WO2013055115A1 - Procédé de reliquéfaction du dioxyde de carbone - Google Patents

Procédé de reliquéfaction du dioxyde de carbone Download PDF

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Publication number
WO2013055115A1
WO2013055115A1 PCT/KR2012/008239 KR2012008239W WO2013055115A1 WO 2013055115 A1 WO2013055115 A1 WO 2013055115A1 KR 2012008239 W KR2012008239 W KR 2012008239W WO 2013055115 A1 WO2013055115 A1 WO 2013055115A1
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stream
carbon dioxide
sub
heat exchange
expansion
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PCT/KR2012/008239
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English (en)
Korean (ko)
Inventor
이상규
이영범
전상희
양영명
신명호
박창원
차규상
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한국가스공사
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid 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
    • 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
    • F25J1/02—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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • 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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal 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
    • F25J1/0257—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
    • 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
    • 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
    • F25J2210/90—Boil-off gas from storage
    • 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
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention relates to a carbon dioxide reliquefaction process, and more particularly to a carbon dioxide reliquefaction process that can simplify the structure and operation of the reliquefaction process, and also lower the initial investment.
  • boil-off gas In general, carbon dioxide is liquefied and then transported to destinations by carriers while stored in tanks. During this transport, the liquefied carbon dioxide is partially vaporized due to external heat to generate boil-off gas (BOG). This boil-off gas is usually just discharged to the outside. However, simply discharging the boil-off gas as described above is not preferable for economic or environmental reasons, and various techniques for re-liquefying the boil-off gas through a constant reliquefaction process and introducing it into the tank are currently being studied. In connection with such a reliquefaction process, a boil-off gas reliquefaction apparatus in a carbon dioxide carrier or the like is usually a secondary device.
  • the present invention has been made to solve the above problems, the object of the present invention is to provide a carbon dioxide reliquefaction process that can simplify the structure and operation of the reliquefaction process, as well as lower the initial investment.
  • a carbon dioxide reliquefaction process for reliquefying the carbon dioxide stream evaporated from the tank in which the liquefied carbon dioxide is stored, the compression step of compressing the carbon dioxide stream, and the compression step And a first expansion step of expanding at least a portion of the carbon dioxide stream to lower the temperature of the carbon dioxide stream, wherein the carbon dioxide stream is at least partially supplied to the tank after the first expansion step.
  • the carbon dioxide reliquefaction process for reliquefying the carbon dioxide stream evaporated from the tank in which the liquefied carbon dioxide is stored, the compression step of compressing the carbon dioxide stream, the cooling step of cooling the carbon dioxide stream passed through the compression step A first heat exchange step of exchanging the carbon dioxide stream which has undergone the cooling step in the first heat exchange zone with the carbon dioxide stream evaporated from the tank, a first expansion step of expanding the carbon dioxide stream passing through the first heat exchange zone after the cooling step, and the first A first separation step of separating the expanded carbon dioxide stream into a gaseous first substream and a liquid phase substream, a first inflow step of introducing the first substream into the first heat exchange zone, and a first inflow step To expand the first sub stream passing through the first heat exchange zone.
  • the carbon dioxide reliquefaction process according to the present invention not only utilizes a separate refrigerant to reliquefy carbon dioxide, but also sometimes does not use a portion of carbon dioxide as a refrigerant, thereby compressing, condensing and expanding the refrigerant. No heat exchanger is required, and in some cases, the structure and operation of the carbon dioxide reliquefaction process can be greatly simplified, and the simplicity of the initial investment can be greatly reduced.
  • FIG. 1 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 1 of the present invention.
  • FIG. 2 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 2 of the present invention.
  • FIG. 3 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 3 of the present invention.
  • FIG. 4 is a flowchart illustrating a first modification of the carbon dioxide reliquefaction process of FIG. 3.
  • FIG. 5 is a flow chart showing a second modification of the carbon dioxide reliquefaction process of FIG. 3.
  • FIG. 6 is a flow chart showing a third modification of the carbon dioxide reliquefaction process of FIG.
  • FIG. 7 is a flow chart showing a modification of the carbon dioxide reliquefaction process of FIG.
  • FIG. 8 is a flowchart showing a carbon dioxide reliquefaction process according to Embodiment 4 of the present invention.
  • FIG. 9 is a flowchart illustrating a modification of the carbon dioxide reliquefaction process of FIG. 8.
  • FIG. 1 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 1 of the present invention.
  • the reliquefaction process according to the present embodiment is applied to a process of reliquefaction of boil-off gas (BOG) evaporated from the tank 700 in which liquefied carbon dioxide is stored. Carbon dioxide reliquefied according to this process is supplied back to the tank (700).
  • BOG boil-off gas
  • the carbon dioxide stream evaporated from the tank 700 is introduced into the compression means 710 through the conduit 110 and compressed.
  • the compression means 710 may be a conventional compressor.
  • the compressed carbon dioxide stream enters and cools the cooling means 720 through the conduit 130.
  • the cooling means 720 may be a water-cooled or air-cooled cooler.
  • an air-cooled cooler is more preferable.
  • the cooled carbon dioxide stream enters and expands through first conduit 150 to first expansion means 731 to lower its temperature.
  • the first expansion means 731 may be a J-T valve. Expansion means to be described later may be a J-T valve in the same manner as the first expansion means 731.
  • the pressure and temperature of the carbon dioxide stream can both be lowered by the J-T effect.
  • the carbon dioxide stream can be liquefied again.
  • This liquefied carbon dioxide stream is fed back to tank 700 through conduit 170.
  • the tank 700 may be provided with a discharge valve 740 for adjusting the pressure in the tank 700.
  • the discharge valve 740 is provided, impurities in the tank 700 may be removed by opening the discharge valve 740.
  • the carbon dioxide stream may be gaseous or liquid, depending on the thermodynamic properties at each location.
  • Evaporative gas reliquefaction apparatuses in carbon dioxide carriers or the like generally correspond to incidental apparatuses.
  • the general liquefaction process which puts the most importance on efficiency, it is more important that the carbon dioxide reliquefaction process is simple in structure and operation and low in initial investment.
  • the general liquefaction process usually requires a refrigerant. That is, in the general liquefaction process, the gas is liquefied by exchanging the gas with a refrigerant in a heat exchanger.
  • the general liquefaction process further requires means for compressing, condensing and expanding the refrigerant.
  • the reliquefaction process according to the present embodiment does not require a refrigerant as described above. Accordingly, no means for compressing, condensing and expanding the refrigerant is required.
  • the liquefaction process uses a portion of the gas similar to the refrigerant even though the refrigerant is not used. That is, in the liquefaction process using no refrigerant, a portion of the gas is lowered by compression and expansion, and then heat exchanged with the rest of the gas. Accordingly, even in a liquefaction process using no refrigerant, a heat exchanger for at least heat exchange is required. However, the reliquefaction process according to the present embodiment does not require a heat exchanger because some of the carbon dioxide streams are not used for heat exchange as described above.
  • the reliquefaction process according to the present embodiment does not use a separate refrigerant and does not use a portion of the carbon dioxide stream as a refrigerant, unlike a general liquefaction process, and thus means for compressing, condensing, and expanding the refrigerant, or heat exchange. No heat exchanger is required. Accordingly, the carbon dioxide reliquefaction process according to the present embodiment can not only greatly simplify the structure and operation, but also lower the initial investment cost due to this simplicity. In addition, since the following embodiments use part of the carbon dioxide stream similarly to the refrigerant, a heat exchanger for heat exchange is further required.
  • the reliquefaction process according to the following embodiments is more efficient than the reliquefaction process according to Example 1, but the structure is complicated.
  • the reliquefaction process according to the following embodiments does not use a refrigerant, its structure is relatively simple compared to other liquefaction processes.
  • the liquefaction processes according to the following embodiments are also very meaningful.
  • FIG. 2 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 2 of the present invention.
  • the reliquefaction process according to the present embodiment basically has the same configuration as the reliquefaction process according to the first embodiment described above.
  • the reliquefaction process according to the present embodiment is different from the reliquefaction process according to Example 1 in that heat exchange between carbon dioxide streams is used.
  • the same (or equivalent) parts with the same (or equivalent) parts as those described above will be given the same reference numerals, and detailed description thereof will be omitted.
  • the carbon dioxide stream evaporated from the tank 700 enters the first heat exchange zone 751 through the conduit 211.
  • the carbon dioxide stream then enters the compression means 710 through the conduit 212 and is compressed.
  • the compressed carbon dioxide stream enters and cools the cooling means 720 through the conduit 230.
  • the cooled carbon dioxide stream enters the first heat exchange region 751 through conduit 251 and exchanges heat with the carbon dioxide stream introduced into the first heat exchange region 751 through conduit 211.
  • the first heat exchange area 751 may be provided in a conventional heat exchanger. The same applies to the second heat exchange region 752 described later.
  • This heat exchange cools the carbon dioxide stream introduced into conduit 251 into first heat exchange zone 751. That is, this heat exchange is performed to take advantage of the cold heat of the carbon dioxide stream evaporated from the tank 700.
  • the efficiency of the entire liquefaction process can be improved.
  • the carbon dioxide stream enters and expands through the conduit 252 to the first expansion means 731 to further lower its temperature. Through this process, the liquefied carbon dioxide stream is fed back to the tank 700 through the conduit 270.
  • the aforementioned cooling means 720 is an optional configuration, in some cases, the cooling means 720 may not be provided. In such a case, the carbon dioxide stream may enter the first heat exchange zone 751 immediately after passing through the compression means 710.
  • FIG. 3 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 3 of the present invention.
  • the reliquefaction process according to the present embodiment basically has the same configuration as the reliquefaction process according to the second embodiment.
  • the reliquefaction process according to the present embodiment is different from the reliquefaction process according to Example 2 in that the carbon dioxide stream is separated into a gaseous stream and a liquid stream, and then the gaseous stream is used for heat exchange.
  • the same (or equivalent) parts with the same (or equivalent) parts as those described above will be given the same reference numerals, and detailed description thereof will be omitted.
  • the carbon dioxide stream evaporated from the tank 700 enters the first heat exchange zone 751 through conduit 311.
  • the carbon dioxide stream then enters the compression means 710 through the conduit 312 and is compressed.
  • the compressed carbon dioxide stream enters and cools the cooling means 720 through the conduit 330.
  • the cooled carbon dioxide stream enters the first heat exchange zone 751 through conduit 351 and exchanges heat with two carbon dioxide streams introduced into the first heat exchange zone 751 through conduits 311 and 373. This heat exchange cools the carbon dioxide stream introduced into the first heat exchange zone 751 through conduit 351.
  • this heat exchange is carried out to take advantage of the cold heat of the carbon dioxide stream evaporated from the tank 700 and the cold heat of the carbon dioxide stream which has passed through the second expansion means 732 (or separated gas phase by the first separation means) which will be described later. do.
  • the reliquefaction process according to the present embodiment uses the cold heat of the carbon dioxide stream evaporated from the tank 700 and the cold heat of the carbon dioxide stream passed through the second expansion means 732, thereby further improving the efficiency of the entire liquefaction process. Can be.
  • the carbon dioxide stream enters and expands through the conduit 352 to the first expansion means 731 to further lower its temperature.
  • This expanded carbon dioxide stream enters the first separation means 761 via a conduit 371 and is separated into a gaseous first substream and a liquid phase second substream.
  • the first separation means 761 may be a conventional vapor-liquid separator. Separation means to be described later may be a conventional gas-liquid separator similarly to the first separation means 761.
  • the first substream thus separated enters and expands through the conduit 372 to the second expansion means 732 to lower its temperature.
  • the expanded first sub-stream is introduced into the first heat exchange region 751 through the conduit 373.
  • the first sub stream is then discharged outward through conduit 374.
  • This first sub stream may comprise a large amount of nitrogen. Since nitrogen is a kind of impurity, it is preferable to be discharged to the outside.
  • the reliquefaction process according to the present embodiment does not simply discharge the first sub stream to the outside, but further utilizes the cold heat through heat exchange in the first heat exchange region 751, so that the overall efficiency may be further improved.
  • the impurities are discharged through the conduit 374, it is not necessary to use the above-described discharge valve 740 for the impurities discharge.
  • the liquid second sub-stream is fed back into the tank 700 as liquefied carbon dioxide (see conduit at 375).
  • Carbon dioxide reliquefaction process of this configuration can be modified as shown in FIG. 4 is a flowchart illustrating a first modification of the carbon dioxide reliquefaction process of FIG. 3.
  • the first sub stream is further divided into a third sub stream and a fourth sub stream.
  • the third sub-stream thus separated is introduced into and expanded through the second expansion means 732 through the conduit 3721 to lower its temperature.
  • This expanded third sub-stream enters the first heat exchange zone 751 through conduit 3722.
  • the third sub stream is discharged to the outside through the conduit 3723.
  • the fourth sub-stream is entrained in the carbon dioxide stream evaporated from the tank 700 and flows into the first heat exchange region 751 together with the carbon dioxide stream evaporated from the tank 700 (see the conduits 311 and 3724). .
  • FIG. 5 is a flowchart illustrating a second modification of the carbon dioxide reliquefaction process of FIG. 3.
  • the carbon dioxide stream passed through the cooling means 720 is separated into a third sub stream and a fourth sub stream.
  • the third sub stream enters the first heat exchange region 751 through conduit 3511 and exchanges heat with the carbon dioxide stream introduced into the first heat exchange region 751 through conduit 311.
  • the fourth sub-stream is introduced into the second heat exchange region 752 through the conduit 3512 to exchange heat with the carbon dioxide stream introduced into the second heat exchange region 752 through the conduit 373.
  • the third and fourth sub-streams together flow into the first expansion means 731.
  • the reliquefaction process according to the present modification has the advantage of using a heat exchanger having a simple structure compared to the reliquefaction process according to the third embodiment. That is, an expensive (and complex) triple heat exchanger is used in the reliquefaction process according to Example 3 because three streams flow in one heat exchange zone, but two streams are used in the reliquefaction process according to this variant. Since these flow in each of the two heat exchange zones, an expensive triple heat exchanger is not used.
  • FIG. 6 is a flowchart illustrating a third modification of the carbon dioxide reliquefaction process of FIG. 3.
  • the carbon dioxide stream passing through the first heat exchange zone 751 after the cooling means 720 passes through the first sub stream passing through the second expansion means 732 and the second heat exchange. Heat exchange is made in region 752.
  • FIG. 7 is a flowchart illustrating a modification of the carbon dioxide reliquefaction process of FIG. 6. As shown in FIG.
  • the carbon dioxide stream passing through the first heat exchange zone 751 after the cooling means 720 is introduced into the third expansion means 733 through the conduit 3531 and expanded.
  • the expanded carbon dioxide stream enters the second separation means 762 through conduit 3532 and is separated into a third sub stream in the gas phase and a fourth sub stream in the liquid phase.
  • the third sub-stream enters the second heat exchange zone 752 through conduit 3533.
  • the fourth sub-stream is introduced into the fourth expansion means 734 through the conduit 3534 and expanded and then supplied to the tank 700 together with the second sub-stream described above.
  • the remaining flow is the same as the reliquefaction process according to the third variant.
  • FIG. 8 is a flowchart illustrating a carbon dioxide reliquefaction process according to Embodiment 4 of the present invention.
  • the carbon dioxide stream evaporated from the tank 700 enters the first heat exchange zone 751 through conduit 411.
  • the carbon dioxide stream then enters the compression means 710 through conduit 412 and is compressed.
  • the compressed carbon dioxide stream enters and cools the cooling means 720 through the conduit 430.
  • the cooled carbon dioxide stream enters the first heat exchange zone 751 through conduit 451 to exchange heat with other carbon dioxide streams.
  • the carbon dioxide stream enters and expands through the conduit 452 to the first expansion means 731.
  • the expanded carbon dioxide stream enters the first separation means 761 via a conduit 471 and is separated into a first sub stream in the gas phase and a second sub stream in the liquid phase.
  • the first sub stream enters the first heat exchange zone 751 again through conduit 472.
  • the first sub stream then enters and expands through the conduit 473 to the second expansion means 732.
  • the first sub stream then enters the second separation means 762 via conduit 474 and is further separated into a third sub stream in the gas phase and a fourth sub stream in the liquid phase.
  • the third sub-stream enters and expands through third conduit 475 to third expansion means 733.
  • a fifth sub-stream see conduit of reference numeral 482) to be described later is mixed.
  • the third sub-stream then flows back into the first heat exchange zone 751 along with the fifth sub-stream, and then exits through the conduit 477 to the outside.
  • the second sub-stream enters the fourth expansion means 734 through the conduit 478 and expands, and then enters the third separation means 763 together with the fourth sub stream.
  • the third separating means 763 further separates the second and fourth sub-streams into a fifth sub-stream in the gas phase and a sixth sub-stream in the liquid phase.
  • the fifth sub stream enters the conduit 480 into the fifth expansion means 735 and expands. Then, as described above, the fifth sub stream is incorporated into the third sub stream through the third expansion means 733. And the sixth sub stream is supplied to the tank 700.
  • Carbon dioxide reliquefaction process of this configuration can be modified as shown in FIG. 9 is a flowchart illustrating a modification of the carbon dioxide reliquefaction process of FIG. 8.
  • the fifth sub-stream is not discharged to the outside, but is introduced back to the first heat exchange region 751 together with the carbon dioxide stream evaporated from the tank 700.
  • the fifth sub stream then enters the compression means 710 together with the carbon dioxide stream evaporated from the tank 700.
  • the reliquefaction process according to the present modification has an advantage of increasing the recovery rate of carbon dioxide because the fifth substream is not discharged to the outside.
  • the performance of the reliquefaction processes according to the above-described embodiment or modification can be expressed as shown in the table below.
  • the table below shows: 1) carbon dioxide (99.5%) and nitrogen (0.5%) are stored in the tank (assuming 8 Bar), 2) 1,000 kg of carbon dioxide evaporation gas (BOG) is generated per hour, and 3) carbon dioxide evaporates.
  • the results are calculated assuming that the gas consists of carbon dioxide (64%, 736 kg / h) and nitrogen (36%, 264 kg / h). However, the pressure of carbon dioxide was assumed to be the same for comparison between the reliquefaction processes.
  • the amount of reliquefaction represents the amount recovered in the tank 700 in the liquid state after 1,000 kg / h of carbon dioxide evaporated gas was reliquefied through the reliquefaction process
  • the required power represents the power of the compressor required for the reliquefaction process
  • the efficiency is the reliquefaction carbon dioxide.
  • 5 kg of CO 2 recovery rate represents the rate at which carbon dioxide entered into the reliquefaction process from the tank is reliquefied through the reliquefaction process and recovered to the tank 700.
  • the present invention relates to a carbon dioxide reliquefaction process that can not only simplify the structure and operation of the reliquefaction process but also lower the initial investment cost, and thus has industrial applicability.

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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)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

La présente invention concerne un procédé de reliquéfaction du dioxyde de carbone permettant de reliquéfier un courant de dioxyde de carbone évaporé d'une cuve stockant du dioxyde de carbone liquéfié. Le procédé de l'invention comprend : une étape de compression du courant de dioxyde de carbone ; et une première étape d'expansion d'au moins une partie du courant de dioxyde de carbone afin de diminuer la température du courant de dioxyde de carbone après l'étape compression, au moins une partie du courant de dioxyde de carbone étant introduite dans la cuve après la première étape d'expansion.
PCT/KR2012/008239 2011-10-11 2012-10-11 Procédé de reliquéfaction du dioxyde de carbone WO2013055115A1 (fr)

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Cited By (4)

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Publication number Priority date Publication date Assignee Title
FR3016436A1 (fr) * 2014-01-10 2015-07-17 Air Liquide Procede et appareil de liquefaction d’un courant de co2 gazeux
CN109080995A (zh) * 2018-10-10 2018-12-25 惠州市华达通石化有限公司 一种液体二氧化碳储罐气相外回收装置
WO2020012129A1 (fr) * 2018-07-11 2020-01-16 Engie Dispositif et procédé de liquéfaction d'un flux de dioxyde de carbone
FR3088416A1 (fr) * 2018-11-08 2020-05-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de liquefaction d'un courant gazeux contenant du dioxyde de carbone

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KR101309963B1 (ko) 2013-06-27 2013-09-17 한국가스공사 증발 가스의 재액화 방법
KR20160003474A (ko) 2014-07-01 2016-01-11 대우조선해양 주식회사 터보차저를 이용한 연료가스 공급시스템
KR20160003473A (ko) 2014-07-01 2016-01-11 대우조선해양 주식회사 터보차저를 이용한 bog 재액화 시스템 및 방법
KR20160003475A (ko) 2014-07-01 2016-01-11 대우조선해양 주식회사 터보차저를 이용한 연료가스 공급시스템
KR101763677B1 (ko) * 2014-11-24 2017-08-02 삼성중공업 주식회사 재액화 시스템
KR102379478B1 (ko) * 2020-10-16 2022-03-31 삼성중공업 주식회사 선박용 가스처리시스템

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3016436A1 (fr) * 2014-01-10 2015-07-17 Air Liquide Procede et appareil de liquefaction d’un courant de co2 gazeux
WO2020012129A1 (fr) * 2018-07-11 2020-01-16 Engie Dispositif et procédé de liquéfaction d'un flux de dioxyde de carbone
CN109080995A (zh) * 2018-10-10 2018-12-25 惠州市华达通石化有限公司 一种液体二氧化碳储罐气相外回收装置
CN109080995B (zh) * 2018-10-10 2024-05-07 惠州市华达通气体制造股份有限公司 一种液体二氧化碳储罐气相外回收装置
FR3088416A1 (fr) * 2018-11-08 2020-05-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de liquefaction d'un courant gazeux contenant du dioxyde de carbone

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