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WO2024172216A1 - Système de séparation et de récupération de dioxyde de carbone - Google Patents

Système de séparation et de récupération de dioxyde de carbone Download PDF

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Publication number
WO2024172216A1
WO2024172216A1 PCT/KR2023/008035 KR2023008035W WO2024172216A1 WO 2024172216 A1 WO2024172216 A1 WO 2024172216A1 KR 2023008035 W KR2023008035 W KR 2023008035W WO 2024172216 A1 WO2024172216 A1 WO 2024172216A1
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exhaust gas
carbon dioxide
heat exchanger
unit
nozzle
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Korean (ko)
Inventor
이창형
박성호
류주열
황성현
박혜민
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Institute for Advanced Engineering
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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
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant 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
    • 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
    • F25J1/0221—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 using the cold stored in an external cryogenic component in an open refrigeration loop
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0296—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0296—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink
    • F25J1/0297—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink using an externally chilled fluid, e.g. chilled water
    • 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
    • F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
    • 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
    • F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • 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
    • 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
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising loop

Definitions

  • the present invention relates to a carbon dioxide separation and recovery system.
  • Carbon dioxide capture, storage, and utilization technology includes technologies for capturing carbon dioxide generated from industrial facilities, storing the captured carbon dioxide underground, and converting carbon dioxide into useful resources with high added value.
  • carbon dioxide capture technology is largely divided into post-combustion technology, pre-combustion technology, and oxy-fuel combustion technology.
  • post-combustion capture technology is a method to separate carbon dioxide from the exhaust gas emitted when burning fossil fuels with air
  • pre-combustion capture technology is a method to separate carbon dioxide in the process of producing hydrogen from fossil fuels, converting the synthesis gas generated after gasifying fossil fuels into carbon dioxide and hydrogen through the water gas shift reaction, and then separating only the carbon dioxide
  • oxy-combustion technology is a method to separate only carbon dioxide after combustion by separating oxygen in the air instead of air and combusting fossil fuels.
  • post-combustion capture technologies are classified into wet absorption methods using amine-based wet absorbents, dry absorption methods using solid absorbents, membrane separation methods using membranes, and phase separation methods using phase change.
  • the compression work required to liquefy the carbon dioxide separated from the wet absorbent after separating carbon dioxide from the wet absorbent is large, and that high energy is required to regenerate the wet absorbent to its initial state.
  • the dry absorption method also has a problem that the compression work required to liquefy the carbon dioxide separated from the solid absorbent after separating carbon dioxide from the solid absorbent is large, and that high energy is required to regenerate the solid absorbent to its initial state.
  • the membrane separation method there is a problem that it is difficult to increase large capacity, and durability is poor due to deterioration of the separation membrane.
  • the phase separation method since a pressure higher than the triple point is required to separate carbon dioxide from the exhaust gas into a liquid, there is a disadvantage of low energy efficiency.
  • Embodiments of the present invention have been made to solve the above-described conventional problems, and to provide a carbon dioxide separation and recovery system having improved energy efficiency by reducing the energy consumed to separate and recover carbon dioxide from exhaust gas.
  • a carbon dioxide separation and recovery system including: a compression unit that receives and compresses exhaust gas; a supercooling unit connected to the compression unit and receives and supercools the exhaust gas compressed in the compression unit; a phase change unit connected to the supercooling unit and expands the exhaust gas supercooled in the supercooling unit to phase-change gaseous carbon dioxide included in the exhaust gas into solid carbon dioxide; and a separation unit connected to the phase change unit and separating the solid carbon dioxide included in the exhaust gas expanded in the phase change unit.
  • the supercooling unit includes a first heat exchanger that is provided at the rear end of the compression unit and cools the exhaust gas discharged from the compression unit, and the exhaust gas expanded in the phase change unit, after the solid carbon dioxide is separated, can be supplied to the first heat exchanger.
  • the apparatus further includes a first passage connecting the first heat exchanger and the separator and providing a path for the remaining exhaust gas to flow, and the cooling heat of the remaining exhaust gas flowing through the first passage can be transferred to the exhaust gas discharged from the compression section in the first heat exchanger.
  • the supercooling unit may further include a second heat exchanger that cools the exhaust gas that has passed through the first heat exchanger once again.
  • the second passage further includes a path for providing a path for the first cooling supply medium to flow, and a second heat exchanger is connected to the second passage, so that cooling of the first cooling supply medium flowing in the second passage can be transferred to the exhaust gas from the second heat exchanger.
  • the supercooling unit may further include a second heat exchanger that cools the exhaust gas passing through the first heat exchanger once again; and a third heat exchanger that cools the first cooling supply medium that has exchanged heat with the exhaust gas in the second heat exchanger.
  • system may further include a third path connecting the second heat exchanger and the third heat exchanger and providing a path for the second cooling medium to circulate through the second heat exchanger and the third heat exchanger.
  • the fourth path is further included to provide a path for a third cooling supply medium different from the second cooling supply medium to flow, and a third heat exchanger is connected to the fourth path so that cooling of the third cooling supply medium flowing in the fourth path can be transferred to the second cooling supply medium from the third heat exchanger.
  • the phase change unit may include a nozzle that receives the supercooled exhaust gas from the supercooling unit and discharges it, but induces the exhaust gas to be discharged at a speed increased from the speed at which the exhaust gas was introduced; a diffuser connected to the nozzle and induces the exhaust gas to be discharged at a speed reduced from the speed at which the exhaust gas was discharged from the nozzle; and a connecting member that connects the nozzle and the diffuser.
  • the nozzle may include a nozzle-side reduction portion formed so that the flow cross-sectional area of the exhaust gas supercooled in the supercooling portion can be gradually reduced; a nozzle-side expansion portion formed so that the flow cross-sectional area of the exhaust gas supercooled in the supercooling portion can be gradually increased; and a nozzle-side throat portion connecting the nozzle-side reduction portion and the nozzle-side expansion portion.
  • the diffuser may include a diffuser-side reduction portion formed so that the flow cross-sectional area of the exhaust gas passing through the nozzle can be gradually reduced; a diffuser-side expansion portion formed so that the flow cross-sectional area of the exhaust gas passing through the nozzle can be gradually increased; and a diffuser-side neck portion connecting the diffuser-side reduction portion and the diffuser-side expansion portion.
  • a storage unit may be further included, which is provided at the rear end of the separation unit and supplies and stores the solid carbon dioxide separated through the separation unit.
  • the compression work required in the process of separating and recovering carbon dioxide from exhaust gas is significantly reduced compared to the compression work of conventional wet absorption methods, dry absorption methods, and phase separation methods, thereby saving energy and having improved energy efficiency.
  • the compression work is relatively short compared to conventional wet absorption methods, dry absorption methods, and phase separation methods, energy consumption for the compression work is lower than conventional methods, so it can be easily applied to large plants that emit large amounts of carbon dioxide.
  • the equipment can be simplified and miniaturized, maintenance is easy, and operation is easier, which has the effect of improving operational efficiency.
  • FIG. 1 is a block diagram illustrating a carbon dioxide separation and recovery system according to one embodiment of the present invention.
  • Figure 2 is a process diagram illustrating the carbon dioxide separation and recovery system of Figure 1.
  • Figure 3 is a conceptual diagram illustrating a phase change part of the carbon dioxide separation and recovery system of Figure 1.
  • FIG. 4 is a process diagram illustrating a carbon dioxide separation and recovery system according to another embodiment of the present invention.
  • a carbon dioxide separation and recovery system (1) may include a compression unit (10), a supercooling unit (20), a phase change unit (30), a separation unit (40), and a storage unit (50).
  • the compression unit (10) can receive exhaust gas from the exhaust gas emission source (2) and compress it.
  • the exhaust gas emitted from the exhaust gas emission source (2) may be, for example, flue gas composed of nitrogen, oxygen, carbon dioxide, and water vapor.
  • flue gas composed of nitrogen, oxygen, carbon dioxide, and water vapor.
  • this is only an example for convenience of explanation, and the composition of the exhaust gas may vary to various compositions containing at least carbon dioxide.
  • the compression unit (10) may include a desulfurization unit (11), a catalytic converter (12), an exhaust gas compressor (13), a water condenser (14), and a water treatment unit (15).
  • the desulfurization unit (11) and the catalytic converter (12) may perform a pretreatment role of separating and removing combustion products contained in exhaust gas discharged from an exhaust gas emission source (2), and the exhaust gas compressor (13) may receive and compress gas that has undergone pretreatment through the desulfurization unit (11) and the catalytic converter (12).
  • the exhaust gas compressor (13) can pressurize the gas that has undergone pretreatment through the desulfurization unit (11) and the catalytic converter (12) to a pressure of about 2 to 3 bar, which is lower than the conventional pressure.
  • the gas compressed in the exhaust gas compressor (13) (hereinafter referred to as “compressed gas”) can be post-treated while sequentially passing through the moisture condenser (14) and the moisture treatment unit (15).
  • the post-treatment means that moisture contained in the compressed gas is removed.
  • the compressed gas that has undergone the post-treatment in this manner can be supplied to the first heat exchanger (21) of the supercooling unit (20) to be described later. This will be described later.
  • the supercooling unit (20) can receive compressed gas from the compression unit (10) and supercool it.
  • the supercooling unit (20) can include a first heat exchanger (21) and a second heat exchanger (22).
  • the first heat exchanger (21) may be provided at the rear end of the compression unit (10) and may perform the function of pre-cooling the compressed gas discharged from the compression unit (10) to the first temperature. In other words, the first heat exchanger (21) may remove the sensible heat of the compressed gas discharged from the compression unit (10) to lower the temperature of the compressed gas.
  • the cold heat for pre-cooling the compressed gas may be gas supplied from the separation unit (40).
  • the gas supplied from the separation unit (40) may be the remaining exhaust gas after the solid carbon dioxide is separated from the exhaust gas expanded in the phase change unit (30). Since the gas discharged from the separation unit (40) is gas for pre-cooling the compressed gas, hereinafter, for the convenience of explanation, the gas discharged from the separation unit (40) will be referred to as a 'gas for cold heat transfer'.
  • the first heat exchanger (21) may be connected to the separator (40) through the first flow path (L1).
  • the first flow path (L1) may be configured so that the cold heat transfer gas discharged from the separator (40) flows to the first heat exchanger (21).
  • the cold heat transfer gas discharged from the separator (40) and flowing along the first flow path (L1) may be vented to the outside after passing through the first heat exchanger (21).
  • the cold heat transfer gas flowing along the first flow path (L1) may be heat-exchanged with the compressed gas in the first heat exchanger (21). As the cold heat of the cold heat transfer gas is transferred to the compressed gas in the first heat exchanger (21), the compressed gas may be cooled to the first temperature.
  • the second heat exchanger (22) can perform the function of cooling the compressed gas that has passed through the first heat exchanger (21) once again.
  • the second heat exchanger (22) can cool the compressed gas that has been cooled to a first temperature while passing through the first heat exchanger (21) to a second temperature that is lower than the first temperature.
  • the cold heat for re-cooling the compressed gas pre-cooled to the first temperature to the second temperature can be provided from the first cold heat supply medium.
  • the first cold heat supply medium can be, for example, a liquid fuel or refrigerant such as LNG.
  • the second heat exchanger (22) may be arranged on the second flow path (L2) through which the first cooling supply medium circulates and flows.
  • a first cooling supply medium compressor (221), a first cooling supply medium condenser (222), a first cooling supply medium expander (223), and a second heat exchanger (22) may be arranged on the second flow path (L2).
  • the second flow path (L2) may form a closed loop that allows the first cooling supply medium to circulate through the first cooling supply medium compressor (221), the first cooling supply medium condenser (222), the first cooling supply medium expander (223), and the second heat exchanger (22).
  • the first cooling supply medium flowing along the second path (L2) can exchange heat with the compressed gas that has passed through the first heat exchanger (21) in the second heat exchanger (22).
  • the compressed gas that has passed through the first heat exchanger (21) can be cooled to the second temperature.
  • the compressed gas cooled to the second temperature corresponds to a supercooled compressed gas, and the supercooled compressed gas can be supplied to the phase change unit (20).
  • the phase change unit (30) can expand the compressed gas (hereinafter referred to as “supercooled compressed gas”) supercooled in the supercooling unit (20) to change the gaseous carbon dioxide contained in the exhaust gas into solid carbon dioxide.
  • the phase change unit (30) can include a nozzle (31), a diffuser (32), and a connecting member (33).
  • the nozzle (31) receives the supercooled compressed gas from the supercooling unit (20) and discharges it, but can induce the supercooled compressed gas to be discharged at a speed that is increased from the speed at which it was introduced.
  • the supercooled compressed gas expands inside the nozzle (31), and during the expansion process of the supercooled compressed gas, the carbon dioxide in the gaseous state contained in the supercooled compressed gas can change into a solid state.
  • the carbon dioxide contained in the supercooled compressed gas is separated into a solid state, and other gases in the supercooled compressed gas, for example, nitrogen/oxygen, are expanded into a gaseous state.
  • the gas expanded from the nozzle (31) can be a mixture of solid carbon dioxide and gaseous nitrogen/oxygen.
  • carbon dioxide that has started to solidify can be accompanied by an exothermic reaction that releases heat to the surroundings, and releases heat inside the system.
  • gaseous nitrogen/oxygen continuously decreases in temperature through expansion, so it can reach thermal equilibrium with the exothermic reaction of carbon dioxide.
  • the nozzle (31) can be divided into a nozzle-side reduction portion (311), a nozzle-side expansion portion (312), and a nozzle-side throat portion (313).
  • the nozzle-side reduction portion (311) can be formed so that the flow cross-sectional area of the compressed gas supercooled in the supercooling portion (20) can be gradually reduced, and the nozzle-side expansion portion (312) can be formed so that the flow cross-sectional area of the exhaust gas supercooled in the supercooling portion (20) can be gradually increased.
  • the nozzle-side reduction portion (311) and the nozzle-side expansion portion (312) can be connected by the nozzle-side throat portion (313), and operation at a supersonic speed is possible even at a low pressure depending on the area ratio of the nozzle-side expansion portion (312) and the nozzle-side throat portion (313).
  • the internal energy i.e., the sum of thermal energy and kinetic energy
  • the internal energy and kinetic energy can be expressed as enthalpy, and the pressure and temperature can be extremely low through the nozzle (31) that can accelerate the fluid to supersonic speed.
  • the diffuser (32) can perform the function of a pressure booster that reduces the velocity energy of the expansion gas discharged from the nozzle (31) to increase the pressure of the expansion gas.
  • the diffuser (32) can induce the expansion gas discharged from the nozzle (31) to be discharged at a reduced velocity than the velocity at which it was discharged from the nozzle (31).
  • the diffuser (32) can be divided into a diffuser-side reduction portion (321), a diffuser-side expansion portion (322), and a diffuser-side neck portion (323).
  • the diffuser-side reduction portion (321) can be formed so that the flow cross-sectional area of the exhaust gas passing through the nozzle (31) can be gradually reduced, and the diffuser-side expansion portion (322) can be formed so that the flow cross-sectional area of the exhaust gas passing through the nozzle (31) can be gradually increased.
  • the diffuser-side reduction portion (321) and the diffuser-side expansion portion (322) can be connected by the diffuser-side neck portion (323).
  • a connecting member (33) is provided between the nozzle (31) and the diffuser (32) to extend the flow path of the expansion gas.
  • the separation unit (40) can separate solid carbon dioxide contained in the gas expanded in the phase change unit (30).
  • the separation unit (40) can be equipped with a centrifugal separator such as a cyclone.
  • the expansion gas supplied to the separation unit (40) may be a mixed gas of solid carbon dioxide and gaseous nitrogen/oxygen.
  • the solid carbon dioxide and gaseous nitrogen/oxygen may be separated through the separation unit (40).
  • the gaseous nitrogen/oxygen refers to the remaining gas after the solid carbon dioxide contained in the expansion gas is separated, so below, for the convenience of explanation, the separated gaseous nitrogen/oxygen will be referred to as the 'remaining gas'.
  • the remaining gas separated through the separation unit (40) can be supplied to the first heat exchanger (21) through the first flow path (L1).
  • the remaining gas separated through the separation unit (40) can be utilized for preliminary cooling of the compressed gas that has been compressed in the compression unit (10).
  • the overall system efficiency can be improved since the cold heat of the remaining gas separated through the separation unit (40) can be recovered and reused for cooling the compressed gas compressed in the compression unit (10), the overall system efficiency can be improved.
  • the storage unit (50) can receive and store solid carbon dioxide separated through the separation unit (40).
  • the carbon dioxide separation and recovery system (1) having the configuration described above has the effect of saving energy and improving energy efficiency by significantly reducing the compression work required in the process of separating and recovering carbon dioxide from exhaust gas compared to the compression work of conventional wet absorption methods, dry absorption methods, and phase separation methods.
  • the compression work is relatively short compared to conventional wet absorption methods, dry absorption methods, and phase separation methods, energy consumption for the compression work is lower than conventional methods, so it can be easily applied to large plants that emit large amounts of carbon dioxide.
  • the equipment can be simplified and miniaturized, maintenance is easy, and operation is easier, which has the effect of improving operational efficiency.
  • a carbon dioxide separation and recovery system (1') may include a compression unit (10), a supercooling unit (20'), a phase change unit (30), a separation unit (40), and a storage unit (50).
  • the carbon dioxide separation and recovery system (1') illustrated in FIG. 4 is substantially the same as the carbon dioxide separation and recovery system (1) described with reference to FIGS. 1 to 3 except for the supercooling unit (20'), and therefore, the supercooling unit (20'), which is the difference, will be described below.
  • the supercooling unit (20') can receive compressed gas from the compression unit (10) and supercool it.
  • the supercooling unit (20') can include a first heat exchanger (21), a second heat exchanger (22), and a third heat exchanger (23).
  • the first heat exchanger (21) may be provided at the rear end of the compression unit (10) and may perform the function of pre-cooling the compressed gas discharged from the compression unit (10) to the first temperature.
  • the first heat exchanger (21) may be provided at the rear end of the compression unit (10).
  • the cooling for pre-cooling of the compressed gas can be provided from the gas supplied from the separation unit (40).
  • the gas supplied from the separation unit (40) can be the remaining exhaust gas from which solid carbon dioxide is separated among the exhaust gas expanded in the phase change unit (30).
  • the gas discharged from the separation unit (40) is gas for pre-cooling the compressed gas, so below, for the convenience of explanation, the gas discharged from the separation unit (40) will be referred to as a 'gas for cooling heat transfer'.
  • the first heat exchanger (21) may be connected to the separator (40) through the first flow path (L1).
  • the first flow path (L1) may be configured so that the cold heat transfer gas discharged from the separator (40) flows to the first heat exchanger (21).
  • the cold heat transfer gas discharged from the separator (40) and flowing along the first flow path (L1) may be vented to the outside after passing through the first heat exchanger (21).
  • the cold heat transfer gas flowing along the first flow path (L1) may be heat-exchanged with the compressed gas in the first heat exchanger (21). As the cold heat of the cold heat transfer gas is transferred to the compressed gas in the first heat exchanger (21), the compressed gas may be cooled to the first temperature.
  • the second heat exchanger (22) can once again cool the exhaust gas that has passed through the first heat exchanger (21), and the third heat exchanger (23) can cool the first cooling supply medium that has undergone heat exchange with the exhaust gas in the second heat exchanger (22).
  • the second heat exchanger (22) can cool the compressed gas cooled to the first temperature by passing through the first heat exchanger (21) to a second temperature lower than the first temperature.
  • the cooling heat for re-cooling the compressed gas pre-cooled to the first temperature to the second temperature can be provided from the second cooling heat supply medium.
  • the second cooling supply medium can be heat-exchanged with the compressed gas that has passed through the first heat exchanger (21), and the second cooling supply medium that has been heat-exchanged with the compressed gas that has passed through the first heat exchanger (21) can be heat-exchanged with a third cooling supply medium that is different from the second cooling supply medium.
  • the second cooling supply medium can be a liquid fuel or refrigerant such as LNG, and the third cooling supply medium can be brine.
  • the second heat exchanger (22) and the third heat exchanger (23) may be arranged on the third flow path (L3) through which the second cooling supply medium circulates and flows.
  • the second heat exchanger (22), the second cooling supply medium compressor (224), the third heat exchanger (23), and the second cooling supply medium expander (225) may be arranged on the third flow path (L3).
  • the third flow path (L3) may form a closed loop that allows the second cooling supply medium to circulate through the second heat exchanger (22), the second cooling supply medium compressor (224), the third heat exchanger (23), and the second cooling supply medium expander (225).
  • the second cooling supply medium circulating along the third path (L3) can be heat-exchanged with the compressed gas that has passed through the first heat exchanger (21) in the second heat exchanger (22). As the cooling heat of the second cooling supply medium is transferred to the compressed gas that has passed through the first heat exchanger (21) in the second heat exchanger (22), the compressed gas that has passed through the first heat exchanger (21) can be cooled to the second temperature.
  • the second cooling supply medium that cools the compressed gas that has passed through the first heat exchanger (21) can be cooled again through heat exchange with the third cooling supply medium flowing along the fourth flow path (L4).
  • a third heat exchanger (23) can be connected to the fourth flow path (L4).
  • a compressor (231), a condenser (232), an expander (233), and a third heat exchanger (23) may be arranged on the fourth path (L4).
  • the fourth path (L4) may form a closed loop that allows a third cooling supply medium to circulate through the compressor (231), the condenser (232), the expander (233), and the third heat exchanger (23).
  • the third cooling supply medium flowing along the fourth path (L4) can be heat-exchanged with the second cooling supply medium in the third heat exchanger (23). As the cooling heat of the third cooling supply medium is transferred to the second cooling supply medium in the third heat exchanger (23), the second cooling supply medium can be cooled.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

La présente invention concerne un système de séparation et de récupération de dioxyde de carbone. Le système de séparation et de récupération de dioxyde de carbone selon un mode de réalisation de la présente invention comprend : une unité de compression qui reçoit des gaz d'échappement et les comprime ; une unité de surfusion qui est reliée à l'unité de compression, reçoit les gaz d'échappement comprimés dans l'unité de compression et procède à une surfusion ; une unité de changement de phase qui est reliée à l'unité de surfusion et dilate les gaz d'échappement en surfusion dans l'unité de surfusion pour effectuer un changement de phase du dioxyde de carbone gazeux contenu dans les gaz d'échappement en dioxyde de carbone solide ; et une unité de séparation qui est reliée à l'unité de changement de phase et sépare le dioxyde de carbone solide contenu dans les gaz d'échappement détendus dans l'unité de changement de phase.
PCT/KR2023/008035 2023-02-15 2023-06-12 Système de séparation et de récupération de dioxyde de carbone Ceased WO2024172216A1 (fr)

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KR20230019754 2023-02-15
KR10-2023-0019754 2023-02-15
KR10-2023-0042758 2023-03-31
KR1020230042758A KR102682895B1 (ko) 2023-02-15 2023-03-31 이산화탄소 분리 회수 시스템

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JP2008202812A (ja) * 2007-02-16 2008-09-04 Mitsubishi Electric Corp 冷凍サイクル装置
KR20140016794A (ko) * 2012-07-30 2014-02-10 한국생산기술연구원 축소확대노즐을 구비한 가스연료 공급장치
KR20160015923A (ko) * 2014-08-01 2016-02-15 한국가스공사 천연가스 액화공정
KR20160134348A (ko) * 2015-05-15 2016-11-23 대우조선해양 주식회사 천연가스의 이산화탄소 분리 시스템 및 방법
KR20190048178A (ko) * 2017-10-30 2019-05-09 두산중공업 주식회사 액화 천연 가스의 냉열을 이용한 이산화탄소 포집 장치 및 발전 시스템

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JPH07157306A (ja) * 1993-12-03 1995-06-20 Mitsubishi Heavy Ind Ltd 固体炭酸ガスの回収装置
JPH0914831A (ja) * 1995-06-27 1997-01-17 Mitsubishi Heavy Ind Ltd Ｃｏ２ 回収装置及び回収方法
US20130283852A1 (en) * 2012-04-26 2013-10-31 General Electric Company Method and systems for co2 separation

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Publication number Priority date Publication date Assignee Title
JP2008202812A (ja) * 2007-02-16 2008-09-04 Mitsubishi Electric Corp 冷凍サイクル装置
KR20140016794A (ko) * 2012-07-30 2014-02-10 한국생산기술연구원 축소확대노즐을 구비한 가스연료 공급장치
KR20160015923A (ko) * 2014-08-01 2016-02-15 한국가스공사 천연가스 액화공정
KR20160134348A (ko) * 2015-05-15 2016-11-23 대우조선해양 주식회사 천연가스의 이산화탄소 분리 시스템 및 방법
KR20190048178A (ko) * 2017-10-30 2019-05-09 두산중공업 주식회사 액화 천연 가스의 냉열을 이용한 이산화탄소 포집 장치 및 발전 시스템

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