EP4571224A1 - Procédé de compression et de liquéfaction de co2 - Google Patents

Procédé de compression et de liquéfaction de co2 Download PDF

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Publication number
EP4571224A1
EP4571224A1 EP23307196.8A EP23307196A EP4571224A1 EP 4571224 A1 EP4571224 A1 EP 4571224A1 EP 23307196 A EP23307196 A EP 23307196A EP 4571224 A1 EP4571224 A1 EP 4571224A1
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EP
European Patent Office
Prior art keywords
stream
refrigerant
feed
heat exchanger
cold
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP23307196.8A
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German (de)
English (en)
Inventor
Marco Valente
Imane Chakroun
Sébastien MAUFRAIS
Adrien NARBONNE
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Technip Energies France SAS
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Technip Energies France SAS
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Technip Energies France SAS filed Critical Technip Energies France SAS
Priority to EP23307196.8A priority Critical patent/EP4571224A1/fr
Priority to TW113147847A priority patent/TW202530615A/zh
Priority to PCT/EP2024/025336 priority patent/WO2025124739A1/fr
Publication of EP4571224A1 publication Critical patent/EP4571224A1/fr
Pending legal-status Critical Current

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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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0095—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
    • F25J1/02—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
    • F25J1/0221—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
    • F25J1/0222—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 in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
    • 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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • 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
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • 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
    • 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
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide

Definitions

  • the present disclosure deals with a method for compressing and liquefying a feed of wet CO2.
  • the disclosure also deals with an installation adapted for performing such a method.
  • CO2 is usually recovered at low pressure, compressed, dehydrated and exported at very high pressure into export pipelines, or injected into depleted natural gas or oil wells.
  • CO2 is compressed through a multistage compressor, dehydrated and then, if needed, liquefied.
  • the liquefaction process is stand alone.
  • An external refrigeration unit is required to cool and liquefy CO2.
  • the refrigerant used is an industrial refrigerant, or sometimes ammonia.
  • An objective of the disclosure is to provide a method that partially or entirely overcomes the above drawbacks, in particular a method allowing to reduce the cost (CAPEX and OPEX) of producing liquefied CO2.
  • the disclosure proposes a method comprising:
  • the method may comprise one or several of the following features, taken in isolation or any technically feasible combination:
  • the disclosure also proposes an installation comprising:
  • upstream and downstream are generally relative to the normal direction of circulation of a fluid.
  • the ambient temperature prevailing around the installation is not significant for the purposes of the disclosure and can be in particular between 5°C and 40°C.
  • the installation 10 is adapted for compressing and liquefying a feed 12 comprising gaseous, for example wet, CO2 ( Figure 1 ) and obtaining a CO2 rich liquid 14.
  • the feed 12 for example comes from a CO2 capture unit 15.
  • the feed 12 for example contains more than 90% of CO2 on a dry basis, preferably more than 95%.
  • the feed 12 may contain light elements, such as nitrogen, hydrogen or methane.
  • the feed 12 may also contain water, which is then removed in order to prevent hydrate formation or freezing, and to allow liquefying CO2.
  • the feed may be at a feeding pressure comprised between 0.1 and 5.0 bar.
  • CO2 rich in the present document, it is meant that the CO2 fraction is "between 90.0% and 100.0%, preferably between 95.0%, and 100.0%".
  • the CO2 rich liquid 14 is preferably at a pressure comprised between 6.0 and 70 bar.
  • the installation 10 comprises a compression unit 16 adapted for receiving the feed 12 and producing a compressed feed 18 and in the example several streams of liquid 20A, 20B, 20C, and optionally a dehydration unit 22 adapted for dehydrating the compressed feed 18.
  • the installation 10 comprises a liquefaction unit 26 adapted for liquefying the compressed and optionally dehydrated feed 18 and producing the CO2 rich liquid 14.
  • the installation 10 comprises a first cooling cycle 28, in which a first refrigerant 30 is intended to circulate, in order to bring cold to the compression unit 16.
  • the installation 10 comprises a second cooling cycle 32 shown in Figure 2 , in which a second refrigerant 34 is intended to circulate, in order to bring cold to the liquefaction unit 26, and optionally to the first cooling cycle 28.
  • the installation 10 comprises a first heat exchanger 36 within the liquefaction unit 26, and a second heat exchanger 38 within the compression unit 16 and the first cooling cycle 28, and a third heat exchanger 40 within the first cooling cycle 28.
  • the installation 10 comprises a fourth heat exchanger 41 within the liquefaction unit 26, a fifth heat exchanger 42 within the first cooling cycle 28 and the second cooling cycle 32, a sixth heat exchanger 44 and a seventh heat exchanger 46 both within the liquefaction unit 26 and the second cooling cycle 32, and an eighth heat exchanger 48 within the liquefaction unit 26.
  • the compression unit 16 for example comprises a suction drum 50, and a compressor 52 for example having a low pressure stage 52A and a high pressure stage 52B.
  • the compressor 52 comprises a low pressure desuperheater 54A (or intercooler), a high pressure desuperheater 54B, a high pressure stage suction drum 56A and a high pressure stage discharge drum 56B.
  • the low pressure is higher than the feeding pressure, and for example comprised between ween 0.3 and 7.0 bar.
  • the high pressure is higher than the low pressure, and for example comprised between ween 8.0 and 25 bar.
  • the compressor 52 may have a single stage, a single desuperheater 54B and a single discharge drum 56B, or may have three stages or more, each stage having a dedicated desuperheater and suction drum.
  • the second heat exchanger 38 is advantageously located downstream of the desuperheater 54B and upstream of the discharge drum 56B of the last stage of the compressor 52.
  • the second heat exchanger 38, the discharge drum 56B and the optional dehydration unit 22 are located between the suction drum 56A and the high pressure stage 52B.
  • the first cooling cycle 28 for example comprises a pump 58 to circulate the first refrigerant 30.
  • the first refrigerant 30 advantageously comprises, or is, glycol water.
  • the dehydration unit 22 may be adapted to use various known technologies, and for example comprises one or several molecular sieve(s), silica gel, or triethylene glycol (TEG) (not shown).
  • the liquefaction unit 26 for example comprises an end flash drum 60 and a pump 62.
  • the liquefaction unit 26 is adapted for receiving a cold fluid 64, such as LNG (liquefied natural gas).
  • LNG is a liquid, usually at a temperature below -140°C.
  • the cold fluid 64 may be a pressurized one, with a pressure for example above 31 bar or even above 81 bar.
  • the liquefaction unit 26 is adapted for producing a partially heated gas 66 by heating the cold fluid 64, and advantageously for producing an end flash gas 68.
  • the partially heated gas 66, once heated in the third heat exchanger 40 advantageously becomes a fluid 70 at ambient temperature, or close to, which can for example be exported to a network 72 or a user.
  • the end flash gas 68 may be recycled in a process unit 73, which can be part of the installation 10 or be an outside unit.
  • the first heat exchanger 36 is advantageously an intermediate fluid liquefier (IFL) using an intermediate fluid 74, for example comprising more than 90% of ethane or an equivalent fluid, such as propane, ethylene, propylene or ammonia.
  • an intermediate fluid 74 for example comprising more than 90% of ethane or an equivalent fluid, such as propane, ethylene, propylene or ammonia.
  • the intermediate fluid 74 is ethane.
  • the second cooling cycle 32 for example comprises a compressor 76, which is for example three staged, a medium pressure desuperheater 78, a pressure booster 80, a high pressure desuperheater 82A, a condenser 82B, and an accumulator 84.
  • the second cooling cycle 32 for example comprises three expansion organs 86A, 86B, 86C, such as valves or turbines, and three suction drums 88A, 88B, 88C.
  • the second cooling cycle 32 for example comprises a by-pass 90 for by-passing the fifth heat exchanger 42 totally or partially.
  • the booster 80 may be a final stage of the compressor 76, or the second cooling cycle 32 has no booster.
  • the compressor 76 may be a single staged machine.
  • the by-pass 90 for example comprises an expansion organ 86D, such as a valve or a turbine.
  • the second refrigerant 34 may be any type of refrigerant that can cool and liquefy CO2.
  • the second refrigerant 34 is a CO2 rich fluid, advantageously obtained from the compressed and optionally dehydrated feed 18.
  • the second refrigerant 34 is advantageously made up from the compressed feed 18.
  • the feed 12 is first obtained, in the example from the capture unit 15.
  • the feed 12 is compressed and dried in the compression unit 16 in order to obtain the compressed feed 18 and the streams of liquid 20A, 20B, 20C.
  • the feed 12 is received in the suction drum 50, in which water, and other liquids if any, are collected to form the stream of liquid 20A.
  • the feed 12 then enters the compressor 52, in the example via the first stage 52A, where pressure is increased from the feeding pressure to the low pressure.
  • the feed 12 is cooled in the low pressure desuperheater 54A and admitted in the high pressure stage suction drum 56A, from which the second stream of liquid 20B is extracted.
  • the feed 12 then enters the second stage 52B, where pressure is increased from the low pressure to the high pressure.
  • the feed 12 is cooled in the high pressure desuperheater 54B.
  • the feed 12 is cooled by receiving cold in the second heat exchanger 38 from a cooling stream 92 of the first refrigerant 30. After this additional cooling, the feed 12 is admitted in the high pressure discharge drum 56B from which the stream of liquid 20C is extracted.
  • the second heat exchanger 38 provides additional cooling to the feed 12 compared to what the desuperheater 54B can do, which allows condensing more water before the compressed feed 18 flows into the optional dehydration unit 22 and thus allows reducing the size of the dehydration unit 22, if any.
  • the feed 12 is cooled to the minimum possible temperature down while preventing the formation of CO2 hydrates or ice in the feed.
  • the first refrigerant 30 is circulated in the first cooling cycle 28 by the pump 58.
  • the first refrigerant 30, after exiting the second heat exchanger 38, is cooled in the third exchanger 40 by receiving cold from the partially heated gas 66, which is in the example natural gas still rather cold. This produces the fluid 70 at ambient temperature (or close to) which is advantageously exported to the network 72 or a user.
  • the first refrigerant 30, after passing in the third exchanger 40, is further cooled in the fifth heat exchanger 42 by receiving cold from the second refrigerant 34, in order to obtain the cooling stream 92.
  • the temperature of the cooling stream 92 is advantageously controlled above the temperature of CO2 hydrate formation in the feed 12 flowing in the second heat exchanger 38, in order to prevent such formation.
  • the compressed feed 18 is optionally dehydrated in the dehydrating unit 22.
  • the compressed feed 18 is then liquefied in the liquefaction unit 26 in order to obtain the CO2 rich liquid 14.
  • At least a first part 93 of the compressed feed 18 is precooled in the fourth heat exchanger 41 by heat exchange with a partially heated fluid 67 coming from the first heat exchanger 36, in order to obtain a precooled CO2 rich gas 94 and to heat the partially heated fluid 67.
  • the temperature of the partially heated gas 66 entering the fourth exchanger 41 is advantageously controlled above the CO2 freezing temperature, so that no freezing occurs in the fourth exchanger 41.
  • a heat exchange between at least a first portion 96 of the compressed feed 18 and the cold fluid 64 is performed in the first heat exchanger 36 in order to obtain a first stream 98 of CO2 rich liquid and the partially heated fluid 67.
  • the first portion 96 is at least a portion the precooled CO2 rich gas 94.
  • the first portion 96 is not a portion of the precooled CO2 rich gas 94, but a portion or the totality of the compressed feed 18 which is not precooled.
  • the intermediate fluid 74 is vaporized by heat exchange with the first portion 96 of the compressed feed 18, for example in a first section 36A of the first heat exchanger 36.
  • the vaporized intermediate fluid 74 for example goes up in a second section 36B of the first heat exchanger 36 where it is condensed by heat exchange with the cold fluid 64.
  • the condensed intermediate fluid 74 for example returns by gravity to the first section 36A below, where the intermediate fluid 74 is vaporized again.
  • the first portion 96 is thus liquefied and the cold fluid 64 thus heats and/or evaporates.
  • the first heat exchanger 36 may be a single piece of equipment, or two separate pieces of equipment comprising or forming section 36A and section 36B respectively.
  • the operating pressure of the intermediate fluid 74 allows controlling its temperature, and therefore the temperature of the first stream 98 of CO2 rich liquid. This is also used to ensure that the liquid intermediate fluid 74 has a temperature above the CO2 freezing temperature.
  • the use of the intermediate fluid 74 in the way described above may not allow to heat all the cold fluid 64 to ambient temperature. This may depend on what the operating pressure of the cold fluid 64 is, and what the temperature of the first stream 98 of CO2 rich liquid to be reached is.
  • the amount of LNG needed depends entirely on the exit temperature of the vaporized LNG. If the objective is to warm up entirely the LNG/NG to ambient temperature, so that it can be exported, the heat exchange between CO2 and LNG will set the LNG flow needed. If the LNG pressure is high (typically above 31 bar), the amount of LNG needed implies that LNG vaporizes at a temperature that is warmer than the CO2 liquefaction temperature, while it is not possible to liquefy CO2 with LNG that is too warm. This is known as a pinch effect. If the LNG pressure is low (typically below 31 bar), the pinch effect does not occur, and the entire heat exchange can take place in the first heat exchanger 36.
  • the flow of the cold fluid 64 can be increased relative to the flow of the first portion 96. Then, thanks to the excess of the cold fluid 64, the temperature of the partially heated fluid 67 will remain colder, and the pinch effect is avoided. However, due to the relatively large amount of the cold fluid 64, the partially heated fluid 67 exiting the first heat exchanger 36 is colder and cannot be sent directly to an export grid.
  • the fourth heat exchanger 41 (precooler) and the third heat exchanger 40 allow to warm-up the partially heated gas 66 (cold natural gas in the example) to ambient temperature so that it can be exported, while its energy is recovered. This improves the overall efficiency of the installation 10.
  • the CO2 rich liquid 14 is obtained from at least the first stream 98 of CO2 rich liquid.
  • the first stream 98 of CO2 rich liquid is flashed in the end flash drum 60 in order to obtain the CO2 rich liquid 14 and the end flash gas 68. This enables to improve the quality (purity) of the first stream 98 of CO2 rich liquid, since some light components, if any, go in the end flash gas 68.
  • the CO2 rich liquid 14 is advantageously pumped by the pump 62 at a target export pressure. This advantageously reduces the power required by the CO2 compressor 52 and improves the overall efficiency of the installation 10.
  • the target export pressure of the CO2 rich liquid 14 may be lower than the liquefaction pressure, in which case the pump 62 is not required.
  • a second portion 100 of the compressed feed 18 is cooled by heat exchange with the second refrigerant 34 in order to obtain a second stream 102 of CO2 rich liquid.
  • the second portion 100 does not flow in the first heat exchanger 36 and is diverted from the precooled CO2 rich gas 94 toward the sixth heat exchanger 44, and then advantageously the seventh heat exchanger 46.
  • Using two heat exchangers, corresponding to at least two pressure levels in the second cooling cycle 32 allows a better efficiency.
  • only one of the sixth heat exchanger 44 and the seventh heat exchanger 46 may be present.
  • the sixth heat exchanger 44 and the seventh heat exchanger 46 allow not to reduce the flow of liquefied CO2 produced in case there is not enough cold fluid 64, and/or allow overcoming the pinch effect without reducing the flow of liquefied CO2 produced.
  • the fourth heat exchanger 41 and the third heat exchanger 40 allow recovering the amount of cold still contained in the partially heated fluid 67 and the partially heated gas 66, this amount being particularly large when the cold fluid 64 is at a high pressure, for example above 31 bar.
  • the CO2 rich liquid 14 is obtained from the second stream 102 of CO2 rich liquid, which is for example mixed with the first stream 98 to be flashed in the end flash drum 60 and pumped by the pump 62.
  • a heat exchange is performed between at least a second part 104 of the compressed feed 18 and the end flash gas 68 in the eighth heat exchanger 48 in order to obtain a third stream 106 of CO2 rich liquid and to heat the end flash gas 68.
  • the third stream 106 is for example mixed with the first stream 98 and/or the second stream 102 to be flashed and pumped.
  • the second refrigerant 34 circulates in the second cooling cycle 32 ( Figure 2 ) which, in the example, involves four pressure levels, with the expansion organs 86A, 86B, and 86C or 86D in between the pressure levels.
  • the second refrigerant 34 is recovered from the suction drums 88A to 88C and is compressed in the compressor 76, which in the example has three stages.
  • the compressed second refrigerant 34 is then cooled in the medium pressure desuperheater 78 (or intercooler), and its pressure is advantageously further increased in the booster 80.
  • the second refrigerant then flows for example through the high pressure desuperheater 82A and the condenser 82B, and is recovered in the accumulator 84.
  • the CO2 critical point is at 31 °C. Therefore, CO2 does not condense if its temperature is higher.
  • the ability to condense CO2 below its critical point temperature with a cooling media provides an important advantage. However, in case the cooling media temperature does not allow to condense CO2 at a temperature below 31°C, CO2 is compressed sufficiently higher than its critical pressure, behaves like a liquid (even though it is not) and provides cooling when it is let down.
  • At least a stream 108 or all of the second refrigerant 34 is expanded in the expansion organ 86A in order to obtain a first cold stream 110 of the second refrigerant 34.
  • a heat exchange is performed between the first cold stream 110 and the first refrigerant 30 in the fifth heat exchanger 42 in order to obtain the cooling stream 92 of the first refrigerant 30.
  • some or all of the second refrigerant 34 may flow through the by-pass 90 to avoid the fifth heat exchanger 42 and be expanded in the expansion organ 86D.
  • the second refrigerant 34 enters the suction drum 88A and a liquid stream 112 is recovered and expanded in the expansion organ 86B in order to obtain a second cold stream 114 of the second refrigerant 34.
  • a heat exchange is performed between the second cold stream 114 and the second portion 100 of the compressed feed 18 in the sixth heat exchanger 44 in order to obtain the cold CO2 rich gaseous stream 118.
  • the remaining liquid fraction of second refrigerant 34, stream 116, is expanded in the expansion organ 86C in order to obtain a third cold stream 120 of the second refrigerant 34.
  • a heat exchange is performed between the third cold stream 120 and the gaseous stream 118 in the seventh heat exchanger 46 in order to obtain the second stream 102 of CO2 rich liquid.
  • cooling can be provided with LNG (or any other cold fluid 64). Maximum usage of those is considered to optimise the overall efficiency of the installation 10. This reduces the amount of power consumed by the second cooling cycle 32.
  • LNG from an LNG receiving terminal (not shown) may be considered.
  • LNG may be vaporized in the first heat exchanger 36.
  • the operating pressure of LNG may be adapted and compatible with export of the fluid 70 (natural gas).
  • the seawater may be used by the installation 10 instead (since not used anymore by the LNG terminal, as the LNG is vaporized in the first heat exchanger 36.
  • the installation 10 allows reducing the cost and energy consumption for producing the CO2 rich liquid 14.
  • the method uses the cold fluid 64, such as LNG.
  • the optional use of the intermediate fluid 74, and the fourth heat exchanger 41 allow overcoming thermal pinch, CO2 freezing and mechanical stress issues.
  • the overall heat integration provided by the different heat exchangers allows recovering the entire cold energy from LNG for example, since LNG is heated to ambient temperature and can be sent to the network 72 or to a user.
  • the size and duty of the latter is reduced. This is achieved by further cooling the wet CO2, using the first refrigerant 30. The risk of hydrate formation, or even freezing, is avoided by controlling the temperature of the cooling stream 92 of first refrigerant 30 above the CO2 hydrate formation temperature. Besides, the first refrigerant 30 is cooled using the partially heated gas 66 (cold natural gas in the example). Additional cooling of the first refrigerant 30 may be provided by the second cooling cycle 32 if needed.
  • the second cooling cycle 32 may be used to provide additional cooling to the liquefaction unit 26. Any type of refrigerant compatible for this service may be used, but as part of the disclosure, some of the compressed and optionally dehydrated feed 18 may be used as the second refrigerant 34.
  • the second cooling cycle 32 may involve only one pressure stage, or multiple pressure stages for better efficiency. Depending on the operating pressure of the cold fluid 64, and the CO2 precooling achieved in the fourth heat exchanger 41, the number of pressure stages in the second cooling cycle 32 may be adapted.
  • Using the final pump 62 allows liquefying CO2 before it is fully compressed to its final pressure, which reduces the power required by the CO2 compressor 52 and improves the overall efficiency of the installation 10.
  • the streams 98, 102 and/or 106 of CO2 rich liquid are advantageously flashed in the end flash drum 60. This allows removing most of the light components that may be present. Liquid CO2 quality (composition) is also improved.
  • the end flash gas 68 is advantageously sent to the eighth exchanger 48 where the cold of the end flash gas may be recovered for liquefaction. Once the end flash gas 68 is warm, it can be recycled back to the process unit 73.
  • the integration of the process of liquefaction of CO2 with the vaporization of LNG improves the efficiency of the process.
  • the method can accommodate with the use of LNG at high pressure (above 31 bar) or at low pressure (below 31 bar).
  • Utilities available from an LNG terminal may be shared with the installation 10 (such as cooling sea water, etc%) to further improve its efficiency.

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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)
  • Separation By Low-Temperature Treatments (AREA)
EP23307196.8A 2023-12-13 2023-12-13 Procédé de compression et de liquéfaction de co2 Pending EP4571224A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP23307196.8A EP4571224A1 (fr) 2023-12-13 2023-12-13 Procédé de compression et de liquéfaction de co2
TW113147847A TW202530615A (zh) 2023-12-13 2024-12-10 一種用於co2壓縮及液化之方法
PCT/EP2024/025336 WO2025124739A1 (fr) 2023-12-13 2024-12-10 Procédé de compression et de liquéfaction de co2

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3383873A (en) * 1964-11-03 1968-05-21 Linde Ag Engine expansion of liquefied gas at below critical temperature and above critical pressure
FR2975478A1 (fr) * 2011-05-18 2012-11-23 Air Liquide Procede et appareil de liquefaction d'un debit gazeux riche en dioxyde de carbone
WO2013055115A1 (fr) * 2011-10-11 2013-04-18 한국가스공사 Procédé de reliquéfaction du dioxyde de carbone
US8601833B2 (en) * 2007-10-19 2013-12-10 Air Products And Chemicals, Inc. System to cold compress an air stream using natural gas refrigeration
CN111692836A (zh) * 2019-03-12 2020-09-22 有进超低温(株) 使用液化天然气的冷能的氢液化装置
CN112284039A (zh) * 2019-07-25 2021-01-29 乔治洛德方法研究和开发液化空气有限公司 气体液化方法和气体液化设备
US20220252341A1 (en) * 2021-02-05 2022-08-11 Air Products And Chemicals, Inc. Method and system for decarbonized lng production
CN116357423A (zh) * 2023-04-11 2023-06-30 江苏科技大学 基于富氧燃烧碳捕集的lng动力船能量综合利用系统

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3045798A1 (fr) * 2015-12-17 2017-06-23 Engie Procede hybride de liquefaction d'un gaz combustible et installation pour sa mise en œuvre

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3383873A (en) * 1964-11-03 1968-05-21 Linde Ag Engine expansion of liquefied gas at below critical temperature and above critical pressure
US8601833B2 (en) * 2007-10-19 2013-12-10 Air Products And Chemicals, Inc. System to cold compress an air stream using natural gas refrigeration
FR2975478A1 (fr) * 2011-05-18 2012-11-23 Air Liquide Procede et appareil de liquefaction d'un debit gazeux riche en dioxyde de carbone
WO2013055115A1 (fr) * 2011-10-11 2013-04-18 한국가스공사 Procédé de reliquéfaction du dioxyde de carbone
CN111692836A (zh) * 2019-03-12 2020-09-22 有进超低温(株) 使用液化天然气的冷能的氢液化装置
CN112284039A (zh) * 2019-07-25 2021-01-29 乔治洛德方法研究和开发液化空气有限公司 气体液化方法和气体液化设备
US20220252341A1 (en) * 2021-02-05 2022-08-11 Air Products And Chemicals, Inc. Method and system for decarbonized lng production
CN116357423A (zh) * 2023-04-11 2023-06-30 江苏科技大学 基于富氧燃烧碳捕集的lng动力船能量综合利用系统

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