CN114345079B - Temperature and pressure swing adsorption device and method for capturing carbon dioxide in flue gas - Google Patents
Temperature and pressure swing adsorption device and method for capturing carbon dioxide in flue gas Download PDFInfo
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- CN114345079B CN114345079B CN202210182134.4A CN202210182134A CN114345079B CN 114345079 B CN114345079 B CN 114345079B CN 202210182134 A CN202210182134 A CN 202210182134A CN 114345079 B CN114345079 B CN 114345079B
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 530
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 270
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 270
- 239000003546 flue gas Substances 0.000 title claims abstract description 62
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims description 22
- 239000007789 gas Substances 0.000 claims abstract description 126
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 230000008929 regeneration Effects 0.000 claims abstract description 14
- 238000011069 regeneration method Methods 0.000 claims abstract description 14
- 238000003795 desorption Methods 0.000 claims abstract description 8
- 230000006835 compression Effects 0.000 claims description 100
- 238000007906 compression Methods 0.000 claims description 100
- 239000007788 liquid Substances 0.000 claims description 56
- 239000006096 absorbing agent Substances 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 239000012071 phase Substances 0.000 claims description 17
- 238000010438 heat treatment Methods 0.000 claims description 15
- 230000006837 decompression Effects 0.000 claims description 9
- 239000007791 liquid phase Substances 0.000 claims description 9
- 238000010248 power generation Methods 0.000 claims description 9
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 238000005057 refrigeration Methods 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 238000003303 reheating Methods 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004146 energy storage Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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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
-
- 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
-
- 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
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Engine Equipment That Uses Special Cycles (AREA)
Abstract
The adsorption device comprises a solar generator, a solar refrigerator, a solar collector, an organic Rankine cycle generator, a flue gas pressurizing and cooling subsystem, a carbon dioxide adsorption subsystem, a carbon dioxide desorption subsystem and a carbon dioxide liquefying subsystem. The solar energy generator provides electric energy required by the subsystem, the solar energy refrigerator provides cold energy required by condensing gaseous carbon dioxide of the carbon dioxide liquefying subsystem, the solar energy collector heats the carbon dioxide gas by using heat conduction oil, heat is provided for subsystem regeneration, and solar heat energy generated in daytime is stored; the organic Rankine cycle generator is used for replacing a solar generator at night and simultaneously is matched with the carbon dioxide liquefying subsystems to drive the subsystems to continuously work at night. The invention can realize continuous operation all weather, and has the advantages of simple operation, high load adjustment elasticity, safety, reliability, environmental protection and high energy utilization efficiency.
Description
Technical Field
The invention relates to the technical field of solar energy storage and power plant flue gas purification, in particular to a temperature and pressure swing adsorption device and a method for capturing carbon dioxide in flue gas.
Background
In recent years, with the rapid development of industrialization, environmental problems caused by the large-scale emission of carbon dioxide accompanying the consumption of a large amount of fossil fuels are increasing. At the same time, carbon dioxide as an exhaust gas is also a valuable carbon and oxygen resource, and its reserves in the earth are many times greater than the sum of natural gas, oil and coal. However, due to the unfavorable measures for recycling the carbon dioxide, the carbon dioxide which can be recycled and reused every year is less than 1% of the emission, which not only causes the pollution of the atmosphere and the greenhouse effect, but also wastes valuable resources. Therefore, carbon dioxide trapping and recycling research is widely focused at home and abroad, and has become an important direction of social and economic development in the future. In China, the absolute quantity of carbon dioxide gas emission of the flue gas of the coal-fired power plant accounts for about half of the total quantity of carbon dioxide gas emission in China. At present, the main method for capturing carbon dioxide in flue gas is to wash the flue gas by using alkaline solution to remove carbon dioxide in the flue gas. The method has the advantages of high absorption rate and good removal effect, but the consumption of the absorbent in the absorption process is large, and the heat consumption of the absorbent regeneration is also large. The heat source form of the existing flue gas carbon dioxide capturing device for the power plant mostly takes steam extracted from the power plant, flue gas waste heat and the like as a regeneration heat source, so that the power generation efficiency of the power plant is reduced. Therefore, the energy consumption of carbon dioxide trapping is reduced, the economy of the process is improved, and the method is the most main problem of flue gas carbon dioxide trapping.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a temperature and pressure swing adsorption device and a method for capturing the carbon dioxide in the flue gas, which realize the high integration of the capturing process of the carbon dioxide and the utilization of renewable energy sources, can realize the functions of efficiently separating and purifying the carbon dioxide in the flue gas of a power plant, and can fully utilize clean energy sources to realize the emission reduction task.
In order to achieve the above purpose, the present invention has the following technical scheme:
The temperature and pressure swing adsorption device comprises a solar generator, a solar refrigerator, a solar heat collector, an organic Rankine cycle generator, a flue gas pressurizing and cooling subsystem, a carbon dioxide adsorption subsystem, a carbon dioxide desorption subsystem and a carbon dioxide liquefaction subsystem, wherein the solar generator is used for providing electric energy required by the flue gas pressurizing and cooling subsystem, the carbon dioxide desorption subsystem and the carbon dioxide liquefaction subsystem, the solar refrigerator is used for providing cold energy required by the carbon dioxide liquefaction subsystem for condensing gas carbon dioxide, and the solar heat collector utilizes heat conduction oil to heat carbon dioxide gas, so as to provide heat for regeneration of the carbon dioxide absorption subsystem and store solar heat energy generated in daytime; the organic Rankine cycle generator is used for replacing a solar generator at night, and simultaneously is matched with the carbon dioxide liquefying subsystem to utilize stored liquid carbon dioxide as a working medium to drive the smoke pressurizing and cooling subsystem, the carbon dioxide adsorbing subsystem and the carbon dioxide desorbing subsystem to continuously work at night.
Preferably, the flue gas pressurizing and cooling subsystem comprises a flue gas pipeline, a third tail gas heat exchanger, a carbon dioxide heat exchanger, a first compression and expansion integrated machine, a first water cooler, a second tail gas heat exchanger, a first compressor, a second compression and expansion integrated machine, a second water cooler, a first tail gas heat exchanger and a gas-liquid separator; the tube pass of the third tail gas heat exchanger, the tube pass of the carbon dioxide heat exchanger and the compression end inlet of the first compression and expansion integrated machine are sequentially connected with a flue gas pipeline through pipelines; the outlet of the compression end of the first compression and expansion integrated machine is sequentially connected with the tube pass of the first water cooler and the tube pass of the second tail gas heat exchanger, and is respectively connected with the second water cooler, the first tail gas heat exchanger and the gas-liquid separator after being respectively connected with the compression end of the first compressor or the compression end of the second compression and expansion integrated machine.
Preferably, the carbon dioxide absorption subsystem comprises a first adsorber and a second adsorber, the carbon dioxide desorption subsystem comprises a vacuum pump, a third compression and expansion integrated machine, a carbon dioxide gas pipeline, a tail gas pipeline and a water pipeline, and the carbon dioxide liquefaction subsystem comprises a carbon dioxide heater, a second compressor, a third water cooler, a carbon dioxide condenser, a liquid carbon dioxide storage tank and a carbon dioxide evaporator; the gas phase outlet of the gas-liquid separator is connected with the lower passage of the first absorber or the second absorber, and the lower passage of the first absorber or the second absorber is connected with the compression end of the vacuum pump or the third compression and expansion integrated machine through a pipeline, and then sequentially enters the inlet of the carbon dioxide pipeline or the second compressor through the carbon dioxide heater, the bed heating pipeline of the first absorber or the second absorber and the carbon dioxide heat exchanger shell pass; the upper channel of the first absorber or the second absorber is sequentially connected with the expansion end of the first compression and expansion integrated machine, the first tail gas heat exchanger, the second tail gas heat exchanger, the third tail gas heat exchanger shell pass and the tail gas pipeline through pipelines; the outlet of the liquid carbon dioxide storage tank is sequentially connected with the carbon dioxide evaporator shell pass through a pipeline, and then is respectively connected with expansion ends of the third compression and expansion integrated machine and the second compression and expansion integrated machine, and then is connected with a carbon dioxide gas pipeline through the shell pass of the carbon dioxide heat exchanger; the shell side of the carbon dioxide heat exchanger, the shell side of the first water cooler and the shell side of the second tail gas heat exchanger are connected with a water pipeline through pipelines.
Preferably, the device of the invention further comprises a first heat conduction oil storage tank and a second heat conduction oil storage tank, wherein an inlet of the carbon dioxide heater is connected with a heat conduction oil outlet of the first heat conduction oil storage tank through a pipeline, and an outlet of the carbon dioxide heater is connected with a heat conduction oil inlet of the second heat conduction oil storage tank through a pipeline; the second heat conduction oil storage tank is connected with a heat conduction oil inlet of the solar heat collector through a pipeline; the high-temperature heat conduction oil at the output part of the heat conduction oil outlet of the solar heat collector is sequentially connected with the first heat conduction oil storage tank and the shell side of the carbon dioxide heater through pipelines, and the other part of the high-temperature heat conduction oil is connected with the first heat conduction oil storage tank through the pipelines so as to store solar heat energy generated in daytime; the first heat-conducting oil storage tank is further connected with the organic Rankine cycle power generator through a pipeline, and a heat-conducting oil outlet of the organic Rankine cycle power generator is connected with an outlet of the carbon dioxide heater and a heat-conducting oil inlet of the second heat-conducting oil storage tank.
Preferably, the device of the invention further comprises a plurality of control valves, wherein a first control valve is arranged on an inlet pipeline of a compression end of the third compression and expansion integrated machine, a fourth control valve is arranged on an outlet pipeline of the compression end of the third compression and expansion integrated machine, a second control valve is arranged on an inlet pipeline of the vacuum pump, and a third control valve is arranged on an outlet pipeline of the vacuum pump; a fifth control valve is arranged on a connecting pipeline between the second heat conduction oil storage tank and the solar heat collector; a sixth control valve is arranged on an outlet pipeline of a compression end of the second compression and expansion integrated machine, a seventh control valve is arranged on an outlet pipeline of the first compressor, an eighth control valve is arranged on an inlet pipeline of the first compressor, and a ninth control valve is arranged on an inlet pipeline of a compression end of the second compression and expansion integrated machine; a tenth control valve is arranged on an outlet pipeline of the liquid carbon dioxide storage tank; an eleventh control valve is arranged on an outlet pipeline of an expansion end of the second compression and expansion integrated machine; a twelfth control valve is arranged on a pipeline between the carbon dioxide heat exchanger and the carbon dioxide pipeline; a thirteenth control valve is arranged between the gas phase outlet of the gas-liquid separator and the lower passage of the first adsorber, and a fourteenth control valve is arranged between the gas phase outlet of the gas-liquid separator and the lower passage of the second adsorber; a fifteenth control valve and a sixteenth control valve are respectively arranged between the lower channels of the first adsorber and the second adsorber and the compression end of the vacuum pump or the third compression and expansion integrated machine; a seventeenth control valve and an eighteenth control valve are respectively arranged between the upper channels of the first adsorber and the second adsorber and the expansion end of the first compression and expansion integrated machine; a nineteenth control valve is arranged on an outlet pipeline of an expansion end of the third compression and expansion integrated machine; a twenty-first control valve and a twenty-second control valve are respectively arranged between the carbon dioxide heater and the bed heating pipeline of the first adsorber and the bed heating pipeline of the second adsorber; a twenty-second control valve is arranged on a pipeline between the carbon dioxide heat exchanger and the second compressor; and a twenty-third control valve is arranged on a pipeline between the first heat conduction oil storage tank and the organic Rankine cycle power generator.
Preferably, the solar power generator is connected to the vacuum pump, the first compressor and the second compressor through cables.
Preferably, the organic rankine cycle generator is connected to the vacuum pump, the first compressor, and the second compressor through cables.
Preferably, the organic working medium gas phase outlet of the organic Rankine cycle generator is connected with the tube side inlet of the carbon dioxide evaporator through a pipeline, and the organic working medium liquid phase inlet of the organic Rankine cycle generator is connected with the tube side outlet of the carbon dioxide evaporator through a pipeline.
Preferably, the solar refrigerator is circularly connected with the tube side of the carbon dioxide condenser through a pipeline.
Based on the control method of the temperature and pressure swing adsorption device for capturing the carbon dioxide in the flue gas, the following processes are executed by controlling the on-off of the control valve:
In the sunshine time, the solar power generator and the solar refrigerator are in power generation and refrigeration working states, and the organic Rankine cycle power generator is in a closed state; the normal-temperature and normal-pressure flue gas sequentially enters a tube pass of a third tail gas heat exchanger, a carbon dioxide heat exchanger, a compression end of a first compression and expansion integrated machine, a tube pass of a first water cooler, a tube pass of a second tail gas heat exchanger, a first compressor, a second water cooler, a tube pass of the first tail gas heat exchanger and a gas-liquid separator, and the flue gas is pressurized and cooled step by step; then, the high-pressure low-temperature flue gas enters a first adsorber or a second adsorber, and carbon dioxide in the flue gas is adsorbed until the adsorption is saturated; the high-pressure low-temperature tail gas after carbon dioxide removal enters an expansion end of a first compression and expansion integrated machine, and after expansion, decompression and temperature reduction, the low-temperature normal-pressure tail gas sequentially enters shell passes of a first tail gas heat exchanger, a second tail gas heat exchanger and a third tail gas heat exchanger to provide cooling capacity for flue gas, and the normal-temperature normal-pressure tail gas after reheating and temperature rising is sent out of a boundary region through a tail gas pipeline; the first absorber or the second absorber reaching the saturation state is vacuumized through a vacuum pump, adsorbed carbon dioxide is desorbed, the carbon dioxide is regenerated, the desorbed carbon dioxide sequentially enters a shell side of a carbon dioxide heater, a bed heating pipeline of the first absorber or the second absorber, a shell side of a carbon dioxide heat exchanger reaches an inlet of a carbon dioxide gas pipeline or a second compressor, part of carbon dioxide gas is sent out of a boundary region, after the rest part of carbon dioxide gas is pressurized, the carbon dioxide gas sequentially passes through a third water cooler and a shell side of a carbon dioxide condenser to reach a carbon dioxide storage tank or a carbon dioxide liquid pipeline, the carbon dioxide gas is cooled and condensed into liquid step by step, part of liquid enters the tank region to be stored, and the part of carbon dioxide gas is sent out of the boundary region; the solar refrigerator is communicated with the tube side of the carbon dioxide condenser to provide cold energy for condensing gaseous carbon dioxide; the heat conducting oil outlet part of the solar heat collector is sequentially connected with the first heat conducting oil storage tank and the shell side of the carbon dioxide heater to heat carbon dioxide gas, heat is provided for regeneration of the first adsorber or the second adsorber, and the other part of high-temperature heat conducting oil is introduced into the first heat conducting oil storage tank to store solar heat energy generated in daytime; the solar generator provides electric energy for the vacuum pump, the first compressor and the second compressor;
In the non-sunshine time, the solar power generator, the solar refrigerator and the second compressor are all in a closed state, the organic Rankine cycle power generator is in a power generation state, and the organic Rankine cycle power generator replaces the solar power generator to provide electric energy for the vacuum pump and the first compressor; after the primary decompression, the liquid carbon dioxide in the liquid carbon dioxide storage tank is sent to a shell side of a carbon dioxide evaporator for evaporation, and the obtained high-pressure carbon dioxide gas is respectively sent to an expansion end of a second compression and expansion integrated machine and an expansion end of a third compression and expansion integrated machine to drive the compression ends to work, so that the load of a first compressor and a vacuum pump in sunshine time is partially replaced, and the residual load is completed by driving the operation of the first compressor and the vacuum pump by an organic Rankine cycle generator; carbon dioxide gas subjected to expansion, decompression and cooling enters a shell pass of a carbon dioxide heat exchanger, and is sent out of a boundary region through a carbon dioxide gas pipeline after cold energy is recovered; the heating working medium of the carbon dioxide evaporator tube is from an organic working medium gas phase outlet of the organic Rankine cycle power generator, and after the gas phase organic working medium is condensed into a liquid phase through heat exchange, the organic working medium liquid phase returns to an organic working medium liquid phase inlet of the organic Rankine cycle power generator; the first heat conducting oil storage tank provides high-temperature heat conducting oil for the organic Rankine cycle power generator, the temperature is reduced after the heat supply task is completed, and the high-temperature heat conducting oil is converged with low-temperature heat conducting oil from the shell side of the carbon dioxide heater and is sent to the second heat conducting oil storage tank for storage.
Compared with the prior art, the invention has at least the following beneficial effects:
The method has the advantages of simple operation, high load adjustment elasticity, safety, reliability, environmental friendliness and high energy utilization efficiency, can greatly improve the economy of capturing the flue gas and the carbon dioxide, and is suitable for being applied to engineering. The temperature and pressure swing adsorption device for capturing the carbon dioxide in the flue gas replaces the traditional energy with solar energy, fully utilizes the cleanliness and the reproducibility of renewable energy sources to capture the carbon dioxide, and effectively improves the economy and the environmental friendliness of the process.
Furthermore, the adsorption device further comprises a first heat conduction oil storage tank and a second heat conduction oil storage tank, solar heat energy generated in daytime of the solar heat collector is stored through switching operation of the two heat conduction oil storage tanks, and is provided for carbon dioxide gas heating for regeneration and use of night operation of the organic Rankine cycle generator, so that traditional steam consumption is saved.
Furthermore, the invention stores the cold energy generated in the daytime of the solar refrigerator through condensation, liquefaction and storage of the carbon dioxide gas, and is used for the night operation of the organic Rankine cycle power generator, and the high-pressure carbon dioxide gas generated by gasification of the solar refrigerator can drive the compression end of the third compression and expansion integrated machine to work at night, so that the solar energy storage function is realized.
Furthermore, the heating coil is arranged in the adsorbent bed layer of the adsorber, high-temperature carbon dioxide gas in the tube is used as a heat carrier to provide heat for the regeneration operation of the adsorber, the high temperature generated by the heating coil is beneficial to the desorption of carbon dioxide, the requirement of the regeneration operation on the vacuum degree can be effectively reduced, namely, the power consumption in the regeneration process can be saved.
Furthermore, the low-temperature flue gas after carbon dioxide removal is realized in the adsorption device of the invention and then is subjected to heat exchange with the flue gas through the three-stage flue gas heat exchanger, so that the heat utilization efficiency is improved.
Furthermore, the adsorption device can effectively recover the pressure potential energy of tail gas and carbon dioxide through the expansion ends of the three compression and expansion integrated machines, and is used for driving the compression ends to do work, so that the electricity consumption is saved.
Drawings
FIG. 1 is a schematic diagram of a temperature and pressure swing adsorption device for capturing carbon dioxide in flue gas;
In the accompanying drawings: 1-a solar power generator; 2-solar refrigerator; 3-a first compression and expansion integrated machine; 4-a first compressor; 5-a first water cooler; 6-a second water cooler; 7-a first tail gas heat exchanger; 8-carbon dioxide heat exchanger; 9-a first adsorber; 10-a second adsorber; 11-a second compression and expansion integrated machine; 12-a vacuum pump; 13-a third compression and expansion integrated machine; 14-a liquid carbon dioxide storage tank; 15-a second compressor; a 16-carbon dioxide evaporator; 17-carbon dioxide condenser; 18-a third water cooler; 19-a gas-liquid separator; 20-a second tail gas heat exchanger; 21-an organic rankine cycle generator; 22-a first conduction oil storage tank; 23-a third tail gas heat exchanger; 24-solar collector; 25-a second conduction oil storage tank; 30-a first control valve; 31-a second control valve; 32-a third control valve; 33-fourth control valve; 34-a fifth control valve; 35-sixth control valve; 36-seventh control valve; 37-eighth control valve; 38-ninth control valve; 39-tenth control valve; 40-eleventh control valve; 41-twelfth control valve; 42-thirteenth control valve; 43-fourteenth control valve; 44-fifteenth control valve; 45-sixteenth control valve; 46-seventeenth control valve; 47-eighteenth control valve; 48-nineteenth control valve; 49-twentieth control valve; 50-twenty-first control valve; 51-twenty-second control valve; 52-twenty-third control valve; 60-flue gas pipeline; 61-carbon dioxide gas pipeline; 62-carbon dioxide liquid conduit; 63-an off-gas pipeline; 64-water pipeline.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
Referring to fig. 1, the temperature and pressure swing adsorption device for capturing carbon dioxide in flue gas of the present invention has the following structure:
The inlet of the compression end of the first compression and expansion integrated machine 3 is sequentially connected with the tube pass of the carbon dioxide heat exchanger 8 and the third tail gas heat exchanger 23 and the flue gas pipeline 60 through pipelines, the outlet of the compression end of the first compression and expansion integrated machine 3 is sequentially connected with the tube pass of the first water cooler 5, the tube pass of the second tail gas heat exchanger 20, the compression end of the first compressor 4 or the second compression and expansion integrated machine 11, the second water cooler 6, the tube pass of the first tail gas heat exchanger 7, the gas phase outlet of the gas-liquid separator 19 and the lower passage of the first absorber 9 or the second absorber 10 through pipelines and valves, and the lower passage of the first absorber 9 or the lower passage of the second absorber 1 is sequentially connected with the vacuum pump 12 or the compression end of the third compression and expansion integrated machine 13 through pipelines and valves, The bed heating pipeline of the carbon dioxide heater 26, the first absorber 9 or the second absorber 10, the shell pass of the carbon dioxide heat exchanger 8, the carbon dioxide pipeline 61 or the inlet of the second compressor 15 are connected, the upper channel is sequentially connected with the expansion end of the first compression and expansion integrated machine 3, the shell pass of the first tail gas heat exchanger 7 and the second tail gas heat exchanger 20 and the tail gas pipeline 63 through pipelines and valves, the outlet of the second compressor 15 is sequentially connected with the third water cooler 18, the shell pass of the carbon dioxide condenser 17 and the liquid carbon dioxide storage tank 14 through pipelines, and the outlet of the liquid carbon dioxide storage tank 1 is sequentially connected with the shell pass of the carbon dioxide evaporator 16 through pipelines and valves, The expansion end of the second compression and expansion integrated machine 11 and the third compression and expansion integrated machine 13, the shell side of the carbon dioxide heat exchanger 8 and the carbon dioxide gas pipeline 61 are connected, the shell side of the carbon dioxide heat exchanger 8, the shell side of the first 5 water cooler, the shell side of the second tail gas heat exchanger 20 and the liquid discharge ports of the gas-liquid separator 19 are connected with the water pipeline 64 through pipelines, the inlet of the carbon dioxide heater 26 is connected with the heat conduction oil outlet of the first heat conduction oil storage tank 22 through a pipeline, and the outlet of the carbon dioxide heater is connected with the heat conduction oil inlet of the second heat conduction oil storage tank 25 through a pipeline. The outlet of the solar refrigerator 2 is connected with the tube side inlet of the carbon dioxide condenser 17 through a pipeline, and the inlet of the solar refrigerator is connected with the tube side outlet of the carbon dioxide condenser 17 through a pipeline. The heat conducting oil outlet of the solar heat collector 24 is sequentially connected with the first heat conducting oil storage tank 22, the heat conducting oil channel of the organic Rankine cycle generator 21 and the second heat conducting oil storage tank 25 through pipelines and valves, the heat conducting oil inlet of the organic Rankine cycle generator 21 is connected with the outlet of the second heat conducting oil storage tank 25 through pipelines and valves, the organic working medium gas phase outlet of the organic Rankine cycle generator 21 is connected with the tube side inlet of the carbon dioxide evaporator 16 through a pipeline, and the organic working medium liquid phase inlet of the organic Rankine cycle generator is connected with the tube side outlet of the carbon dioxide evaporator 16 through a pipeline. The solar generator 1 is connected with the vacuum pump 12, the first compressor 4 and the second compressor 15 through cables, the organic Rankine cycle generator 21 is also connected with the vacuum pump 12, the first compressor 4 and the second compressor 15 through cables, the daytime power generation capacity of the solar generator 1 can meet the daytime power consumption requirement of the first compressor 4 and the second compressor 15 and the vacuum pump 12, the nighttime (i.e. in non-sunshine time) power generation capacity of the organic Rankine cycle generator 21 can meet the nighttime power consumption requirement of the first compressor 4 and the second compressor 15 and the vacuum pump 12, the heat generated by the solar collector 1 day can meet the nighttime operation requirement of the carbon dioxide heater 26 and the organic Rankine cycle generator 21, the solar refrigerator 2 daytime refrigeration capacity meets the refrigeration capacity demand of the carbon dioxide condenser 17, including the product sales, and the total amount of liquid carbon dioxide required to maintain the organic rankine cycle generator 21, the second compression expansion integrated machine 11, and the third compression expansion integrated machine 13 during night time operation.
A control method based on the temperature and pressure swing adsorption device for capturing the carbon dioxide in the flue gas, which comprises the following steps:
During the daytime (sunlight time), both the solar power generator 1 and the solar refrigerator 2 are in normal power generation and refrigeration operation states, and the organic rankine cycle power generator 21 is in an off state. The first control valve 30, the fourth control valve 33, the sixth control valve 35, the ninth control valve 38, the eleventh control valve 40, the nineteenth control valve 48, and the twenty-third control valve 52 are closed, and the remaining valves are all opened. Firstly, the normal-temperature and normal-pressure flue gas sequentially enters the tube side of the third tail gas heat exchanger 23, the carbon dioxide heat exchanger 8, the compression end of the first compression and expansion integrated machine 3, the first water cooler 5, the tube side of the third tail gas heat exchanger 20, the first compressor 4, the second water cooler 6 and the tube side and gas-liquid separator 19 of the first tail gas heat exchanger 7 through the flue gas pipeline 60 and the valve connection, and the flue gas is pressurized and cooled step by step; then, the high-pressure low-temperature flue gas enters the first absorber 9 or the second absorber 10 through a pipeline and a valve, and carbon dioxide in the flue gas is absorbed until the absorption is saturated; the high-pressure low-temperature tail gas after carbon dioxide removal enters an expansion end of the first compression and expansion integrated machine 3 through a pipeline connection, and after expansion, decompression and temperature reduction, the low-temperature normal-pressure tail gas sequentially enters shell passes of the first tail gas heat exchanger 7, the third tail gas heat exchanger 20 and the second tail gas heat exchanger 23 through pipeline connection, so as to provide cold energy for flue gas, and the normal-temperature normal-pressure tail gas after reheating and temperature rising is sent out of a boundary region through a tail gas pipeline 63; the first absorber 9 or the second absorber 10 reaching the saturation state is vacuumized through a vacuum pump 12 connected through a pipeline and a valve, adsorbed carbon dioxide is desorbed, so that the carbon dioxide is regenerated, the desorbed carbon dioxide sequentially enters a shell side of a carbon dioxide heater 26, a bed heating pipeline of the first absorber 9 or the second absorber 10, a shell side of a carbon dioxide heat exchanger 23, a carbon dioxide pipeline 61 or a second compressor inlet connection 15 through the pipeline and the valve, part of carbon dioxide is sent out of a boundary region, after the rest part of the carbon dioxide is pressurized, the carbon dioxide sequentially passes through a third water cooler 18, a shell side of a carbon dioxide condensation 17 and a liquid carbon dioxide storage tank 14 or a carbon dioxide liquid pipeline 62 through the pipeline connection, the carbon dioxide is gradually cooled and condensed into liquid, part of the liquid enters the tank region to be stored, and the part of the liquid is sent out of the boundary region; the outlet of the solar refrigerator 2 is connected with the tube side inlet of the carbon dioxide condenser 17 through a pipeline, and the inlet of the solar refrigerator is connected with the tube side inlet of the carbon dioxide condenser 17 through a pipeline to provide cold for condensing gaseous carbon dioxide; the heat conducting oil outlet part of the solar heat collector 24 is sequentially connected with the first heat conducting oil storage tank 22 and the shell side of the carbon dioxide heater 26 through a pipeline and a valve, heats carbon dioxide gas, provides heat for the regeneration of the first adsorber 9 or the second adsorber 10, and the high-temperature heat conducting oil of the rest part is connected with the first heat conducting oil storage tank 22 through the pipeline to store solar heat energy generated in daytime; in the above process, the solar power generator 1 is connected to the vacuum pump 12, the first compressor 4 and the second compressor 15 through cables to supply electric power thereto.
During the night (non-sunlight time), the solar power generator 1, the solar refrigerator 2 and the second compressor 15 are all in the off state, and the organic rankine cycle power generator 21 is in the power generation state. The fifth control valve 34 and the twenty-second control valve 51 are closed and the remaining valves are all opened. The organic rankine cycle generator 21 replaces the solar generator 1, and is connected with the vacuum pump 12 and the first compressor 4 through cables to supply electric energy thereto; meanwhile, after the primary decompression of the liquid carbon dioxide in the carbon dioxide storage tank 14, the liquid carbon dioxide is sent into the shell side of the carbon dioxide evaporator 16 for evaporation through the pipeline connection, the obtained high-pressure carbon dioxide gas enters the expansion end of the second compression and expansion integrated machine 11 and the expansion end of the third compression and expansion integrated machine 13 through the pipeline connection respectively to drive the compression ends to work, so that the aim of partially replacing the load of the first compressor 4 and the vacuum pump 12 in the daytime process is fulfilled, and the residual load is finished by driving the operation of the first compressor 4 and the vacuum pump 12 at night through the Rankine cycle generator 21; the carbon dioxide gas after expansion, decompression and cooling is connected to the shell side of the carbon dioxide heat exchanger 8 through a pipeline, and the carbon dioxide gas is sent out of the boundary region through a carbon dioxide gas pipeline 61 after the cold energy is recovered; the heating medium on the tube side of the carbon dioxide evaporator 16 comes from an organic working medium gas phase outlet of the organic rankine cycle generator 21 connected through a pipeline, and after being condensed through heat exchange, the organic working medium phase is returned to an organic working medium phase inlet of the organic rankine cycle generator 21 through the pipeline connection; the first heat-conducting oil storage tank 22 is connected with a valve through a pipeline to provide high-temperature heat-conducting oil for the organic Rankine cycle power generator 21, after the heat supply task is completed, the temperature of the heat-conducting oil is reduced, and then the low-temperature heat-conducting oil from the shell side of the carbon dioxide heater 26 is converged through the pipeline connection and is sent to the second heat-conducting oil storage tank 25 to be stored.
In the above process, when the first adsorber 9 is in the adsorption state, the thirteenth control valve 42 and the seventeenth control valve 46 are opened, and the fifteenth control valve 44, the eighteenth control valve 47, and the twenty-first control valve 50 are closed; the second adsorber 10 is in the regeneration state with the sixteenth control valve 45 and the twentieth control valve 49 open and the fourteenth control valve 43, the fifteenth control valve 44 and the eighteenth control valve 47 closed; when the first adsorber 9 is saturated with adsorption, the thirteenth, sixteenth and seventeenth control valves 42, 45 and 46 are switched to the regeneration state by the fifteenth, twenty-first and twenty-first control valves 44, 50 being opened, and the second adsorber 10 is correspondingly switched to the adsorption state, the fourteenth, sixteenth and twenty-first control valves 43, 47 being opened, and the thirteenth, sixteenth and twentieth control valves 42, 45 and 49 being closed. The operation is switched to each other repeatedly, so that the continuous and stable operation of the system is realized.
Meanwhile, in the process, water from the carbon dioxide heat exchanger 8 shell pass, the first water cooler shell pass 5, the second tail gas heat exchanger shell pass 20 and the liquid outlet of the gas-liquid separator 19 are converged together, and are connected with a water pipeline 64 through a pipeline to be sent out of the boundary region.
According to the analysis, the temperature and pressure swing adsorption device for capturing the carbon dioxide in the flue gas, disclosed by the invention, has the advantages of simplicity in operation, high load adjustment elasticity, safety and reliability, environment friendliness and high energy utilization efficiency, can greatly improve the economy of capturing the carbon dioxide in the flue gas, and is suitable for being applied to engineering, and finally, the adsorption device capable of realizing continuous operation in all weather can be obtained.
The foregoing is a further detailed description of the present invention in connection with the preferred embodiments, and it is not to be construed as limiting the invention to the preferred embodiments, but rather as merely enabling those skilled in the art to which the invention pertains without departing from its spirit and scope.
Claims (8)
1. A temperature and pressure swing adsorption device for flue gas carbon dioxide entrapment which characterized in that: the solar energy system comprises a solar energy generator (1), a solar energy refrigerator (2), a solar energy heat collector (24), an organic Rankine cycle generator (21) and a flue gas pressurizing and cooling subsystem, a carbon dioxide adsorption subsystem, a carbon dioxide desorption subsystem and a carbon dioxide liquefaction subsystem which are connected, wherein the solar energy generator (1) is used for providing electric energy required by the flue gas pressurizing and cooling subsystem, the carbon dioxide desorption subsystem and the carbon dioxide liquefaction subsystem, the solar energy refrigerator (2) is used for providing cold energy required by the carbon dioxide liquefaction subsystem for condensing gas carbon dioxide, the solar energy heat collector (24) heats the carbon dioxide gas by utilizing heat conduction oil, heat is provided for regeneration of the carbon dioxide adsorption subsystem, and solar heat energy generated in daytime is stored; the organic Rankine cycle generator (21) is used for replacing the solar generator (1) at night, and simultaneously is matched with the carbon dioxide liquefying subsystem to drive the smoke pressurizing and cooling subsystem, the carbon dioxide adsorbing subsystem and the carbon dioxide desorbing subsystem to continuously work at night by using the stored liquid carbon dioxide as a working medium;
After the smoke at normal temperature and normal pressure is pressurized and cooled step by step through the smoke pressurizing and cooling subsystem, carbon dioxide in the smoke is adsorbed by the carbon dioxide absorbing and adsorbing system, and then the adsorbed carbon dioxide is desorbed through the carbon dioxide desorbing subsystem, and the desorbed carbon dioxide is cooled step by step and condensed into liquid by the carbon dioxide liquefying subsystem;
The carbon dioxide liquefying subsystem comprises a liquid carbon dioxide storage tank (14) and a carbon dioxide evaporator (16), the flue gas pressurizing and cooling subsystem comprises a second compression and expansion integrated machine (11), and the carbon dioxide desorbing subsystem comprises a third compression and expansion integrated machine (13); in non-sunshine time, after the liquid carbon dioxide in the liquid carbon dioxide storage tank (14) is initially decompressed, the liquid carbon dioxide is sent into a shell side of a carbon dioxide evaporator (16) for evaporation, and the obtained high-pressure carbon dioxide gas respectively enters an expansion end of the second compression and expansion integrated machine (11) and an expansion end of the third compression and expansion integrated machine (13) to drive the compression ends of the second compression and expansion integrated machine to work;
The flue gas pressurizing and cooling subsystem comprises a flue gas pipeline (60), a third tail gas heat exchanger (23), a carbon dioxide heat exchanger (8), a first compression and expansion integrated machine (3), a first water cooler (5), a second tail gas heat exchanger (20), a first compressor (4), a second compression and expansion integrated machine (11), a second water cooler (6), a first tail gas heat exchanger (7) and a gas-liquid separator (19); the third tail gas heat exchanger (23), the tube side of the carbon dioxide heat exchanger (8) and the compression end inlet of the first compression and expansion integrated machine (3) are sequentially connected with a flue gas pipeline (60) through pipelines; the outlet of the compression end of the first compression and expansion integrated machine (3) is sequentially connected with the tube passes of the first water cooler (5) and the second tail gas heat exchanger (20), and is respectively connected with the compression end of the first compressor (4) or the compression end of the second compression and expansion integrated machine (11) and then sequentially connected with the second water cooler (6), the first tail gas heat exchanger (7) and the gas-liquid separator (19);
The carbon dioxide absorption subsystem comprises a first adsorber (9) and a second adsorber (10), the carbon dioxide desorption subsystem comprises a vacuum pump (12), a third compression and expansion integrated machine (13), a carbon dioxide gas pipeline (61) and a tail gas pipeline (63), and the carbon dioxide liquefaction subsystem comprises a carbon dioxide heater (26), a second compressor (15), a third water cooler (18), a carbon dioxide condenser (17), a liquid carbon dioxide storage tank (14) and a carbon dioxide evaporator (16); the gas phase outlet of the gas-liquid separator (19) is connected with the lower passage of the first absorber (9) or the second absorber (10), the lower passage of the first absorber (9) or the second absorber (10) is also connected with the compression end of the vacuum pump (12) or the third compression and expansion integrated machine (13) through a pipeline, and then enters the inlet of the carbon dioxide gas pipeline (61) or the inlet of the second compressor (15) through the carbon dioxide heater (26), the bed heating pipeline of the first absorber (9) or the second absorber (10) and the shell side of the carbon dioxide heat exchanger (8) in sequence; the upper channel of the first absorber (9) or the second absorber (10) is sequentially connected with the expansion end of the first compression and expansion integrated machine (3), the first tail gas heat exchanger (7), the second tail gas heat exchanger (20) and the third tail gas heat exchanger (23) through pipelines, and the shell side of the first tail gas heat exchanger is connected with a tail gas pipeline (63); the outlet of the second compressor (15) is sequentially connected with a third water cooler (18), a carbon dioxide condenser (17) shell pass and a liquid carbon dioxide storage tank (14) through pipelines, the outlet of the liquid carbon dioxide storage tank (14) is sequentially connected with the carbon dioxide evaporator (16) shell pass through pipelines, and then is respectively connected with expansion ends of the third compression and expansion integrated machine (13) and the second compression and expansion integrated machine (11) and is further connected with a carbon dioxide pipeline (61) through the carbon dioxide heat exchanger (8) shell pass.
2. The temperature and pressure swing adsorption device for flue gas carbon dioxide capture of claim 1, wherein: the device further comprises a first heat-conducting oil storage tank (22) and a second heat-conducting oil storage tank (25), wherein an inlet of the carbon dioxide heater (26) is connected with a heat-conducting oil outlet of the first heat-conducting oil storage tank (22) through a pipeline, and an outlet of the carbon dioxide heater (26) is connected with a heat-conducting oil inlet of the second heat-conducting oil storage tank (25) through a pipeline; the second heat conduction oil storage tank (25) is connected with a heat conduction oil inlet of the solar heat collector (24) through a pipeline; the high-temperature heat conduction oil at the output part of the heat conduction oil outlet of the solar heat collector (24) is sequentially connected with the first heat conduction oil storage tank (22) and the shell side of the carbon dioxide heater (26) through pipelines, and the other part of the high-temperature heat conduction oil is connected with the first heat conduction oil storage tank (22) through the pipelines so as to store solar heat energy generated in daytime; the first heat conduction oil storage tank (22) is further connected with the organic Rankine cycle power generator (21) through a pipeline, and a heat conduction oil outlet of the organic Rankine cycle power generator (21) is connected with an outlet of the carbon dioxide heater (26) and a heat conduction oil inlet of the second heat conduction oil storage tank (25).
3. The temperature and pressure swing adsorption apparatus for flue gas carbon dioxide capture of claim 2, wherein: the system further comprises a plurality of control valves, wherein a first control valve (30) is arranged on an inlet pipeline of a compression end of the third compression and expansion integrated machine (13), a fourth control valve (33) is arranged on an outlet pipeline of the compression end of the third compression and expansion integrated machine (13), a second control valve (31) is arranged on an inlet pipeline of the vacuum pump (12), and a third control valve (32) is arranged on an outlet pipeline of the vacuum pump (12); a fifth control valve (34) is arranged on a connecting pipeline between the second heat conduction oil storage tank (25) and the solar heat collector (24); a sixth control valve (35) is arranged on an outlet pipeline of a compression end of the second compression and expansion integrated machine (11), a seventh control valve (36) is arranged on an outlet pipeline of the first compressor (4), an eighth control valve (37) is arranged on an inlet pipeline of the first compressor (4), and a ninth control valve (38) is arranged on an inlet pipeline of the compression end of the second compression and expansion integrated machine (11); a tenth control valve (39) is arranged on an outlet pipeline of the liquid carbon dioxide storage tank (14); an eleventh control valve (40) is arranged on an outlet pipeline of the expansion end of the second compression and expansion integrated machine (11); a twelfth control valve (41) is arranged on a pipeline between the carbon dioxide heat exchanger (8) and the carbon dioxide pipeline (61); a thirteenth control valve (42) is arranged between the gas phase outlet of the gas-liquid separator (19) and the lower passage of the first adsorber (9), and a fourteenth control valve (43) is arranged between the gas phase outlet of the gas-liquid separator (19) and the lower passage of the second adsorber (10); a fifteenth control valve (44) and a sixteenth control valve (45) are respectively arranged between the lower channels of the first adsorber (9) and the second adsorber (10) and the compression end of the vacuum pump (12) or the third compression and expansion integrated machine (13); a seventeenth control valve (46) and an eighteenth control valve (47) are respectively arranged between the upper channels of the first adsorber (9) and the second adsorber (10) and the expansion end of the first compression and expansion integrated machine (3); a nineteenth control valve (48) is arranged on an outlet pipeline of an expansion end of the third compression and expansion integrated machine (13); a twenty-first control valve (50) and a twenty-second control valve (49) are respectively arranged between the carbon dioxide heater (26) and the bed heating pipelines of the first adsorber (9) and the second adsorber (10); a twenty-second control valve (51) is arranged on a pipeline between the carbon dioxide heat exchanger (8) and the second compressor (15); a twenty-third control valve (52) is arranged on a pipeline between the first heat conduction oil storage tank (22) and the organic Rankine cycle generator (21).
4. The temperature and pressure swing adsorption device for flue gas carbon dioxide capture of claim 1, wherein: the solar power generator (1) is connected with the vacuum pump (12), the first compressor (4) and the second compressor (15) through cables.
5. The temperature and pressure swing adsorption device for flue gas carbon dioxide capture of claim 1, wherein: the organic Rankine cycle generator (21) is connected with the vacuum pump (12), the first compressor (4) and the second compressor (15) through cables.
6. The temperature and pressure swing adsorption device for flue gas carbon dioxide capture of claim 1, wherein: the organic working medium gas phase outlet of the organic Rankine cycle generator (21) is connected with the tube side inlet of the carbon dioxide evaporator (16) through a pipeline, and the organic working medium liquid phase inlet of the organic Rankine cycle generator is connected with the tube side outlet of the carbon dioxide evaporator (16) through a pipeline.
7. The temperature and pressure swing adsorption device for flue gas carbon dioxide capture of claim 1, wherein: the solar refrigerator (2) is circularly connected with the tube side of the carbon dioxide condenser (17) through a pipeline.
8. A control method based on the temperature and pressure swing adsorption device for flue gas carbon dioxide capture according to claim 3, characterized in that the following procedure is performed by manipulating the on-off of the control valve:
In the sunshine time, the solar power generator (1) and the solar refrigerator (2) are in power generation and refrigeration working states, and the organic Rankine cycle power generator (21) is in a closed state; the normal-temperature normal-pressure flue gas sequentially enters a tube side of a third tail gas heat exchanger (23), a carbon dioxide heat exchanger (8), a compression end of a first compression and expansion integrated machine (3), a first water cooler (5), a tube side of a second tail gas heat exchanger (20), a first compressor (4), a second water cooler (6) and a tube side and gas-liquid separator (19) of a first tail gas heat exchanger (7), and the flue gas is pressurized and cooled step by step; then, the high-pressure low-temperature flue gas enters a first absorber (9) or a second absorber (10), and carbon dioxide in the flue gas is absorbed until the absorption is saturated; the high-pressure low-temperature tail gas after carbon dioxide removal enters an expansion end of a first compression and expansion integrated machine (3), after being subjected to expansion, decompression and temperature reduction, the low-temperature normal-pressure tail gas sequentially enters shell passes of a first tail gas heat exchanger (7), a second tail gas heat exchanger (20) and a third tail gas heat exchanger (23), cooling capacity is provided for flue gas, and normal-temperature normal-pressure tail gas after reheating and temperature rising is sent out of a boundary region through a tail gas pipeline (63); the first absorber (9) or the second absorber (10) reaching a saturated state is vacuumized through a vacuum pump (12), adsorbed carbon dioxide is desorbed to be regenerated, the desorbed carbon dioxide sequentially enters a shell side of a carbon dioxide heater (26), a bed heating pipeline of the first absorber (9) or the second absorber (10), a shell side of a carbon dioxide heat exchanger (8) reaches an inlet of a carbon dioxide gas pipeline (61) or a second compressor (15), part of carbon dioxide gas is sent out of a boundary region, the rest part of carbon dioxide gas is pressurized and then sequentially passes through a third water cooler (18) and a shell side of a carbon dioxide condenser (17) to reach a carbon dioxide storage tank (14) or a carbon dioxide liquid pipeline (62), the carbon dioxide gas is cooled and condensed into liquid step by step, and part of liquid enters the tank region to be stored and part of carbon dioxide gas is sent out of the boundary region; the solar refrigerator (2) is communicated with the tube side of the carbon dioxide condenser (17) to provide cold energy for condensing gaseous carbon dioxide; the heat conducting oil outlet part of the solar heat collector (24) is sequentially connected with the first heat conducting oil storage tank (22) and the shell side of the carbon dioxide heater (26), carbon dioxide gas is heated, heat is provided for regeneration of the first adsorber (9) or the second adsorber (10), and the other part of high-temperature heat conducting oil is introduced into the first heat conducting oil storage tank (22) to store solar heat energy generated in daytime; the solar generator (1) provides electric energy for the vacuum pump (12), the first compressor (4) and the second compressor (15);
In non-sunlight time, the solar power generator (1), the solar refrigerator (2) and the second compressor (15) are all in a closed state, the organic Rankine cycle power generator (21) is in a power generation state, and the organic Rankine cycle power generator (21) replaces the solar power generator (1) to provide electric energy for the vacuum pump (12) and the first compressor (4); after the primary decompression of the liquid carbon dioxide in the liquid carbon dioxide storage tank (14), the liquid carbon dioxide is sent into a shell side of a carbon dioxide evaporator (16) for evaporation, the obtained high-pressure carbon dioxide gas is respectively sent into an expansion end of a second compression and expansion integrated machine (11) and an expansion end of a third compression and expansion integrated machine (13) to drive the compression ends to work, the load of a first compressor (4) and a vacuum pump (12) in sunshine time is partially replaced, and the residual load is completed by driving the operation of the first compressor (4) and the vacuum pump (12) by an organic Rankine cycle generator (21); carbon dioxide gas subjected to expansion, decompression and cooling enters a shell side of a carbon dioxide heat exchanger (8), and after cooling capacity is recovered, the carbon dioxide gas is sent out of a boundary region through a carbon dioxide gas pipeline (61); the heating working medium of the tube side of the carbon dioxide evaporator (16) comes from an organic working medium gas phase outlet of the organic Rankine cycle generator (21), and after the gas phase organic working medium is condensed into a liquid phase through heat exchange, the organic working medium liquid phase returns to an organic working medium liquid phase inlet of the organic Rankine cycle generator (21); the first heat conducting oil storage tank (22) provides high-temperature heat conducting oil for the organic Rankine cycle power generator (21), the temperature is reduced after the heat supply task is completed, and the low-temperature heat conducting oil from the shell side of the carbon dioxide heater (26) is collected and sent to the second heat conducting oil storage tank (25) for storage.
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