CN115025512B - Switching type CO 2 De-sublimating separation system - Google Patents
Switching type CO 2 De-sublimating separation system Download PDFInfo
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- CN115025512B CN115025512B CN202210562346.5A CN202210562346A CN115025512B CN 115025512 B CN115025512 B CN 115025512B CN 202210562346 A CN202210562346 A CN 202210562346A CN 115025512 B CN115025512 B CN 115025512B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D7/00—Sublimation
- B01D7/02—Crystallisation directly from the vapour phase
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D7/00—Sublimation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/32—Direct CO2 mitigation
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- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a switching type CO 2 Desublimation fractionThe separation system comprises a flue gas flow path and a cooling module; the flue gas flow path comprises a sublimation flow path; the desublimation flow path comprises a dehumidifying device, a gas booster, a first switching valve, a sublimation heat exchanger a inlet, a sublimation heat exchanger a outlet, a second switching valve, a first precooling heat exchange channel of a precooling heat exchanger, a third switching valve, a desublimation heat exchanger, a fourth switching valve and a second precooling heat exchange channel of the precooling heat exchanger which are sequentially communicated; the sublimation flow path comprises an outlet of the sublimation heat exchanger d, a fifth switching valve, a compressor, a water cooling device and liquid CO which are sequentially communicated 2 And a storage tank. The invention combines CO 2 De-sublimation characteristic and switching separation method, and low-temperature de-sublimation method is adopted for CO in low-concentration low-pressure flue gas 2 High-efficiency separation is carried out by using solid CO 2 The cold quantity is used for preliminary precooling of the incoming smoke, and the clean smoke cold quantity is used for precooling the incoming smoke again, so that the energy consumption is further reduced, and the purpose of energy conservation is achieved.
Description
Technical Field
The present invention relates to CO 2 The separation field, in particular to a switching type CO 2 A desublimation separation system.
Background
Thermal power generation is currently still one of the important ways in which many countries meet their energy demands. Traditional thermal power generation relies on combustion of fuel such as coal, natural gas, biomass and the like with air, and the flue gas of the product mainly comprises CO 2 、N 2 And H 2 0. Among all carbon emissions sources, coal-fired power plants contributed global CO in 2012 2 42% of the discharge. In recent years, for CO 2 Separation mode exploration never stops, and the separation mode is mainly divided into a separation technology before combustion, an oxygen-enriched combustion technology and a separation technology after combustion, wherein the separation technology after combustion is relatively widely applied.
Low temperature CO 2 The separation technology belongs to one of the separation technology after combustion. Research indicates that low temperature CO 2 Separation saves 30% on energy compared to other methods, however, for a long time, because of the CO 2 The problem of clogging after desublimation is difficult to solve,low temperature CO 2 Separation is mainly focused on CO 2 The principle of the liquefaction separation is that CO is realized according to different melting boiling points of different components in the mixed gas 2 Is separated from the other components. CO 2 The critical temperature of (2) is 304.1K, the critical pressure is 7.377MPa, the triple point temperature is 216.55K, and the triple point pressure is 0.518MPa. For CO 2 Gases having a content above their three-phase pressure are in principle suitable for gas-liquid separation by cooling and partial condensation; whereas for CO 2 When the flue gas with the content lower than the pressure of the three-phase points is subjected to low-temperature separation, the flue gas needs to be compressed, and the initial pressure is increased to be higher than the pressure of the three-phase points, so that the flue gas enters a liquefiable state, and the process often needs to be subjected to multi-stage compression, so that the construction cost and the separation energy consumption are increased to a great extent, the early-stage investment is large, and the operation cost is high.
Theoretical analysis shows that low temperature CO is used 2 In the liquefaction and separation, CO is carried out as the separation is continued 2 The partial pressure of (2) is continuously reduced, and the separation difficulty is continuously increased, thereby leading to CO 2 The separation rate is low. When the flue gas pressure is increased, although the CO can be increased 2 Separation rate, but its purity decreases with increasing pressure, while energy consumption increases. Thus low temperature CO 2 Liquefaction separation is not suitable for CO 2 Low concentration flue gas.
Using low temperature CO 2 The separation of desublimation can obviously improve CO 2 Purity and separation rate. Chinese patent publication No. CN101854990a discloses a process for separating CO from a gaseous feed stream 2 CO by bed movement using 3 separate fixed beds 2 Is realized in the 1 st, 2 nd and 3 rd beds respectively 2 By using a pre-cooled porous body in the separation stage, which has a limited cold storage, which results in a process which can only separate limited CO in one cycle 2 The energy consumption of the bed layer movement is high.
Chinese patent publication No. CN113975938A discloses a device and method for capturing carbon dioxide in flue gas by rotary low-temperature adsorption, and CO is carried out by continuous rotation of an integral adsorbent bed in adsorption, desorption and cooling stages 2 The separation is complicated in structure, the waste heat requirement is high, and the energy consumption required by continuous rotation of the adsorption bed is high.
Therefore, in order to solve the problems of small treatment capacity, high energy consumption and the like in the prior art, a novel CO needs to be explored 2 A separation system.
Disclosure of Invention
The invention provides a switching type CO 2 Desublimation separation system, from mainly comprising CO 2 、N 2 And H 2 0 separation of CO from flue gas 2 The method comprises the steps of carrying out a first treatment on the surface of the The desublimation of CO2 is realized at low temperature and normal pressure, and the hot flue gas is used for heat exchange to lead CO to 2 Output after sublimation, thereby realizing CO 2 And (3) precooling incoming smoke at the same time, so that the cooling capacity is saved, and the energy consumption is reduced.
Switching type CO 2 The desublimation separation system comprises a dehumidifying device, a gas booster, a cooling module, a precooling heat exchanger, a sublimation heat exchanger, a desublimation heat exchanger, a compressor, a water cooling device and liquid CO 2 A storage tank;
the precooling heat exchanger comprises a first precooling heat exchange channel and a second precooling heat exchange channel; the sublimation heat exchanger and the desublimation heat exchanger have the same structure and comprise a first heat exchange channel and a second heat exchange channel, wherein the first heat exchange channel comprises an a inlet, a b inlet, a corresponding a outlet and a corresponding b outlet, and the second heat exchange channel comprises a c inlet, a corresponding c outlet and a corresponding d outlet;
the dehumidifying device is sequentially connected with the gas booster and the first switching valve, and the other two interfaces of the first switching valve are respectively connected with the two inlets a;
the two outlets a are respectively connected with two interfaces of a second switching valve, the other interface of the second switching valve is sequentially connected with a first precooling heat exchange channel and a third switching valve, and the other two interfaces of the third switching valve are respectively connected with two inlets c; the two outlets c are respectively connected with two interfaces of a fourth switching valve, and the other interface of the fourth switching valve is connected with a second precooling heat exchange channel; the two d outlets are respectively connected with two interfaces of a fifth switching valve, and the other interface of the fifth switching valve is sequentially connected with a compressor, a water cooling device and liquid CO 2 A storage tank;
the output end and the input end of the cooling module are respectively connected with one interface of a sixth switching valve and one interface of a seventh switching valve, the other two interfaces of the sixth switching valve are respectively connected with two inlets b, and the other two interfaces of the seventh switching valve are respectively connected with two outlets b.
Further, the sublimation heat exchanger and the desublimation heat exchanger realize the conversion of sublimation and desublimation functions under the control of all the switching valves;
when the sublimation heat exchanger is in a sublimation function and the desublimation heat exchanger is in a desublimation function; the first switching valve is opened to the first heat exchanger and closed to the second heat exchanger; the second switching valve is opened to a passage from the first heat exchanger and closed to a passage from the second heat exchanger; the third switching valve is opened to the second heat exchanger and closed to the first heat exchanger; the fourth switching valve is closed to the passage from the first heat exchanger and opened to the passage from the second heat exchanger; the fifth switching valve and the second switching valve are kept consistent; the sixth switching valve and the third switching valve are kept consistent; the seventh switching valve and the fourth switching valve are kept consistent;
when all the switching valves change direction, the sublimation heat exchanger is converted into a desublimation function, and the desublimation heat exchanger is converted into a sublimation function.
Further, when the sublimation heat exchanger is sublimation, the desublimation heat exchanger is desublimation; the desublimation flow path comprises a dehumidifying device, a gas booster, a first switching valve, an inlet a of the sublimation heat exchanger, an outlet a of the sublimation heat exchanger, a second switching valve, a first pre-cooling heat exchange channel of the pre-cooling heat exchanger, a third switching valve, the desublimation heat exchanger, a fourth switching valve and a second pre-cooling heat exchange channel of the pre-cooling heat exchanger which are sequentially communicated;
the sublimation flow path comprises an outlet d of the sublimation heat exchanger, a fifth switching valve, a compressor, a water cooling device and liquid CO which are sequentially communicated 2 And a storage tank.
Alternatively, all of the switching valves may be manual switching valves, solenoid switching valves, or other forms.
Further, the flue gas to be treated enters the system through the dehumidifying device, and the separated CO is separated 2 Into liquid CO 2 The storage tank is sealed and stored, and the rest clean flue gas is discharged after passing through a second precooling heat exchange channel of the precooling heat exchanger.
Further, the flue gas contains all CO generated by the coal-fired power plant or the gas-fired power plant 2 Is a smoke of the gas turbine.
Alternatively, the pre-cooling heat exchanger, the sublimation heat exchanger and the desublimation heat exchanger are divided wall type, double pipe type heat exchangers or any other forms, and any ribs such as straight ribs, needle ribs and the like can be added.
Alternatively, the cooling module includes a refrigeration unit and a circulation flow path, or an external cold source (such as LNG waste refrigeration) is used.
Compared with the prior art, the invention has the following beneficial effects:
(1) The invention obviously reduces the power consumption caused by multi-stage compression and improves the CO at the same time 2 Separation purity and separation rate. Using solid CO 2 And the clean flue gas pre-cools the incoming flue gas in two steps, so that the energy consumption is reduced. If there is a recyclable external cold source (such as LNG cold energy), the temperature of the refrigerant is lower than Wen Ninghua CO 2 The separation method can almost realize zero energy consumption, and has incomparable advantages to the liquefaction separation method.
(2) The invention adopts two sublimation or sublimation heat exchangers to carry out the treatment on CO in the flue gas 2 The switching separation can be carried out according to the flow of the treated flue gas and CO 2 The heat exchanger area is flexibly adjusted in the earlier stage according to the different concentrations, so that the CO in the high-flow low-pressure low-concentration flue gas is satisfied 2 Separation requirements.
(3) The invention removes and separates CO 2 In addition to the high concentration of N is produced 2 By-products, the running cost is reduced.
Drawings
FIG. 1 shows a switched CO in an embodiment of the invention 2 A schematic overall structure of the desublimation separation system;
FIG. 2 shows a switched CO in an embodiment of the invention 2 A first mode schematic of a desublimation separation system;
FIG. 3 shows a switched CO in an embodiment of the invention 2 First stage of desublimation separation systemTwo modes of schematic diagrams.
In the figure: 1. a dehumidifying device 2, a gas booster 3, a first switching valve 4, a sublimation heat exchanger 5, a second switching valve 6, a pre-cooling heat exchanger 7, a third switching valve 8, a desublimation heat exchanger 9, a fourth switching valve 10, a fifth switching valve 11, a compressor 12, a water cooling device 13, and liquid CO 2 A storage tank, 14, a cooling module, 15, a sixth switching valve, 16, a seventh switching valve.
Detailed Description
The invention will be described in further detail with reference to the drawings and examples, it being noted that the examples described below are intended to facilitate the understanding of the invention and are not intended to limit the invention in any way.
As shown in fig. 1, a switched CO 2 The desublimation separation system comprises a dehumidifier 1, a gas booster 2, a cooling module 14, a pre-cooling heat exchanger 6, a sublimation heat exchanger 4, a desublimation heat exchanger 8, a compressor 11, a water cooling device 12 and a liquid CO2 storage tank 13.
The precooling heat exchanger 6 comprises a first precooling heat exchange channel and a second precooling heat exchange channel; the sublimation heat exchanger 4 and the desublimation heat exchanger 8 have the same structure and comprise a first heat exchange channel and a second heat exchange channel, wherein the first heat exchange channel comprises an a inlet, a b inlet, a corresponding a outlet and a corresponding b outlet, and the second heat exchange channel comprises a c inlet, a corresponding c outlet and a corresponding d outlet.
The dehumidifying device 1 is sequentially connected with a gas booster 2 and a first switching valve 3, and the other two interfaces of the first switching valve 3 are respectively connected with two inlets a; the two outlets a are respectively connected with two interfaces of the second switching valve 5, the other interface of the second switching valve 5 is sequentially connected with the first precooling heat exchange channel and the third switching valve 7, and the other two interfaces of the third switching valve 7 are respectively connected with two inlets c; the two outlets c are respectively connected with two interfaces of a fourth switching valve 9, and the other interface of the fourth switching valve 9 is connected with a second precooling heat exchange channel; the two d outlets are respectively connected with two interfaces of the fifth switching valve 10, and the other interface of the fifth switching valve 10 is sequentially connected with the compressor 11, the water cooling device 12 and the liquid CO2 storage tank 13. The output end and the input end of the cooling module 14 are respectively connected with one interface of a sixth switching valve 15 and a seventh switching valve 16, the other two interfaces of the sixth switching valve 15 are respectively connected with two b inlets, and the other two interfaces of the seventh switching valve 16 are respectively connected with two b outlets.
The invention is suitable for CO in low-pressure low-concentration flue gas 2 The separation system comprises a flue gas flow path and a cooling module, wherein the flue gas flow path comprises CO 2 Desublimation flow path and CO 2 And a sublimation flow path.
The sublimation heat exchanger 4 and the desublimation heat exchanger 8 can realize the conversion of two modes of sublimation and desublimation under the control of all the switching valves.
The working process is as follows: the flue gas enters the dehumidifying device 1, enters the gas booster 2 after being dehydrated, and is slightly boosted, so that the resistance of subsequent pipelines and equipment can be overcome. Then enters the sublimation heat exchanger 4 through the first switching valve 3 to be pre-cooled for the first step and is solid CO 2 Sublimation provides heat; solid CO 2 Sublimating and leaving the sublimation heat exchanger 4, and processing the sublimated liquid by the compressor 11 and the water cooling device 12 to obtain liquid CO 2 The storage tank 13 is sealed; the incoming smoke enters the pre-cooling heat exchanger 6 through the second switching valve 5, is pre-cooled again by the pre-cooling heat exchanger, and enters the desublimation heat exchanger 8 through the third switching valve 7; the refrigerant provides cold energy for the desublimation heat exchanger 8 through the sixth switching valve 15 and the seventh switching valve 16, and CO in the flue gas 2 Desublimation to solid in the desublimation heat exchanger 8; clean flue gas leaves the desublimation heat exchanger 8, enters the pre-cooling heat exchanger 6 through the fourth switching valve 9, exchanges heat with incoming flow flue gas, discharges the flue gas after utilizing residual cold energy, and completes primary CO 2 Desublimation separation (this mode is defined as the first mode, with the flow path shown in fig. 2). All switching valves are reversed, the sublimation heat exchanger 4 and the desublimation heat exchanger 8 are functionally switched, and the next separation is performed (this mode is defined as a second mode, and the flow path is shown in fig. 3).
In the first mode, the first switching valve 3 is opened to the first heat exchanger 4 and closed to the second heat exchanger 8; the second switching valve 5 opens to the passage from the first heat exchanger 4 and closes to the passage from the second heat exchanger 8; the third switching valve 7 is opened to the second heat exchanger 8 and closed to the first heat exchanger 4; the fourth switching valve 9 is closed to the passage from the first heat exchanger 4 and opened to the passage from the second heat exchanger 8; the fifth switching valve 10 and the second switching valve 5 are kept consistent; the sixth switching valve 15 and the third switching valve 7 are kept in agreement; the seventh switching valve 16 and the fourth switching valve 9 remain identical.
In this mode, CO 2 The desublimation flow path comprises a dehumidifying device 1, a gas booster 2, a first switching valve 3, an inlet a of a sublimation heat exchanger 4, an outlet a of the sublimation heat exchanger 4, a second switching valve 5, a first pre-cooling heat exchange channel of a pre-cooling heat exchanger 6, a third switching valve 7, a desublimation heat exchanger 8, a fourth switching valve 9 and a second pre-cooling heat exchange channel of the pre-cooling heat exchanger 6 which are sequentially communicated;
CO 2 the sublimation flow path comprises an outlet of the sublimation heat exchanger 4, a fifth switching valve 10, a compressor 11, a water cooling device 12 and liquid CO which are communicated in sequence 2 A storage tank 13.
The cooling module 14 is connected to the desublimation heat exchanger 8 via a sixth switching valve 15 and a seventh switching valve 16, providing cold thereto.
In the embodiment of the invention, a proper heat insulation mode is used, such as stacking heat insulation, vacuum powder and fiber heat insulation, high-vacuum multi-layer heat insulation and the like, so as to achieve a better heat insulation effect.
The gas booster adopts a piston structure for slightly boosting the incoming smoke so that the resistance of the pipeline and the equipment can be overcome. The switching valve is used for controlling the flow direction of the fluid, so that the heat exchanger is switched between the desublimation mode and the sublimation mode. For better overall control, the switching valve can be any form of manual switching valve, electromagnetic switching valve and the like according to economic requirements or technical requirements so as to adapt to the requirements of different economical efficiency or response speeds.
To strengthen heat exchange, the heat exchange efficiency and CO are improved 2 The cleanliness and heat exchanger can be in any form of a partition type, a sleeve type and the like, and any rib such as a straight rib, a needle rib and the like can be added to improve the heat exchange area.
To provide for CO 2 Sufficient cooling to sublimate at atmospheric pressure, preferably the cooling module includes a refrigeration unit and a circulation flow path or external cooling source (e.g., LNG waste cooling).
The foregoing embodiments have described in detail the technical solution and the advantages of the present invention, it should be understood that the foregoing embodiments are merely illustrative of the present invention and are not intended to limit the invention, and any modifications, additions and equivalents made within the scope of the principles of the present invention should be included in the scope of the invention.
Claims (6)
1. Switching type CO 2 The desublimation separation system is characterized by comprising a dehumidifying device (1), a gas booster (2), a cooling module (14), a pre-cooling heat exchanger (6), a sublimation heat exchanger (4), a desublimation heat exchanger (8), a compressor (11), a water cooling device (12) and liquid CO 2 A storage tank (13);
the precooling heat exchanger (6) comprises a first precooling heat exchange channel and a second precooling heat exchange channel; the sublimation heat exchanger (4) and the desublimation heat exchanger (8) have the same structure and respectively comprise a first heat exchange channel and a second heat exchange channel, wherein the first heat exchange channel comprises an a inlet, a b inlet, a corresponding a outlet and a corresponding b outlet, and the second heat exchange channel comprises a c inlet, a corresponding c outlet and a corresponding d outlet;
the dehumidifying device (1) is sequentially connected with the gas booster (2) and the first switching valve (3), and the other two interfaces of the first switching valve (3) are respectively connected with the two inlets a;
the two outlets a are respectively connected with two interfaces of the second switching valve (5), the other interface of the second switching valve (5) is sequentially connected with the first precooling heat exchange channel and the third switching valve (7), and the other two interfaces of the third switching valve (7) are respectively connected with two inlets c; the two outlets c are respectively connected with two interfaces of a fourth switching valve (9), and the other interface of the fourth switching valve (9) is connected with a second precooling heat exchange channel; the two d outlets are respectively connected with two interfaces of a fifth switching valve (10), and the other interface of the fifth switching valve (10) is sequentially connected with a compressor (11), a water cooling device (12) and liquid CO 2 A storage tank (13);
the output end and the input end of the cooling module (14) are respectively connected with one interface of a sixth switching valve (15) and a seventh switching valve (16), the other two interfaces of the sixth switching valve (15) are respectively connected with two inlets b, and the other two interfaces of the seventh switching valve (16) are respectively connected with two outlets b;
the sublimation heat exchanger (4) and the desublimation heat exchanger (8) realize the transformation of sublimation and desublimation functions under the control of all the switching valves;
when the sublimation heat exchanger (4) has a sublimation function and the desublimation heat exchanger (8) has a desublimation function, the sublimation heat exchanger (4) is a first heat exchanger, and the desublimation heat exchanger (8) is a second heat exchanger; the first switching valve (3) is opened to the first heat exchanger and closed to the second heat exchanger; the second switching valve (5) is opened to a passage from the first heat exchanger and closed to a passage from the second heat exchanger; the third switching valve (7) is opened to the second heat exchanger and closed to the first heat exchanger; the fourth switching valve (9) is closed to the passage from the first heat exchanger and opened to the passage from the second heat exchanger; the fifth switching valve (10) and the second switching valve (5) are kept consistent; the sixth switching valve (15) and the third switching valve (7) are kept consistent; the seventh switching valve (16) and the fourth switching valve (9) are kept consistent;
when all the switching valves change direction, the sublimation heat exchanger (4) is converted into a desublimation function, and the desublimation heat exchanger (8) is converted into a sublimation function;
when the sublimation heat exchanger (4) has a sublimation function and the desublimation heat exchanger (8) has a desublimation function; the desublimation flow path comprises a dehumidifying device (1), a gas booster (2), a first switching valve (3), an a inlet of a sublimation heat exchanger (4), an a outlet of the sublimation heat exchanger (4), a second switching valve (5), a first pre-cooling heat exchange channel of a pre-cooling heat exchanger (6), a third switching valve (7), a desublimation heat exchanger (8), a fourth switching valve (9) and a second pre-cooling heat exchange channel of the pre-cooling heat exchanger (6) which are sequentially communicated; the sublimation flow path comprises an d outlet of the sublimation heat exchanger (4), a fifth switching valve (10), a compressor (11), a water cooling device (12) and liquid CO which are communicated in sequence 2 A storage tank (13).
2. According toThe switched CO of claim 1 2 The desublimation separation system is characterized in that all switching valves adopt manual switching valves or electromagnetic switching valves.
3. The switched CO of claim 1 2 The desublimation separation system is characterized in that flue gas to be treated enters the system through a dehumidifying device (1), and separated CO 2 Into liquid CO 2 The storage tank (13) is used for sealing and storing the residual clean flue gas, and the residual clean flue gas is discharged after passing through a second precooling heat exchange channel of the precooling heat exchanger (6).
4. A switched CO according to claim 3 2 The desublimation separation system is characterized in that the flue gas contains all CO generated by a coal-fired power plant or a gas-fired power plant 2 Is a smoke of the gas turbine.
5. The switched CO of claim 1 2 The desublimation separation system is characterized in that the precooling heat exchanger (6), the sublimating heat exchanger (4) and the desublimation heat exchanger (8) adopt dividing wall type heat exchangers.
6. The switched CO of claim 1 2 The desublimation separation system is characterized in that the cooling module comprises a refrigerating unit and a circulating flow path.
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| EP2212003A1 (en) * | 2007-10-12 | 2010-08-04 | Shell Internationale Research Maatschappij B.V. | Process for the separation of co2 from a gaseous feed stream |
| CN103274406B (en) * | 2013-06-13 | 2015-02-11 | 东南大学 | Novel carbon dioxide trapping device performing liquefaction and sublimation |
| CN107677044B (en) * | 2017-08-28 | 2020-06-09 | 浙江大学 | Oxygen-enriched combustion tail gas treatment system adopting low-temperature desublimation method |
| CN109078447A (en) * | 2018-10-18 | 2018-12-25 | 中国华能集团清洁能源技术研究院有限公司 | A kind of device and method of off-gas recovery dry ice |
| CN110926108A (en) * | 2019-11-28 | 2020-03-27 | 天津大学 | Middle and low temperature industrial flue gas carbon dioxide capture system |
| CN112516614A (en) * | 2020-11-17 | 2021-03-19 | 天津大学合肥创新发展研究院 | Power device flue gas carbon dioxide emission reduction system |
| CN113669175B (en) * | 2021-08-27 | 2022-11-08 | 江苏科技大学 | Low-temperature desublimated carbon capture system and method for tail gas of marine natural gas engine |
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