacity is mixed with the lean solution B after desorption and heat exchange, and the mixture is directly returned to the absorption tower 1, and only CO is used 2 And (4) carrying out subsequent regeneration process on the B rich solution with large load.
According to different compositions of the absorbent, the water content of the B rich liquid after phase separation is 20% -50%, and the B rich liquid phase enters a low-temperature multi-effect distiller through a second rich liquid pump 122 for further dehydration and concentration. The driving heat source of the low-temperature multi-effect distillation is hydrophobic flash steam of a reboiler 6, three-effect distillation is arranged, the operating temperature of each effect is 45-60 ℃, and the concentration multiplying power of the absorbent is 1.8-2.2. And after the rich solution B is further concentrated by low-temperature multi-effect distillation, exchanging heat with the desorbed lean solution B in a lean and rich solution heat exchanger 4, wherein the end difference of the lean and rich solution heat exchanger 4 is 5-5 ℃. And the rich liquid B, the barren solution and the top gas of the regeneration tower 5 exchange heat in two stages to more than 95 ℃, and are sent to the top of the regeneration tower 5 for thermal desorption. The operation pressure of the regeneration tower 5 can be set to 1.2-2 bar, the gas phase temperature at the outlet of the tower top is 100 ℃, the liquid phase at the outlet of the tower bottom is 120 ℃, and the lean liquid CO after desorption 2 The load was 0.25mol CO 2 Per mol of amine. Since the rich solution is further concentrated, the water content of the solvent is reduced, and CO is generated 2 The equilibrium partial pressure is improved, and the driving force of mass transfer of rich liquor regeneration is strengthened, so that the latent heat of vaporization and the sensible heat of evaporation of the solvent water in the regeneration process are reduced. Meanwhile, after the rich liquid is further concentrated, the flow of the rich liquid entering the regeneration tower 5 is correspondingly reduced, the temperature of the rich liquid at the inlet of the regeneration tower can be increased, and the waste heat recovery is enhanced.
And the desorbed B barren solution enters a second flash tank 8 for flash evaporation, and the flash evaporation temperature is 90 ℃. Due to the reduced pressure in the second flash tank 8, a large amount of liquid is instantaneously vaporized, a large amount of steam (i.e., secondary steam) is generated, and the latent heat of vaporization of the liquid is converted into the sensible heat of the gas to be extracted. The gasified liquid flows out from the bottom of the second flash tank 8 under the action of self gravity, and is mixed with the A barren solution and returns to the absorption tower 1 after passing through the barren and rich solution heat exchanger 4. The secondary steam generated in the second flash drum 8 is pressurized by the compressor 9 to become gas with the temperature of 120-130 ℃, and the gas enters the regeneration tower 5 to heat and desorb the B rich liquid, so that the load of the reboiler 6 is reduced.
The above, only be the utility model discloses a preferred embodiment, it is not right the utility model discloses do the restriction in any form, all basis the utility model discloses a technical essence makes any simple modification and equal change to above embodiment, all falls into within the protection scope of the utility model.
Claims (8)
1. Post-combustion CO based on waste heat utilization two-phase absorbent 2 A trapping apparatus, characterized by comprising: absorption tower, phase separator, low temperature multi-effect distillation reactor, rich and lean solution heat exchanger and regenerator column, wherein:
the absorption tower comprises a flue gas inlet and a first rich liquid outlet which are arranged at the bottom of the tower and used for the entry of the flue gas after combustion, an A + B two-phase absorbent inlet and a flue gas outlet used for the discharge of the flue gas after decarburization, wherein the A + B two-phase absorbent inlet and the flue gas outlet are arranged at the top of the tower;
the phase separator comprises a phase separator inlet positioned at the upper part, a barren liquor outlet and a second rich liquor outlet positioned at the lower part, and the phase separator inlet is communicated with the first rich liquor outlet of the absorption tower;
the low-temperature multi-effect distillation reactor comprises a plurality of distillation reactors connected end to end, each distillation reactor is provided with a reactor inlet, a dehydration outlet, a concentration outlet and a condensation outlet, and the reactor inlet is communicated with a second rich solution outlet of the phase separator;
the lean-rich liquid heat exchanger comprises a heat exchanger inlet, a cooling outlet and a heating outlet, wherein the heat exchanger inlet is communicated with a concentration outlet of the last-effect distillation reactor, and the cooling outlet, a dehydration outlet of the distillation reactor and a lean liquid outlet of the phase separator are communicated to an A + B two-phase absorbent inlet;
the regeneration tower comprises a regeneration tower first inlet and CO 2 And a first inlet of the regeneration tower is connected with a heating outlet of the lean-rich liquid heat exchanger.
2.A method according to claim 1Post-combustion CO of waste heat utilization two-phase absorbent 2 The trapping device is characterized in that: the regeneration tower also comprises a second inlet of the regeneration tower and a first outlet of the regeneration tower, and the CO after combustion 2 The capture apparatus further comprises a reboiler;
the reboiler comprises a reboiler first inlet communicated with the second outlet of the regeneration tower, a reboiler first outlet communicated with the second inlet of the regeneration tower, a reboiler second inlet into which steam from a unit pipe network enters, and a reboiler second outlet communicated with the inlet of the first flash tank; the distillation reactor also comprises a steam inlet, and a first outlet of the first flash tank is respectively communicated to each steam inlet of the distillation reactor.
3. Post-combustion CO based on waste heat utilization two-phase absorbent according to claim 2 2 A trapping device characterized by: the regeneration tower also comprises a third inlet of the regeneration tower and a second outlet of the regeneration tower, and the second outlet of the regeneration tower sequentially passes through a second flash tank and a compressor and then is communicated to the third inlet of the regeneration tower.
4. Post-combustion CO based on waste heat utilization two-phase absorbent according to claim 3 2 The trapping device is characterized in that: the lean-rich liquid heat exchanger further comprises a lean liquid inlet which is communicated with the other outlet of the second flash tank.
5. Post-combustion CO based on a two-phase absorbent for residual heat utilization according to any of claims 1 to 4 2 A trapping device characterized by: the low-temperature multi-effect distillation reactor is a three-effect low-temperature multi-effect distillation reactor and consists of three low-temperature distillation reactors.
6. Post-combustion CO based on a two-phase absorbent for residual heat utilization according to any of claims 1 to 4 2 A trapping device characterized by: the absorption tower is characterized by further comprising environment-friendly equipment and a flue gas cooler which are sequentially connected to the flue gas inlet of the absorption tower.
7. Root of herbaceous plantsPost-combustion CO recycling two-phase absorbent based on waste heat utilization according to claim 6 2 The trapping device is characterized in that: the absorption tower, the phase separator, the low-temperature multi-effect distillation reactor, the lean-rich liquid heat exchanger and the regeneration tower are connected/communicated through pipelines/pipelines and are conveyed by a pump body.
8. Post-combustion CO based on two-phase waste heat utilization absorbent according to claim 7 2 A trapping device characterized by: the pump body comprises a rich liquid pump and a lean liquid pump, the first rich liquid pump, the second rich liquid pump and the third rich liquid pump are respectively arranged between a first rich liquid outlet, a phase separator and the low-temperature multi-effect distillation reactor of the absorption tower and between the low-temperature multi-effect distillation reactor and the lean rich liquid heat exchanger, and the first lean liquid pump and the second lean liquid pump are respectively arranged between an A + B two-phase absorbent inlet of the absorption tower and between the lean rich liquid heat exchanger and the second flash tank.
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| CN202221086653.2U CN218011967U (en) | 2022-05-07 | 2022-05-07 | Post-combustion CO based on waste heat utilization two-phase absorbent 2 Trapping device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221086653.2U CN218011967U (en) | 2022-05-07 | 2022-05-07 | Post-combustion CO based on waste heat utilization two-phase absorbent 2 Trapping device |
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| CN218011967U true CN218011967U (en) | 2022-12-13 |
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