CN118526923B - Carbon dioxide adsorption system - Google Patents
Carbon dioxide adsorption system Download PDFInfo
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- CN118526923B CN118526923B CN202410986488.3A CN202410986488A CN118526923B CN 118526923 B CN118526923 B CN 118526923B CN 202410986488 A CN202410986488 A CN 202410986488A CN 118526923 B CN118526923 B CN 118526923B
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 178
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 142
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 90
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 85
- 238000011084 recovery Methods 0.000 claims abstract description 49
- 239000002994 raw material Substances 0.000 claims abstract description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 87
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 24
- 239000003546 flue gas Substances 0.000 claims description 24
- 239000003463 adsorbent Substances 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 13
- 238000003795 desorption Methods 0.000 claims description 9
- 239000012621 metal-organic framework Substances 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 239000002808 molecular sieve Substances 0.000 claims description 6
- 239000000741 silica gel Substances 0.000 claims description 6
- 229910002027 silica gel Inorganic materials 0.000 claims description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 238000005336 cracking Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 30
- 238000005265 energy consumption Methods 0.000 abstract description 26
- 230000008569 process Effects 0.000 abstract description 14
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 238000010521 absorption reaction Methods 0.000 description 8
- 230000006835 compression Effects 0.000 description 8
- 238000007906 compression Methods 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 239000012263 liquid product Substances 0.000 description 6
- 230000007613 environmental effect Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 238000004146 energy storage Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000005201 scrubbing Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000003252 repetitive effect Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
- B01D53/0476—Vacuum pressure swing adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0027—Oxides of carbon, e.g. CO2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
-
- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/64—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end by pressure-swing adsorption [PSA] at the hot end
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/70—Flue or combustion exhaust gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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- Oil, Petroleum & Natural Gas (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
本发明涉及碳捕集技术领域，提供二氧化碳吸附系统，包括：依次连接在原料气进气口后端的第一压缩机组、变温吸附单元和真空变压吸附单元；透平膨胀单元，其入口连接真空变压吸附单元的第一出口，且透平膨胀单元连接第一压缩机组；冷量回收单元，其第一入口连接透平膨胀单元的出口、第二入口连接真空变压吸附单元的第二出口，且冷量回收单元设置有脱二氧化碳原料出口；第一分离器，其入口连接冷量回收单元的第一出口、第一出口连接冷量回收单元的第三入口且冷量回收单元的第二出口连接真空变压吸附单元的入口、第二出口连接二氧化碳出液口。本发明有效提高CO2捕集效率，降低设备尺寸，并降低CO2捕集和液化能耗，简化工艺流程，适合大规模应用。
The present invention relates to the technical field of carbon capture, and provides a carbon dioxide adsorption system, including: a first compressor unit, a temperature swing adsorption unit and a vacuum pressure swing adsorption unit connected in sequence to the rear end of a raw gas inlet; a turbine expansion unit, whose inlet is connected to the first outlet of the vacuum pressure swing adsorption unit, and the turbine expansion unit is connected to the first compressor unit; a cold recovery unit, whose first inlet is connected to the outlet of the turbine expansion unit, whose second inlet is connected to the second outlet of the vacuum pressure swing adsorption unit, and whose cold recovery unit is provided with a decarbonated raw material outlet; a first separator, whose inlet is connected to the first outlet of the cold recovery unit, whose first outlet is connected to the third inlet of the cold recovery unit, whose second outlet is connected to the inlet of the vacuum pressure swing adsorption unit, and whose second outlet is connected to the carbon dioxide liquid outlet. The present invention effectively improves CO2 capture efficiency, reduces equipment size, reduces CO2 capture and liquefaction energy consumption, simplifies the process flow, and is suitable for large-scale application.
Description
Technical Field
The invention relates to the technical field of carbon capture, in particular to a carbon dioxide adsorption system.
Background
Carbon dioxide (CO 2) trapping in the flue gas is a main scene of future carbon trapping, and meets the environmental protection requirement. The main methods for achieving carbon dioxide capture are chemical absorption and adsorption.
The chemical absorption method has the problems of high energy consumption, solvent corrosion and the like, and although a great amount of energy-saving process improvement is made, the theoretical regeneration energy consumption of 2.0GJ/t carbon dioxide is basically close to the limit, and the potential of further digging and reducing consumption is limited.
The adsorption method adopts a low-pressure adsorption (1 barg-2 barg) mode conventionally, and has the characteristics of low energy consumption, environmental friendliness and the like compared with a chemical absorption method, but the low-pressure adsorption mode has the problems of low single-pass carbon dioxide trapping efficiency, long process flow, large equipment, difficult large-scale application and the like due to the characteristics of large flue gas amount, low pressure, low carbon dioxide concentration and the like, and two sets of pressure swing adsorption (Pressure Swing Adsorption, PSA) or a combination of membrane separation and pressure swing adsorption are often required to be connected in series.
The pressurized adsorption mode can improve the carbon dioxide capturing efficiency and reduce the equipment size, but has the challenge of high flue gas pressurizing energy consumption, and limits the large-scale application of the adsorption method.
It should be noted that the information disclosed in the foregoing background section is only for enhancement of understanding of the background of the invention and thus may include information that does not form the prior art that is already known to those of ordinary skill in the art.
Disclosure of Invention
In view of the above, the invention provides a carbon dioxide adsorption system, which can effectively improve the carbon dioxide capturing efficiency, reduce the equipment size, reduce the energy consumption for capturing and liquefying carbon dioxide, simplify the process flow and is suitable for large-scale application.
According to one aspect of the invention, a carbon dioxide adsorption system is provided, comprising a first compressor unit, wherein an inlet of the first compressor unit is connected with a raw gas inlet, and the pressure of an outlet of the first compressor unit is 0.9 MPag-2.0 MPag; the outlet of the first compressor unit is connected with the inlet of the temperature swing adsorption unit; the device comprises a vacuum pressure swing adsorption unit, a turbine expansion unit, a third compressor unit, a cold recovery unit, a first separator and a second separator, wherein an outlet of the vacuum pressure swing adsorption unit is connected with an inlet of the vacuum pressure swing adsorption unit, a first outlet of the vacuum pressure swing adsorption unit discharges non-adsorbed gas, a second outlet of the vacuum pressure swing adsorption unit discharges desorption gas with the volume content higher than 90%, the first outlet of the vacuum pressure swing adsorption unit is connected with the inlet of the turbine expansion unit, the turbine expansion unit is connected with a first compressor unit, the turbine expansion unit carries out turbine expansion on the non-adsorbed gas discharged by the vacuum pressure swing adsorption unit and pushes the first compressor unit to boost raw material gas by utilizing the gas after the turbine expansion, the inlet of the third compressor unit is connected with a second outlet of the vacuum pressure swing adsorption unit, the outlet of the third compressor unit has the temperature of 30-50 ℃, the outlet of the third compressor unit is connected with the first inlet of the cold recovery unit, the outlet of the third compressor unit is connected with the second inlet of the cold recovery unit, the outlet of the third compressor unit has the temperature of the first compressor unit is 20-60 ℃, the cold recovery unit is connected with the first separator, and the cold recovery unit is arranged at the first separator and the first separator is connected with the first separator, the first outlet of the first separator is connected with the third inlet of the cold energy recovery unit through a throttling expansion valve so as to enable the cold energy recovery unit to recover the cold energy after throttling expansion, the temperature range of the cold energy after throttling expansion is-50 ℃ to-90 ℃, the second outlet of the cold energy recovery unit is connected with the inlet of the vacuum pressure swing adsorption unit, the second outlet of the first separator is connected with a carbon dioxide liquid outlet, and the cold energy recovery unit recovers the cold energy after turbine expansion of the turbine expansion unit and the cold energy after throttling expansion of the throttling expansion valve and cools the gas after pressurizing of the third compressor unit.
In some embodiments, the temperature of the outlet of the first compressor unit is 100-150 ℃, the dew point temperature of the outlet of the temperature swing adsorption unit is-30-60 ℃, the pressure of the first outlet of the vacuum pressure swing adsorption unit is 0.4-2.0 MPag and the temperature is 20-40 ℃, and the pressure of the outlet of the turbine expansion unit is 0.01-0.05 MPag and the temperature is-40-70 ℃.
In some embodiments, the adsorbent in the temperature swing adsorption unit is a combination of one or more of alumina, activated carbon, silica gel, molecular sieve, and MOFs adsorbent, and the adsorbent in the vacuum pressure swing adsorption unit is a combination of one or more of alumina, activated carbon, silica gel, molecular sieve, and MOFs adsorbent.
In some embodiments, the carbon dioxide adsorption system further comprises a second compressor unit connected between the feed gas inlet and the inlet of the first compressor unit, wherein the pressure at the outlet of the second compressor unit is 0.2 MPag-1.0 MPag, and the temperature is 30-50 ℃.
In some embodiments, the carbon dioxide adsorption system further comprises a scrubbing and cooling unit connected between the feed gas inlet and the inlet of the second compressor unit, wherein the temperature of the outlet of the scrubbing and cooling unit is 30-50 ℃.
In some embodiments, the carbon dioxide adsorption system further comprises a vacuum pump connected between the second outlet of the vacuum pressure swing adsorption unit and the second inlet of the cold recovery unit.
In some embodiments, the pressure at the outlet of the third compressor unit is 3.5-8.0 mpag.
In some embodiments, the carbon dioxide adsorption system further comprises a second separator, wherein a first outlet of the first separator is connected with an inlet of the second separator, a first outlet of the second separator is connected with a third inlet of the cold recovery unit through the throttling expansion valve, and a second outlet of the second separator is connected with the carbon dioxide liquid outlet.
In some embodiments, the carbon dioxide adsorption system further comprises a condenser connected between the first outlet of the first separator and the inlet of the second separator, wherein the temperature of the outlet of the condenser is-30 ℃ to-70 ℃.
In some embodiments, the feed gas introduced by the feed gas inlet is boiler flue gas, catalytic coke-burning flue gas, hydrogen-producing cracking furnace flue gas or industrial furnace flue gas.
Compared with the prior art, the invention has the beneficial effects that at least:
The carbon dioxide adsorption system effectively improves the partial pressure of carbon dioxide by utilizing a compression adsorption mode through the compressor unit comprising the first compressor unit, greatly improves the adsorption performance of carbon dioxide, further improves the carbon capturing efficiency of an adsorption method and the concentration of carbon dioxide in desorption gas, can complete separation by adopting a set of temperature swing adsorption units, reduces the equipment size and the adsorption cost, simplifies the process flow, has lower volume flow of raw material gas after the operation pressure is improved, has smaller size of matched equipment, and is beneficial to large-scale application.
Because of adopting a pressurized adsorption mode, the operation pressure is high, and the compression energy consumption of the raw material gas is increased. According to the carbon dioxide adsorption system, a flue gas boosting energy storage principle is utilized, about 80% -90% of flue gas passing through a vacuum pressure swing adsorption (Vacuum Pressure Swing Adsorption, VPSA) unit is non-adsorbed gas, the pressure drop of the non-adsorbed gas is smaller than that of raw gas (which is equivalent to the pressure energy storage of the non-adsorbed gas), the turbo expansion unit is connected with a compression-turbo expansion unit formed by a first compressor unit, the pressure energy of the non-adsorbed gas of the vacuum pressure swing adsorption unit is recovered, a turbo expansion-raw material supercharging energy-saving process is realized, the electric energy consumption of the compressor unit is greatly reduced, and the carbon dioxide trapping energy consumption is further reduced.
According to the carbon dioxide adsorption system, the cold quantity of the vacuum pressure swing adsorption unit, which does not absorb cold quantity of which the temperature is greatly reduced after the external work of turbine expansion is performed, is utilized for liquefying carbon dioxide, so that the energy consumption of liquefying the carbon dioxide is reduced, the cold quantity of the gas phase noncondensable gas of the separator is recovered, the cold quantity is fully recovered, and the cold quantity is returned to the vacuum pressure swing adsorption unit to further recover carbon dioxide, so that the double recovery of the cold quantity and the carbon dioxide gas is realized.
The carbon dioxide adsorption system can effectively improve the carbon dioxide trapping efficiency, reduce the equipment size, reduce the energy consumption of carbon dioxide trapping and liquefying, simplify the process flow, be suitable for large-scale application and realize environmental protection.
It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the invention as claimed.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and together with the description, serve to explain the principles of the invention. It is evident that the figures described below are only some embodiments of the invention, from which other figures can be obtained without inventive effort for a person skilled in the art.
FIG. 1 shows a schematic diagram of a carbon dioxide adsorption system in an embodiment of the invention.
Detailed Description
Example embodiments will now be described more fully with reference to the accompanying drawings. However, the exemplary embodiments can be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the concept of the example embodiments to those skilled in the art.
The drawings are merely schematic illustrations of the present invention and are not necessarily drawn to scale. The same reference numerals in the drawings denote the same or similar parts, and thus a repetitive description thereof will be omitted. Some of the block diagrams shown in the figures are functional entities and do not necessarily correspond to physically or logically separate entities. These functional entities may be implemented in software or in one or more hardware modules or integrated circuits or in different networks and/or processor devices and/or microcontroller devices.
The use of the terms "first," "second," and the like in the description herein do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. Furthermore, in the description of the present invention, when it is said that a certain component is "connected" to another component, this includes not only the case of direct connection but also the case of indirect connection through the other component.
It should be noted that, without conflict, the embodiments of the present invention and features in different embodiments may be combined with each other.
Fig. 1 illustrates a structure of a carbon dioxide adsorption system, and referring to fig. 1, the carbon dioxide adsorption system provided in an embodiment of the present invention includes:
a first compressor unit 31, an inlet of the first compressor unit 31 being connected to the raw gas inlet a;
A temperature swing adsorption unit 40, the outlet of the first compressor unit 31 being connected to the inlet of the temperature swing adsorption unit 40;
The vacuum pressure swing adsorption unit 50, wherein the outlet of the temperature swing adsorption unit 40 is connected with the inlet of the vacuum pressure swing adsorption unit 50, the first outlet of the vacuum pressure swing adsorption unit 50 discharges non-adsorbed gas and the second outlet discharges desorption gas with high CO 2 content;
the first outlet of the vacuum pressure swing adsorption unit 50 is connected with the inlet of the turboexpansion unit 32, and the turboexpansion unit 32 is connected with the first compressor unit 31, wherein the turboexpansion unit 32 can be connected with the first compressor unit 31 through a clutch;
The outlet of the turbine expansion unit 32 is connected with the first inlet of the cold recovery unit 80, the second outlet of the vacuum pressure swing adsorption unit 50 is connected with the second inlet of the cold recovery unit 80, and the cold recovery unit 80 is provided with a decarbonated raw material outlet B;
The first separator 91, the first outlet of the cold recovery unit 80 is connected to the inlet of the first separator 91, the first outlet of the first separator 91 is connected to the third inlet of the cold recovery unit 80, the second outlet of the cold recovery unit 80 is connected to the inlet of the vacuum pressure swing adsorption unit 50, and the second outlet of the first separator 91 is connected to the carbon dioxide liquid outlet C.
The carbon dioxide adsorption system effectively improves the partial pressure of carbon dioxide by utilizing a pressurized adsorption mode through the compressor unit comprising the first compressor unit 31, greatly improves the adsorption performance of the carbon dioxide, further improves the carbon capturing efficiency of an adsorption method and the concentration of the carbon dioxide in desorption gas, can complete separation by adopting one set of temperature swing adsorption units 40, reduces the equipment size and the adsorption cost, simplifies the process flow, has lower volume flow of raw material gas and smaller size of matched equipment after the operation pressure is improved, and is beneficial to large-scale application.
In a preferred embodiment, the second outlet of the vacuum pressure swing adsorption unit 50 discharges a stripping gas having a CO 2 volume content of greater than 90%.
Because of adopting a pressurized adsorption mode, the operation pressure is high, and the compression energy consumption of the raw material gas is increased. According to the carbon dioxide adsorption system, by utilizing the flue gas boosting energy storage principle, about 80% -90% of flue gas passing through the vacuum pressure swing adsorption unit is non-adsorbed gas, the pressure drop of the non-adsorbed gas is smaller than that of raw gas (which is equivalent to the pressure energy storage of the non-adsorbed gas), the compression-turbine expansion unit 30 formed by connecting the turbine expansion unit 32 with the first compressor unit 31 is utilized, the pressure energy of the non-adsorbed gas of the vacuum pressure swing adsorption unit 50 is recovered, the energy-saving process of 'turbine expansion-raw material boosting' is realized, the electric energy consumption of the compressor unit is greatly reduced, and the carbon dioxide trapping energy consumption is further reduced. Specifically, the turbo expansion unit 32 turbo expands the non-adsorbed gas discharged from the vacuum pressure swing adsorption unit 50, and pressurizes the raw gas by pushing the first compressor group 31 with the turbo-expanded gas.
The carbon dioxide adsorption system also utilizes the cold energy of the vacuum pressure swing adsorption unit 50, which is used for liquefying carbon dioxide and reducing the energy consumption of liquefying the carbon dioxide, and the cold energy of the gas phase noncondensable gas of the separator is recovered to fully recover the cold energy, and then returns to the vacuum pressure swing adsorption unit 50 to further recover the carbon dioxide to realize the double recovery of the cold energy and the carbon dioxide gas through the cold energy recovery unit 80.
The carbon dioxide adsorption system can effectively improve the carbon dioxide trapping efficiency, reduce the equipment size, reduce the energy consumption of carbon dioxide trapping and liquefying, simplify the process flow, be suitable for large-scale application and realize environmental protection.
In some embodiments, the feed gas S-1 introduced by the feed gas inlet A is boiler flue gas, catalytic coke-burning flue gas, hydrogen-producing pyrolysis furnace flue gas, or industrial furnace flue gas.
In some embodiments, the pressure at the outlet of the first compressor unit 31 is 0.4MPag to 2.0MPag and the temperature is 30 ℃ to 130 ℃, for example, but not limited to, the pressure at the outlet of the first compressor unit 31 is 0.9MPag and the temperature is 125 ℃.
The pressure and temperature at the outlet of the first compressor unit 31 may be higher thanks to the action of the turbo-expansion unit 32, for example, in a preferred embodiment, the pressure at the outlet of the first compressor unit 31 is 0.9MPag to 2.0MPag and the temperature is 100 ℃ to 150 ℃.
In some embodiments, the temperature at the outlet of the temperature swing adsorption unit 40 is at a dew point temperature of-30 ℃ to-60 ℃, for example, but not limited to, -40 ℃.
In some embodiments, the pressure at the first outlet of the vacuum pressure swing adsorption unit 50 is 0.4MPag to 2.0MPag and the temperature is 20 ℃ to 40 ℃, for example, but not limited to, the pressure at the first outlet of the vacuum pressure swing adsorption unit 50 is 0.8MPag and the temperature is 30 ℃.
In some embodiments, the pressure at the outlet of the turboexpansion unit 32 is 0.01MPag to 0.05MPag and the temperature is-40 ℃ to-70 ℃, for example, but not limited to, the pressure at the outlet of the turboexpansion unit 32 is 0.02MPag and the temperature is-60 ℃.
In some embodiments, the temperatures of the first outlet and the second outlet of the cold recovery unit 80 are-20 ℃ to-60 ℃, for example, but not limited to, the temperature of the outlet of the cold recovery unit 80 is-30 ℃.
In some embodiments, the adsorbent in temperature swing adsorption unit 40 is one or more of alumina, activated carbon, silica gel, molecular sieve and MOFs (Metal Organic Frameworks, metal organic framework compound) adsorbent, specifically designed according to the properties and dehydration index requirements of feed gas S-1, and the adsorbent in vacuum pressure swing adsorption unit 50 is one or more of alumina, activated carbon, silica gel, molecular sieve and MOFs adsorbent, specifically designed according to the properties and decarbonation index requirements of feed gas S-1. The CO 2 adsorption performance of the MOFs adsorbent is 3-5 times that of the traditional adsorbent, and the trapping efficiency of CO 2 in flue gas can be greatly improved.
In some embodiments, the carbon dioxide adsorption system further includes a second compressor train 20 connected between the feed gas inlet A and the inlet of the first compressor train 31. By two-stage compression of the second compressor unit 20 and the first compressor unit 31, proper pressurization of the feed gas S-1 is ensured.
Wherein the pressure at the outlet of the second compressor unit 20 is 0.2MPag to 1.0MPag, and the temperature is 30 ℃ to 50 ℃. For example, the pressure at the outlet of the second compressor unit 20 is 0.4MPag and the temperature is 40 ℃, but not limited thereto.
In some embodiments, the carbon dioxide adsorption system further comprises a scrubbing cooling unit 10 connected between the feed gas inlet A and the inlet of the second compressor train 20. The scrubbing and cooling unit 10 may scrub and cool the feed gas S-1 to enhance the cleanliness of the feed gas S-1.
Wherein the temperature of the outlet of the washing and cooling unit 10 is 30-50 ℃. For example, the temperature of the outlet of the washing and cooling unit 10 is 40 ℃, but not limited thereto.
In some embodiments, the carbon dioxide adsorption system further includes a vacuum pump 60 connected between the second outlet of the vacuum pressure swing adsorption unit 50 and the second inlet of the cold recovery unit 80.
In some embodiments, the carbon dioxide adsorption system further includes a third compressor unit 70 connected between the outlet of the vacuum pump 60 and the second inlet of the cold recovery unit 80. Wherein the pressure at the outlet of the third compressor unit 70 is 2.0MPag to 4.0MPag, and the temperature is 30 ℃ to 50 ℃. For example, the pressure at the outlet of the third compressor unit 70 is 3.0MPag and the temperature is 40 ℃, but this is not a limitation.
In some embodiments, the pressure at the outlet of the third compressor unit 70 may be higher, for example, 3.5MPag to 8.0MPag, and further, the temperature of the final CO 2 liquid product is 0 to-25 ℃.
In some embodiments, the carbon dioxide adsorption system further comprises a second separator 96, the first outlet of the first separator 91 is connected to the inlet of the second separator 96, the first outlet of the second separator 96 is connected to the third inlet of the cold recovery unit 80 through a throttle expansion valve 97, and the second outlet of the second separator 96 is connected to the carbon dioxide outlet C.
Sufficient separation of CO 2 is achieved by the two-stage separator of the first separator 91 and the second separator 96.
In some embodiments, the carbon dioxide adsorption system further includes a condenser 93 connected between the first outlet of the first separator 91 and the inlet of the second separator 96. Wherein the temperature of the outlet of the condenser 93 is-30 ℃ to-70 ℃. For example, the temperature at the outlet of the condenser 93 is-50 ℃, but not limited thereto.
In some implementations, the process flow for CO 2 capture and liquefaction using the carbon dioxide adsorption system shown in fig. 1 includes:
The raw material gas S-1 containing CO 2 conveyed from the upstream enters a washing and cooling unit 10, the washing and cooling unit 10 cools the raw material gas S-1 to about 40 ℃, the raw material gas S-2 after washing and cooling enters a second compressor unit 20, the raw material gas S-2 after washing and cooling is pressurized to about 0.4MPag by the second compressor unit 20, the pressurized raw material gas S-3 enters a first compressor unit 31 to be pressurized to about 0.9MPag again and the temperature is about 125 ℃, the pressurized and warmed raw material gas S-4 enters a temperature-changing adsorption unit 40 for compression heat regeneration drying dehydration, the dew point temperature of the raw material gas S-5 after compression heat regeneration drying dehydration is controlled to about-40 ℃, the raw material gas S-5 after compression heat regeneration drying dehydration enters a vacuum pressure-changing adsorption unit 50 for CO 2 adsorption separation, the CO 2 is adsorbed by an adsorbent, the raw material gas S-7 after CO 2 removal is discharged from a first outlet of the vacuum adsorption unit 50, and the pressure is about 0.8MPag and the temperature is about 40 ℃.
The raw material gas S-7 discharged from the first outlet of the vacuum pressure swing adsorption unit 50 after CO 2 removal enters the turbine expansion unit 32 to expand and recover pressure energy, the first compressor unit 31 is pushed to boost the pressurized raw material gas S-3 to 0.9MPag, the pressure of the raw material gas S-8 after CO 2 removal after turbine expansion is reduced from 0.8MPag to 0.02MPag and the temperature is about-60 ℃, and then enters the first inlet of the cold energy recovery unit 80, and the cold energy recovery unit 80 recovers part of cold energy for CO 2 liquefaction.
The desorption gas S-10 which is discharged from the second outlet of the vacuum pressure swing adsorption unit 50 and contains high CO2 is pumped by the vacuum pump 60 to form desorption gas S-11, and then enters the third compressor unit 70 to be pressurized to the pressure of about 3.0MPag and the temperature of about 40 ℃, so that the pressurized desorption gas S-12 is delivered to the second inlet of the cold recovery unit 80. The cold energy recovery unit 80 uses the CO 2 removed after turbine expansion and the gas S-20 after throttling to exchange heat with the desorption gas S-12 after pressurization to fully recover two cold energy of S-8 and S-20, the gas-liquid mixture S-13 after heat exchange is cooled to about minus 30 ℃, and enters the first separator 91 from the first outlet of the cold energy recovery unit 80 to respectively obtain a first CO 2 liquid product S-15 and a first noncondensable gas S-14.
Wherein the temperature range of the cooling capacity after throttling expansion is-50 ℃ to-90 ℃. The cold energy recovery unit 80 recovers the cold energy after the turbine expansion and the cold energy after the throttle expansion, and effectively cools the gas after the pressurization of the third compressor unit 70.
Then, the first non-condensable gas S-14 enters a condenser 93, the temperature is further reduced and condensed to be minus 50 ℃, the gas-liquid mixture S-16 after the temperature reduction and condensation enters a second separator 96, and a second CO 2 liquid product S-17 and a second non-condensable gas S-19 are respectively obtained, wherein the first CO 2 liquid product S-15 and the second CO 2 liquid product S-17 are combined and then output as a CO 2 liquid product. The second non-condensable gas S-19 is throttled and expanded by a throttle expansion valve 97, the throttled gas S-20 is conveyed to a third inlet of the cold recovery unit 80, enters the cold recovery unit 80 to recover cold, the gas S-21 recovered by the cold is output from a second outlet of the cold recovery unit 80, and is combined with the raw gas S-5 regenerated and dried by compression heat to form gas S-6 to be adsorbed, and the gas S-6 enters the vacuum pressure swing adsorption unit 50 to adsorb CO 2.
Through measurement and calculation, CO 2 is captured and liquefied by using the carbon dioxide adsorption system, the energy consumption for capturing CO 2 is about 300-400kW/t, the energy consumption for liquefying CO 2 is about 150-200kW/t, the capture cost is about 180-240 yuan/t, the liquefying cost is about 90-120 yuan/t, and the total cost is about 270-360 yuan/t CO 2. The equivalent energy consumption index is about 1.1-1.5GJ/t CO 2, about 0.54-0.72GJ/t CO 2, about 1.64-2.22GJ/t total, which is obviously superior to the equivalent energy consumption index of 3.0-4.0 GJ/tCO 2 and the comprehensive cost of 400-500 yuan/t CO 2 of the conventional process.
The advantages of the carbon dioxide adsorption system of the present invention are described below in conjunction with two experimental cases.
Case one:
In this case, about 60000Nm3/h of flue gas from a coal boiler of an enterprise is adsorbed at about 20kPag and about 50 ℃ in components of 75.51% N 2、5.1％O2、12.24％CO2 and 7.14% H 2 O. The carbon dioxide adsorption system of the invention is compared with the traditional chemical absorption method and the low-pressure adsorption method, and the specific details are shown in the following table.
| Project | Unit (B) | Chemical absorption method | Low pressure adsorption process | The invention is that |
| Liquid CO 2 production | t/h | 12.28 | 12.28 | 12.28 |
| Electricity consumption for trapping | kW | 1093 | 5194 | 4395 |
| Trapping steam consumption | t/h | 14.7 | 0 | 0 |
| Consumption of electricity for liquefaction | kW | 2326 | 2908 | 1998 |
| Liquefied steam consumption | t/h | 2.5 | 0 | 0 |
| Price of electricity | Yuan/kW | 0.6 | 0.6 | 0.6 |
| Price of steam | Meta/t | 200 | 200 | 200 |
| Capturing equivalent energy consumption | GJ/tCO2 | 3.00 | 1.52 | 1.29 |
| Equivalent energy consumption for liquefaction | GJ/tCO2 | 1.14 | 0.85 | 0.59 |
| Cost of trapping | Meta/tCO 2 | 293.4 | 253.8 | 214.7 |
| Cost of liquefaction | Meta/tCO 2 | 154.4 | 142.1 | 97.6 |
| Total equivalent energy consumption | GJ/tCO2 | 4.14 | 2.38 | 1.87 |
| Aggregate cost | Meta/tCO 2 | 447.8 | 395.9 | 312.4 |
As can be seen from the case, the equivalent energy consumption and cost for CO 2 capturing and liquefying the flue gas by adopting the carbon dioxide adsorption system are lowest, namely 1.87GJ/tCO 2 and 312.4 yuan/tCO 2 respectively, and the carbon dioxide adsorption system is remarkably superior to a chemical absorption method (4.14 GJ/tCO 2 and 447.8 yuan/tCO 2 respectively) and a low-pressure adsorption method (2.38 GJ/tCO 2 and 395.9 yuan/tCO 2 respectively), and has remarkable energy-saving benefit.
Case two:
In this case, about 88000Nm3/h of natural gas boiler flue gas of a certain enterprise is absorbed by components 77.77% N 2、2.37％O2、10.3％CO2 and 9.56% H 2 O at a pressure of about 30kPag and a temperature of about 120 ℃. The carbon dioxide adsorption system of the invention is compared with the traditional chemical absorption method and the low-pressure adsorption method, and the specific details are shown in the following table.
As can be seen from the case, the equivalent energy consumption and cost for CO 2 capturing and liquefying the flue gas by adopting the carbon dioxide adsorption system are lowest, namely 1.97GJ/tCO 2 and 328.5 yuan/tCO 2 respectively, and the carbon dioxide adsorption system is remarkably superior to the systems of a chemical absorption method (4.11 GJ/tCO 2 and 440.3 yuan/tCO 2 respectively) and a low-pressure adsorption method (2.45 GJ/tCO 2 and 407.9 yuan/tCO 2 respectively), so that the energy-saving benefit is remarkable.
In summary, the carbon dioxide adsorption system provided by the invention can effectively improve the carbon dioxide trapping efficiency, reduce the equipment size, reduce the carbon dioxide trapping and liquefying energy consumption, simplify the process flow, and is suitable for large-scale application, thereby realizing energy conservation and environmental protection.
The foregoing is a further detailed description of the invention in connection with the preferred embodiments, and it is not intended that the invention be limited to the specific embodiments described. It will be apparent to those skilled in the art that several simple deductions or substitutions may be made without departing from the spirit of the invention, and these should be considered to be within the scope of the invention.
Claims (10)
1. A carbon dioxide adsorption system, comprising:
The inlet of the first compressor unit is connected with the feed gas inlet, and the pressure of the outlet of the first compressor unit is 0.9 MPag-2.0 MPag;
the outlet of the first compressor unit is connected with the inlet of the temperature swing adsorption unit;
The outlet of the temperature swing adsorption unit is connected with the inlet of the vacuum pressure swing adsorption unit, the first outlet of the vacuum pressure swing adsorption unit discharges non-adsorbed gas and the second outlet discharges desorption gas with CO 2 volume content higher than 90%;
The first outlet of the vacuum pressure swing adsorption unit is connected with the inlet of the turbine expansion unit, the turbine expansion unit is connected with the first compressor unit, the turbine expansion unit carries out turbine expansion on the non-adsorption gas discharged by the vacuum pressure swing adsorption unit, and the gas after turbine expansion is utilized to push the first compressor unit to boost the raw material gas;
the inlet of the third compressor unit is connected with the second outlet of the vacuum pressure swing adsorption unit, and the temperature of the outlet of the third compressor unit is 30-50 ℃;
The outlet of the turbine expansion unit is connected with the first inlet of the cold energy recovery unit, the outlet of the third compressor unit is connected with the second inlet of the cold energy recovery unit, the temperatures of the first outlet and the second outlet of the cold energy recovery unit are-20 ℃ to-60 ℃, and the cold energy recovery unit is further provided with a decarbonated raw material outlet;
The first outlet of the cold energy recovery unit is connected with the inlet of the first separator, the first outlet of the first separator is connected with the third inlet of the cold energy recovery unit through a throttling expansion valve so as to enable the cold energy recovery unit to recover the throttled and expanded cold energy, the temperature range of the throttled and expanded cold energy is-50 ℃ to-90 ℃, the second outlet of the cold energy recovery unit is connected with the inlet of the vacuum pressure swing adsorption unit, and the second outlet of the first separator is connected with a carbon dioxide liquid outlet;
The cold energy recovery unit recovers the cold energy after the turbine expansion of the turbine expansion unit and the cold energy after the throttle expansion of the throttle expansion valve, and cools the gas after the pressurization of the third compressor unit.
2. The carbon dioxide adsorption system of claim 1, wherein:
the temperature of the outlet of the first compressor unit is 100-150 ℃;
The dew point temperature of the outlet of the temperature swing adsorption unit is minus 30 ℃ to minus 60 ℃;
the pressure of the first outlet of the vacuum pressure swing adsorption unit is 0.4 MPag-2.0 MPag, and the temperature is 20-40 ℃;
the pressure of the outlet of the turbine expansion unit is 0.01 MPag-0.05 MPag, and the temperature is-40 ℃ to-70 ℃.
3. The carbon dioxide adsorption system of claim 1, wherein the adsorbent in the temperature swing adsorption unit is a combination of one or more of alumina, activated carbon, silica gel, molecular sieves, and MOFs adsorbents;
The adsorbent in the vacuum pressure swing adsorption unit is one or a combination of more of alumina, activated carbon, silica gel, molecular sieve and MOFs adsorbent.
4. The carbon dioxide adsorption system of claim 1, further comprising:
the second compressor unit is connected between the raw gas inlet and the inlet of the first compressor unit;
The pressure of the outlet of the second compressor unit is 0.2 MPag-1.0 MPag, and the temperature is 30-50 ℃.
5. The carbon dioxide adsorption system of claim 4, further comprising:
The washing and cooling unit is connected between the raw gas inlet and the inlet of the second compressor unit;
wherein the temperature of the outlet of the washing and cooling unit is 30-50 ℃.
6. The carbon dioxide adsorption system of claim 1, further comprising:
And the vacuum pump is connected between the second outlet of the vacuum pressure swing adsorption unit and the second inlet of the cold recovery unit.
7. The carbon dioxide adsorption system of claim 1, wherein the pressure at the outlet of the third compressor unit is 3.5-8.0 mpag.
8. The carbon dioxide adsorption system of claim 1, further comprising:
the first outlet of the second separator is connected with the inlet of the second separator, the first outlet of the second separator is connected with the third inlet of the cold energy recovery unit through the throttling expansion valve, and the second outlet of the second separator is connected with the carbon dioxide liquid outlet.
9. The carbon dioxide adsorption system of claim 8, further comprising:
A condenser connected between the first outlet of the first separator and the inlet of the second separator;
Wherein the temperature of the outlet of the condenser is-30 ℃ to-70 ℃.
10. The carbon dioxide adsorption system of any one of claims 1-9, wherein the feed gas introduced into the feed gas inlet is boiler flue gas, catalytic char flue gas, hydrogen production cracking furnace flue gas, or industrial furnace flue gas.
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| CN1197684A (en) * | 1997-01-30 | 1998-11-04 | 普拉塞尔技术有限公司 | System for energy recovery in vacuum pressure swing adsorption apparatus |
| CN101231130A (en) * | 2007-01-23 | 2008-07-30 | 气体产品与化学公司 | Purification of carbon dioxide |
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| CN1197684A (en) * | 1997-01-30 | 1998-11-04 | 普拉塞尔技术有限公司 | System for energy recovery in vacuum pressure swing adsorption apparatus |
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