WO2009107743A1 - 液化ガス再液化装置、これを備えた液化ガス貯蔵設備および液化ガス運搬船、並びに液化ガス再液化方法 - Google Patents
液化ガス再液化装置、これを備えた液化ガス貯蔵設備および液化ガス運搬船、並びに液化ガス再液化方法 Download PDFInfo
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- WO2009107743A1 WO2009107743A1 PCT/JP2009/053594 JP2009053594W WO2009107743A1 WO 2009107743 A1 WO2009107743 A1 WO 2009107743A1 JP 2009053594 W JP2009053594 W JP 2009053594W WO 2009107743 A1 WO2009107743 A1 WO 2009107743A1
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- WIPO (PCT)
- Prior art keywords
- liquefied gas
- secondary refrigerant
- liquefied
- bog
- gas
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- 238000003860 storage Methods 0.000 title claims description 62
- 238000000034 method Methods 0.000 title claims description 17
- 239000003507 refrigerant Substances 0.000 claims abstract description 96
- 239000007788 liquid Substances 0.000 claims abstract description 89
- 238000009833 condensation Methods 0.000 claims abstract description 7
- 230000005494 condensation Effects 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims description 42
- 238000005057 refrigeration Methods 0.000 claims description 16
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 230000008018 melting Effects 0.000 claims description 4
- 238000002844 melting Methods 0.000 claims description 4
- 238000005259 measurement Methods 0.000 claims description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 228
- 239000007789 gas Substances 0.000 abstract description 109
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 77
- 229910001873 dinitrogen Inorganic materials 0.000 description 74
- 239000003949 liquefied natural gas Substances 0.000 description 56
- 238000000926 separation method Methods 0.000 description 24
- 230000032258 transport Effects 0.000 description 13
- 239000012071 phase Substances 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000004781 supercooling Methods 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013526 supercooled liquid Substances 0.000 description 1
Images
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
- F25J2270/91—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration using pulse tube refrigeration
Definitions
- the present invention relates to a liquefied gas reliquefaction device for reliquefying a boil-off gas (hereinafter referred to as “BOG”) vaporized from a liquefied gas such as LNG, a liquefied gas storage facility and a liquefied gas carrier equipped with the same, and a liquefied gas reliquefaction. It is about the method.
- BOG boil-off gas
- the LNG ship is provided with an LNG storage tank (liquefied gas storage tank) for storing LNG (liquefied natural gas).
- LNG liquefied natural gas
- LNG evaporates due to the intrusion heat that penetrates the tank insulation, and BOG is generated.
- BOG is generated in order to keep the internal pressure constant while avoiding an increase in the pressure in the LNG storage tank due to the BOG.
- a method for re-liquefying BOG and returning it to the LNG storage tank a method is generally used in which BOG extracted from the LNG storage tank is pressurized by a compressor, cooled by the cold generated by the refrigerator, and condensed. (See Patent Document 1).
- a Brayton cycle using nitrogen or the like as a primary refrigerant is used as a primary refrigerant.
- the conventional cooling method using the Brayton cycle requires a large-scale plant such as a compressor and an expander, and has a problem that a predetermined skill level is required for its handling.
- the present invention has been made in view of such circumstances, and a liquefied gas reliquefaction device that can be easily handled and can be easily handled, a liquefied gas storage facility and a liquefied gas carrier ship equipped with the same, and
- An object of the present invention is to provide a liquefied gas reliquefaction method.
- a liquefied gas reliquefaction apparatus is a liquefied gas reliquefaction apparatus for reliquefying BOG vaporized from a liquefied gas in a liquefied gas storage tank, wherein the secondary refrigerant is a liquid having a melting point lower than the condensation temperature of the BOG.
- the heat exchange means is provided in the vicinity of the liquefied gas storage tank.
- BOG vaporized from the liquefied gas in the liquefied gas storage tank is condensed and liquefied by the heat exchange means by the liquefied secondary refrigerant liquefied by the cooling means.
- the liquefied secondary refrigerant is conveyed to the heat exchange means by the liquefied secondary refrigerant conveying means.
- the secondary refrigerant circulates between the heat exchange means and the cooling means in the secondary refrigerant circulation passage.
- the heat exchange means is provided in the vicinity of the liquefied gas storage tank, so that the BOG can be reliquefied in the vicinity of the liquefied gas storage tank and separated from the liquefied gas storage tank.
- the secondary refrigerant liquefied by the cooling means is transported to the heat exchanging means by the liquefied secondary refrigerant transport means, and only needs to be circulated in the secondary refrigerant circulation channel, so the secondary refrigerant is transported to the heat exchange means.
- the configuration can be realized simply.
- the cooling means can be separated from the heat exchange means by the secondary refrigerant circulation flow path, and the cooling means can be remotely located from the liquefied gas storage tank. The handling of the means is further simplified.
- the cooling means mainly a forced circulation method in which the liquefied secondary refrigerant is supercooled (in this specification, supercooling means a state cooled to a liquid state below the boiling point); And a natural circulation condensation method in which the gas secondary refrigerant is cooled and condensed.
- liquefied gas typically, liquefied natural gas (LNG) is exemplified.
- LNG liquefied natural gas
- the “secondary refrigerant” only needs to have a lower melting point than BOG, and an inert gas such as nitrogen or a hydrocarbon gas such as propane can be used for the liquefied natural gas.
- a heat exchanger can be preferably used.
- a liquefied gas storage tank or a pipe through which a secondary refrigerant flows is attached to an attached pipe or fitting of the tank. Also good.
- the heat exchange means may be provided above the liquefied gas storage tank.
- the heat exchange means is provided above the liquefied gas storage tank, the liquefied gas condensed and liquefied by the heat exchange means can be returned to the lower liquefied gas storage tank using gravity. . Thereby, equipment such as a pump for pushing the reliquefied liquefied gas into the liquefied gas storage tank can be omitted.
- the heat exchange means may be provided in a header pipe provided above the plurality of liquefied gas storage tanks.
- a header pipe that joins and guides the BOG is provided.
- heat exchange means in the header pipe By providing heat exchange means in the header pipe, reliquefaction can be realized with a simple configuration. It is good also as providing header bypass piping which bypasses header piping, and providing a heat exchange means in this header bypass piping.
- precooling means for precooling the secondary refrigerant supplied to the secondary refrigerant circulation channel with the boil-off gas may be provided.
- a path for supplying the secondary refrigerant to the secondary refrigerant circulation flow path is provided, and the power for cooling and liquefying the secondary refrigerant by precooling the supplied secondary refrigerant using the cold heat of the BOG. Can be reduced.
- the liquefied secondary refrigerant transfer means may be capable of changing the flow rate of the transferred liquefied secondary refrigerant.
- the cooling means may include a plurality of pulse tube refrigerators.
- the pulse tube refrigerator is smaller than a conventional Brayton cycle refrigeration system, it is very easy to handle.
- a combination of a plurality of such pulse tube refrigerators it is possible to obtain high redundancy as a refrigeration system and to ensure flexibility in maintenance. Further, it is possible to realize a refrigeration system that does not require the skill level of the operator as compared with the conventional Brayton cycle type refrigeration system.
- thermometer Based on the measurement results of at least one of a thermometer, a pressure gauge, and a pump discharge flow meter installed in the liquefied gas storage tank, control of the number of operating pulse tube refrigerators and / or each of the pulse tubes It is preferable to control the refrigeration capacity of the refrigerator.
- composition and / or pressure of the secondary refrigerant can be set so that the BOG is condensed by evaporation of the secondary refrigerant. Thereby, the quantity of the secondary refrigerant
- the liquefied gas storage facility of the present invention comprises a liquefied gas storage tank and any one of the above liquefied gas reliquefaction devices for reliquefying BOG vaporized from the liquefied gas in the liquefied gas storage tank.
- the liquefied gas reliquefaction apparatus described above can be suitably used for a liquefied gas storage facility.
- An example of the liquefied gas storage facility is an offshore LNG storage facility that stores LNG on the ocean.
- the liquefied gas carrier of the present invention includes a liquefied gas storage tank and any one of the above liquefied gas reliquefaction devices for reliquefying BOG vaporized from the liquefied gas in the liquefied gas storage tank. To do.
- the above-described liquefied gas reliquefaction apparatus can be suitably used for a liquefied gas carrier ship.
- An example of the liquefied gas carrier ship is an LNG ship that carries LNG.
- the liquefied gas reliquefaction method of the present invention is a liquefied gas reliquefaction method in which BOG vaporized from a liquefied gas in a liquefied gas storage tank is reliquefied.
- heat exchange means provided in the secondary refrigerant circulation flow path for heat exchange between the liquefied secondary refrigerant conveyed by the liquefied secondary refrigerant conveyance means and the BOG to condense and liquefy the boil-off gas. And heat exchange by the heat exchange means is performed in the vicinity of the liquefied gas storage tank.
- the heat exchange means for reliquefying BOG with the secondary refrigerant is provided in the vicinity of the liquefied gas storage tank, the liquefied gas reliquefaction apparatus can be realized with a simple configuration.
- the cooling means is constituted by a plurality of pulse tube refrigerators, it is possible to obtain a refrigeration system that can obtain high redundancy as a refrigeration system and does not require the skill level of an operator.
- LNG reliquefaction equipment (liquefied gas reliquefaction equipment) 3 Cargo tank (liquefied gas storage tank) 7 Vapor header line (header piping) 12 Heat exchanger (heat exchange means) 20 Refrigerator group (cooling means) 21 Pulse tube refrigerator 22 Transport pump (liquefied secondary refrigerant transport means) 24 Secondary refrigerant circulation passage 26 Gas-liquid separation tank
- FIG. 1 shows a main part of an LNG ship (liquefied gas carrier ship) provided with a gas reliquefaction device 1.
- the LNG ship includes a plurality of independent spherical cargo tanks (liquefied gas storage tanks) 3, and liquefied natural gas (LNG) is stored in each cargo tank 3.
- LNG liquefied natural gas
- Above each cargo tank 3 is a vapor header line (vapor) via a gate valve 5.
- header line) 7 is provided.
- the vapor header line 7 is connected to the cargo tanks 3 in common, and is a pipe that collects BOG (hereinafter referred to as “BOG”) in which the LNG has evaporated in each cargo tank 3.
- BOG BOG
- the vapor header line 7 is provided with a bypass line (header bypass pipe) 9 branched from the vapor header line 7 and flowing in parallel. Gate valves 10 are respectively provided at both ends of the bypass line 9.
- a heat exchanger 12 is accommodated in the flow path of the bypass line 9, and the BOG evaporated from each cargo tank 3 is condensed and liquefied by the heat exchanger 12.
- the bypass line 9 is provided with a pre-cooling heat exchanger 14 for circulating a part of the BOG and pre-cooling the nitrogen gas with the cold heat of the BOG.
- the nitrogen gas is compressed by a compressor 43 described later, and then supplied to the precooling heat exchanger 14 through the first nitrogen gas supply pipe 13.
- the LNG return pipe 16 is connected only to the two cargo tanks 3 from the left in the figure, but this is only omitted in order to avoid the complexity of the illustration.
- the LNG return pipe 16 is also connected to the two cargo tanks 3 from the side.
- the heat exchanger 12 includes the United States Chart Energy & Chemicals core in kettle (registered trademark) is preferred. Specifically, a core 18 through which liquid nitrogen (LN 2 ) is guided is disposed in the bypass line 9.
- the core 18 is a plate fin type heat exchanger.
- the liquid nitrogen introduced into the core 18 is evaporated by exchanging heat with the surrounding BOG and flows out from the core 18 as nitrogen gas (N 2 ).
- N 2 nitrogen gas
- FIG. 2A the LNG cooled and condensed into a liquid by the heat exchanger 12 is taken out from below and led to each cargo tank 3 through the LNG return pipe 16 shown in FIG. It is burned.
- BOG is supplied from the upper two locations, which is different from the BOG flow path shown in FIG.
- a core 18 ′ may be provided in the middle of the bypass line 9 and the core 18 ′ may be immersed in LN 2 .
- the gas reliquefaction apparatus 1 includes the heat exchanger 12 described above, a refrigerator group (cooling means) 20 that supercools liquid nitrogen, a transport pump (liquefied secondary refrigerant transport means) 22 that transports liquid nitrogen, A circulation channel (secondary refrigerant circulation channel) 24 that circulates nitrogen, which is a secondary refrigerant, between the heat exchanger 12 and the refrigerator group 20 is mainly provided.
- the refrigerator group 20 includes a plurality of pulse tube refrigerators 21.
- the pulse tube refrigerator 21 forms a pressure wave in a pulse tube filled with helium or the like by a compressor using a linear motor, for example. Cold is obtained by forming a phase difference.
- This pulse tube refrigerator 21 has the advantage that it is not necessary to provide a sliding part in the cold heat generating part and can be configured with low vibration. As shown in FIG. 1, a large number of pulse tube refrigerators 21 are connected in parallel and in series to the liquid nitrogen flow path so as to supercool the liquid nitrogen. By connecting a plurality of pulse tube refrigerators 21 in this way, it is possible to flexibly cope with the required refrigeration capacity and realize a configuration with excellent maintainability.
- the conveyance pump 22 conveys the liquid nitrogen cooled by the refrigerator group 20 to the heat exchanger 12 and circulates it, and in this embodiment, two are provided in parallel.
- Each conveyance pump 22 has a variable number of rotations, and the discharge flow rate can be arbitrarily changed. As described above, by appropriately changing the discharge flow rate, it is possible to prevent liquid nitrogen with supercooling from staying in the pipe and solidifying the liquid nitrogen.
- a gas-liquid separation tank 26 is provided between the transport pump 22 and the refrigerator group 20.
- a refrigerator outlet side lower pipe 27 is connected below the gas-liquid separation tank 26, and liquid nitrogen is supplied from the refrigerator group 20 to the lower side of the tank 27.
- a refrigerator outlet side upper pipe 28 is connected above the gas-liquid separation tank 26, and liquid nitrogen supplied from the refrigerator group 20 is sprayed into the gas phase formed above the tank 26. It has come to be. By thus spraying liquid nitrogen into the gas phase, the nitrogen gas supplied into the tank 26 is effectively condensed.
- the refrigerator outlet side lower pipe 27 is provided with a pressure control valve 27a so that the liquid phase pressure in the gas-liquid separation tank 26 can be controlled.
- the refrigerator outlet side upper pipe 28 is provided with a pressure reducing valve 28a so that the flow rate of liquid nitrogen supplied into the gas-liquid separation tank 26 can be controlled.
- a liquid nitrogen outflow pipe 30 connected to the upstream side of the transfer pump 22 is provided at the lower end of the gas-liquid separation tank 26. Liquid nitrogen is extracted from the liquid nitrogen outflow pipe 30 and is transported by the transport pump 22.
- a liquid nitrogen discharge pipe 32 is provided on the downstream side of the transport pump 22. The liquid nitrogen discharge pipe 32 is provided between the transport pump 22 and the heat exchanger 12. The liquid nitrogen discharge pipe 32 is provided with a pressure control valve 32 a so that the pressure of liquid nitrogen supplied to the heat exchanger 12 can be controlled.
- a liquid nitrogen bypass pipe 34 is provided between the lower portion of the gas-liquid separation tank 26 and the midway position of the liquid nitrogen discharge pipe 32. A part of the liquid nitrogen can be returned to the gas-liquid separation tank 26 by the liquid nitrogen bypass pipe 34.
- a return gas cooling exchanger 38 for precooling nitrogen gas introduced from the heat exchanger 12 through the nitrogen gas return pipe 36 is provided above the gas-liquid separation tank 26, a return gas cooling exchanger 38 for precooling nitrogen gas introduced from the heat exchanger 12 through the nitrogen gas return pipe 36 is provided.
- the return gas cooling heat exchanger 38 is connected to a liquid nitrogen branch pipe 40 branched from a midway position of the liquid nitrogen discharge pipe 32 so that supercooled liquid nitrogen is introduced. . Further, the liquid nitrogen flowing out from the return gas cooling heat exchanger 38 is guided to the refrigerator group 20 via the refrigerator group inlet pipe 42.
- the circulation path 24 for nitrogen as the secondary refrigerant is mainly constituted by the transport pump 22, the liquid nitrogen discharge pipe 32, the heat exchanger 12, the nitrogen gas return pipe 36, and the gas-liquid separation tank 26. .
- Nitrogen used as the secondary refrigerant is supplied from a nitrogen gas generator (not shown).
- the nitrogen supplied from the nitrogen gas supply device is guided to the nitrogen gas storage tank 53 after moisture and carbon dioxide gas are removed by a nitrogen gas dryer 51 (see the lower right in FIG. 1).
- the nitrogen gas storage tank 53 is at room temperature.
- a compressor 54 that is rotationally driven by a motor 54 a is provided on the upstream side of the nitrogen gas storage tank 53.
- a screw type is preferably used as the compressor 54.
- the nitrogen gas whose pressure has been increased by the compressor 54 passes through the nitrogen gas discharge pipe 55 and is led to the first nitrogen gas supply pipe 13 and the second nitrogen gas supply pipe 57 at the branch point 55a.
- the nitrogen gas introduced through the first nitrogen gas supply pipe 13 is pre-cooled by the BOG in the pre-cooling heat exchanger 14 and then the nitrogen gas return pipe 36 positioned in the immediate vicinity of the heat exchanger 12. It joins the upstream side.
- the nitrogen gas introduced through the second nitrogen gas supply pipe 57 is joined to the downstream side of the gas return pipe 36 located immediately upstream of the return gas precooling heat exchanger 38.
- the liquid nitrogen stored in the gas-liquid separation tank 26 is taken out from the lower end of the tank 26 through the liquid nitrogen outflow pipe 30 by the transfer pump 22 and is transferred to the heat exchanger 12 through the liquid nitrogen discharge pipe 32.
- the pressure of liquid nitrogen led to the heat exchanger 12 is adjusted by the pressure control valve 32a.
- the liquid nitrogen guided to the heat exchanger 12 exchanges heat with the BOG guided to the bypass line 9. That is, in the heat exchanger 12, the liquid nitrogen gives latent heat of evaporation to the BOG and evaporates.
- the BOG is cooled by the latent heat of vaporization of liquid nitrogen and becomes condensed.
- the condensed and liquefied BOG is returned to each cargo tank 3 via the LNG return pipe 16 as liquefied LNG.
- the nitrogen evaporated in the heat exchanger 12 is led to the return gas precooling heat exchanger 38 through the nitrogen gas return pipe 36 as nitrogen gas.
- the nitrogen gas is cooled by liquid nitrogen partially branched from the liquid nitrogen branch pipe 40.
- the nitrogen gas cooled by the return gas precooling heat exchanger 38 is guided from above the gas-liquid separation tank 26 into the tank 26.
- liquid nitrogen guided from the refrigerator outlet side upper pipe 28 is sprayed, whereby the nitrogen gas supplied from above is condensed and liquefied, and the lower space in the tank 26.
- the flow rate of liquid nitrogen sprayed into the tank 26 can be adjusted by the pressure reducing valve 28a.
- Liquid nitrogen is cooled by the refrigerator group 20. That is, the liquid nitrogen introduced through the refrigerator group inlet pipe 42 is cooled and supercooled by the pulse tube refrigerator 21 connected in series and in parallel. The liquid nitrogen after supercooling flows out through the refrigerator group outlet pipe 43, a part branches to the refrigerator outlet side upper pipe 28, and the remaining part flows to the refrigerator outlet side lower pipe 27. When the liquid nitrogen passes through the refrigerator outlet side lower pipe 27, the pressure is adjusted by the pressure control valve 27 a and then flows into the gas-liquid separation tank 26.
- nitrogen is supplied to the circulation channel 24 as follows. Nitrogen introduced from a nitrogen gas generator (not shown) is introduced into the nitrogen gas storage tank 53 after moisture and carbon dioxide gas are removed by the nitrogen gas dryer 51. The nitrogen gas boosted by the compressor 54 driven by the motor 54a and guided from the nitrogen gas storage tank 53 is supplied to the first nitrogen gas supply pipe 13 and the second nitrogen gas supply pipe 57 at the branch point 55a. Led. The nitrogen gas led to the first nitrogen gas supply pipe 13 is precooled by the sensible heat of the BOG in the precooling heat exchanger 14 and led to the nitrogen gas return pipe 36. The BOG after the cold heat is applied by the pre-cooling heat exchanger 14 is burned by a combustion means (not shown) and then released to the atmosphere.
- a combustion means not shown
- the reason why a part of the BOG is incinerated in this way is to discharge the nitrogen content that remains in the cargo tank 3 and is concentrated.
- the nitrogen gas guided to the second nitrogen gas supply pipe 57 joins the downstream side of the nitrogen gas return pipe 36 and is then cooled by the return gas precooling heat exchanger 38.
- the LNG reliquefaction apparatus 1 has the following operational effects. Since the heat exchanger 12 for condensing and liquefying BOG is provided in the vicinity of the cargo tank 3, the BOG generated in the cargo tank 3 can be liquefied in the vicinity of the cargo tank 3. Therefore, it is possible to eliminate as much as possible a system such as a pipe for guiding the BOG to a cooling device installed at a remote part away from the cargo tank 3. As a result, it is possible to prevent the BOG from rising due to intrusion heat while transporting the BOG to the cooling device, and to reduce the cooling power for liquefying the BOG. Further, since the liquid is reliquefied in the vicinity of the cargo tank 3, when the reliquefied LNG is returned to the cargo tank 3, only the LNG return pipe 16 is required, and a system such as a redundant pipe can be eliminated.
- the secondary refrigerant (nitrogen) liquefied by the refrigerator group 20 is only transported to the heat exchanger 12 by the transport pump 22 and is circulated in the secondary refrigerant circulation passage 24, the secondary refrigerant (nitrogen) is transferred to the heat exchanger 12.
- a configuration for transporting the secondary refrigerant (nitrogen) can be easily realized.
- the refrigerating machine group 20 can be separated from the heat exchanger 12 by the secondary refrigerant circulation passage 24 and can be remotely arranged from the cargo tank 3, so that the refrigerating machine group 20 can be arranged outside the gas danger zone.
- the handling of the refrigerator group 20 is further simplified.
- the LNG condensed and liquefied by the heat exchanger 12 can be returned to the cargo tank 3 below using gravity. Thereby, equipment such as a pump for pushing the liquefied LNG into the cargo tank 3 can be omitted.
- a bypass line 9 arranged in parallel with the vapor header line 7 provided above the LNG tank was provided, and the heat exchanger 12 was arranged in the bypass line 9.
- a first nitrogen gas supply pipe 13 for supplying nitrogen gas (secondary refrigerant) to a nitrogen gas return pipe 36 that is one of the secondary refrigerant circulation channels 24 is provided. Since the pre-cooling heat exchanger 14 is pre-cooled by the cold heat of the BOG, power for liquefying nitrogen gas can be reduced. Further, since the normal temperature nitrogen gas introduced from the second nitrogen gas supply pipe 57 is precooled by the return gas precooling heat exchanger 38, the power for cooling and liquefying the nitrogen gas can be reduced.
- the refrigeration group 20 is configured by using a plurality of pulse tube refrigerators 21 that are small and extremely easy to handle. Therefore, high redundancy can be obtained, flexibility in maintenance can be ensured, and a system that does not require operator skill can be realized.
- the nitrogen gas return pipe 36 that returns the nitrogen gas evaporated and evaporated in the heat exchanger 12 is directly connected to the gas-liquid separation tank 26. That is, the nitrogen gas returned from the nitrogen gas return pipe 36 is supplied to the gas phase portion in the gas-liquid separation tank 26 without passing through a heat exchanger for precooling (see reference numeral 38 in FIG. 1).
- a refrigerator group inlet pipe 42 is connected to the upper end of the gas-liquid separation tank 26. Nitrogen gas in the gas-liquid separation tank 26 is extracted from this position and led to the refrigerator group 20 to be cooled. Condensed liquid.
- FIG. 3 only a plurality of pulse tube refrigerators 21 constituting the refrigerator group 20 are connected in parallel and not connected in series. However, the present invention is not particularly limited to such a configuration. Alternatively, a plurality of pulse tube refrigerators 21 may be connected in parallel and in series.
- the liquid nitrogen cooled and condensed into the refrigeration group 20 is guided into the gas-liquid separation tank 26 via the refrigeration group outlet pipe 43 and stored in the tank 26.
- the nitrogen gas compressed by the compressor 54 passes through the nitrogen gas discharge pipe 55, passes through the gas-gas heat exchanger 60, and is led to the refrigerator group 20.
- the gas-gas heat exchanger 60 the normal temperature nitrogen gas flowing through the nitrogen gas discharge pipe 55 and the cooled nitrogen gas guided through the nitrogen gas recovery pipe 62 branched from the refrigerator inlet pipe 42 are heat exchanged. Is done.
- the nitrogen gas supplied from the compressor 54 is pre-cooled and guided to the refrigerator group 20. Thereby, the cooling power for condensing the nitrogen gas is saved.
- the liquid nitrogen stored in the gas-liquid separation tank 26 is taken out from the lower end of the tank 26 through the liquid nitrogen outflow pipe 30 by the transfer pump 22 and is transferred to the heat exchanger 12 through the liquid nitrogen discharge pipe 32.
- the liquid nitrogen guided to the heat exchanger 12 exchanges heat with the BOG guided to the bypass line 9. That is, in the heat exchanger 12, the liquid nitrogen gives latent heat of evaporation to the BOG and evaporates.
- the BOG is cooled by the latent heat of vaporization of liquid nitrogen and becomes condensed.
- the condensed and liquefied BOG is returned to each cargo tank 3 via the LNG return pipe 16 as liquefied LNG.
- the nitrogen evaporated in the heat exchanger 12 is led as nitrogen gas to the gas phase portion in the gas-liquid separation tank 26 through the nitrogen gas return pipe 36.
- the nitrogen gas introduced into the gas-liquid separation tank 26 is guided from the refrigerator group inlet pipe 42 to the refrigerator group 20 and is cooled by each pulse tube refrigerator 21 to be condensed and liquefied.
- a natural circulation condensation method in which nitrogen gas is condensed and liquefied by the refrigerator group 20 is employed.
- the liquefied liquid nitrogen is led to the gas-liquid separation tank 26 via the refrigerator group outlet pipe 43 and stored in the lower part of the tank 26.
- the gas-gas heat exchanger 60 exchanges heat with normal temperature nitrogen gas flowing from the compressor 54 driven by the motor 54a through the nitrogen gas discharge pipe 55. To do. Thereby, the nitrogen gas sent from the compressor 54 to the refrigerator group 20 will be pre-cooled, and the cooling power of each pulse tube refrigerator 21 can be reduced.
- the LNG reliquefaction apparatus 1 has the following operational effects. Since the heat exchanger 12 for condensing and liquefying BOG is provided in the vicinity of the cargo tank 3, the BOG generated in the cargo tank 3 can be liquefied in the vicinity of the cargo tank 3. Therefore, it is possible to eliminate as much as possible a system such as a pipe for guiding the BOG to a cooling device installed at a remote part away from the cargo tank 3. As a result, it is possible to prevent the BOG from rising due to intrusion heat while transporting the BOG to the cooling device, and to reduce the cooling power for liquefying the BOG. Further, since the liquid is reliquefied in the vicinity of the cargo tank 3, when the reliquefied LNG is returned to the cargo tank 3, only the LNG return pipe 16 is required, and a system such as a redundant pipe can be eliminated.
- the refrigerator can be used as in the prior art. Compared with the case where the liquefied primary refrigerant is conveyed, the handling of the liquefied refrigerant is facilitated, and a configuration for conveying the secondary refrigerant to the heat exchanger 12 can be easily realized.
- the refrigerating machine group 20 can be separated from the heat exchanger 12 by the secondary refrigerant circulation passage 24 and can be remotely arranged from the cargo tank 3, so that the refrigerating machine group 20 can be arranged outside the gas danger zone.
- the handling of the refrigerator group 20 is further simplified.
- the LNG condensed and liquefied by the heat exchanger 12 can be returned to the cargo tank 3 below using gravity. Thereby, equipment such as a pump for pushing the liquefied LNG into the cargo tank 3 can be omitted.
- a bypass line 9 arranged in parallel with the vapor header line 7 to which the BOG provided above the LNG tank is guided is provided, and the heat exchanger 12 is arranged in the bypass line 9.
- the cooling power of the pulse tube refrigerator 21 constituting the refrigerator group 20 is reduced. be able to.
- the refrigeration group 20 is configured by using a plurality of pulse tube refrigerators 21 that are small and extremely easy to handle. Therefore, high redundancy can be obtained, flexibility in maintenance can be ensured, and a system that does not require operator skill can be realized.
- the LNG gas reliquefaction apparatus used for the LNG ship has been described.
- the present invention is not limited to this, for example, an LNG storage facility, particularly an LNG storage facility installed on the ocean. Good.
- LNG was demonstrated as an example as gas to reliquefy, this invention is not limited to this, It can replace with LNG and can be applied also to LPG, ammonia, etc.
- nitrogen was described as an example of the secondary refrigerant, the present invention is not limited to this, and other gases such as an inert gas such as argon may be used instead of nitrogen.
- the composition and / or pressure of the secondary refrigerant can be set so that the BOG is condensed by evaporation of the secondary refrigerant.
- coolant circulated to a heat exchange means can be reduced significantly.
- the number of operating pulse tube refrigerators 21 and / or each pulse tube refrigeration is controlled. It is preferable to control the refrigerating capacity of the machine 21.
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Abstract
Description
本発明にかかる液化ガス再液化装置は、液化ガス貯蔵タンク内の液化ガスから気化したBOGを再液化する液化ガス再液化装置において、前記BOGの凝縮温度よりも融点が低い液体である二次冷媒が循環する二次冷媒循環流路に設けられ、該二次冷媒を液化する冷却手段と、該冷却手段によって冷却された液化二次冷媒を前記二次冷媒循環流路内で搬送する液化二次冷媒搬送手段と、前記二次冷媒循環流路に設けられ、前記液化二次冷媒搬送手段によって搬送された液化二次冷媒と前記BOGとを熱交換させて該BOGを凝縮液化させる熱交換手段とを備え、該熱交換手段は、前記液化ガス貯蔵タンクの近傍に設けられていることを特徴とする。
本発明の液化ガス再液化装置では、熱交換手段を液化ガス貯蔵タンクの近傍に設けることとしたので、BOGを液化ガス貯蔵タンクの近傍にて再液化することができ、液化ガス貯蔵タンクから離れた遠隔部に設置された冷却装置までBOGを導くための配管等の系統を可及的に排除することができる。これにより、BOGを冷却装置まで輸送する間にBOGが侵入熱によって温度上昇してしまうことを回避することができ、BOGを再液化するための冷却動力を低減することができる。また、液化ガス貯蔵タンクの近傍にて再液化するので、再液化した液化ガスを液化ガス貯蔵タンクへと返送する配管等の系統を簡便化することができる。
冷却手段によって液化された二次冷媒を液化二次冷媒搬送手段によって熱交換手段へと搬送し、二次冷媒循環流路内を循環させるだけで済むので、熱交換手段まで二次冷媒を搬送する構成が簡便に実現することができる。
二次冷媒循環流路によって熱交換手段から冷却手段を分離し、冷却手段を液化ガス貯蔵タンクから遠隔配置することが可能となるので、冷却手段をガス危険区域外に配置することができ、冷却手段の取扱いがさらに簡便となる。
冷却手段による冷熱取得方式としては、主として、液化二次冷媒を過冷却(本明細書において、過冷却とは沸点以下で液状の状態に冷却された状態を意味する。)する強制循環方式と、ガス二次冷媒を冷却凝縮する自然循環凝縮方式とが挙げられる。
ここで、「液化ガス」としては、典型的には、液化天然ガス(LNG)が挙げられる。
「二次冷媒」としては、BOGよりも低融点であれば良く、液化天然ガスに対しては、窒素等の不活性ガスや、プロパン等の炭化水素ガスを用いることができる。
「熱交換手段」としては、好適には、熱交換器を用いることができ、これ以外には、液化ガス貯蔵タンクまたは該タンクの付属配管やフィッティングに二次冷媒が流れる配管を巻き付けた構成としても良い。
ヘッダ配管をバイパスするヘッダバイパス配管を設け、このヘッダバイパス配管内に熱交換手段を設けることとしても良い。
また、複数のパルスチューブ冷凍機によって冷却手段を構成することとしたので、冷凍システムとして高い冗長性を得ることができるとともに作業者の熟練度を要求しない冷凍システムを実現することができる。
3 カーゴタンク(液化ガス貯蔵タンク)
7 ベイパーヘッダーライン(ヘッダ配管)
12 熱交換器(熱交換手段)
20 冷凍機群(冷却手段)
21 パルスチューブ冷凍機
22 搬送ポンプ(液化二次冷媒搬送手段)
24 二次冷媒循環流路
26 気液分離タンク
[第一実施形態]
以下、本発明の第一実施形態について、図1を用いて説明する。
図1には、ガス再液化装置1を備えたLNG船(液化ガス運搬船)の要部が示されている。
LNG船は、複数の独立した球形のカーゴタンク(液化ガス貯蔵タンク)3を備えており、各カーゴタンク3内には液化天然ガス(LNG)が貯蔵されている。
各カーゴタンク3の上方には、仕切弁5を介してベイパーヘッダーライン(vapor
header line;ヘッダ配管)7が設けられている。ベイパーヘッダーライン7は、各カーゴタンク3に対して共通に接続されており、各カーゴタンク3内でLNGが蒸発したBOG(以下「BOG」という。)を回収する配管である。ベイパーヘッダーライン7には、このベイパーヘッダーライン7から分岐して並列的に流れるバイパスライン(ヘッダバイパス配管)9が設けられている。バイパスライン9の両端部には、仕切弁10がそれぞれ設けられている。
バイパスライン9には、一部のBOGを流通させ、BOGが有する冷熱によって窒素ガスを予冷するための予冷熱交換器14が設けられている。窒素ガスは、後述する圧縮機43によって圧縮された後に、第1窒素ガス供給配管13を介して予冷熱交換器14へと供給される。
バイパスライン9の下部には、熱交換器12によって再液化されたLNGを各カーゴタンク3へと返送するためのLNG返送配管16が設けられている。なお、図1では、LNG返送配管16が同図において左方から2つのカーゴタンク3にのみ接続されているが、これは図示の煩雑さを避けるために省略しただけであり、同図において右方から2つのカーゴタンク3にもLNG返送配管16は接続されている。
Chemicals社のコア・イン・ケトル(core in kettle;登録商標)が好適である。具体的には、バイパスライン9内に、液体窒素(LN2)が導かれるコア18が配置された構成とされる。コア18は、プレートフィン型の熱交換器となっている。コア18内に導かれた液体窒素は、周囲のBOGと熱交換して蒸発し、窒素ガス(N2)となってコア18から流出する。
図2Aに示されているように、熱交換器12にて冷却されて凝縮液化したLNGは、下方から取り出され、図1にて示したLNG返送配管16を通って各カーゴタンク3へと導かれる。
なお、図2Aにおいて、BOGが上方の2箇所から供給される構成となっており、図1に示したBOGの流路と異なっているが、これは理解の容易のために示しただけであり、BOGについては熱交換器12へと導かれる構成であれば、その流通形態は限定されない。例えば、図2Bに示すように、バイパスライン9の中途位置にコア18’を設け、このコア18’がLN2に浸漬されるように構成しても良い。
なお、冷凍機出口側下方配管27には、圧力制御弁27aが設けられており、気液分離タンク26内の液相圧力が制御できるようになっている。また、冷凍機出口側上方配管28には、減圧弁28aが設けられており、気液分離タンク26内に供給する液体窒素の流量が制御できるようになっている。
搬送ポンプ22の下流側には、液体窒素吐出配管32が設けられている。液体窒素吐出配管32は、搬送ポンプ22と熱交換器12との間にわたって設けられている。液体窒素吐出配管32には、圧力制御弁32aが設けられており、熱交換器12へと供給する液体窒素の圧力を制御できるようになっている。
気液分離タンク26の下方と液体窒素吐出配管32の途中位置との間には、液体窒素バイパス配管34が設けられている。この液体窒素バイパス配管34によって、一部の液体窒素を気液分離タンク26へと戻すことができるようになっている。
以上の通り、二次冷媒である窒素の循環流路24は、主として、搬送ポンプ22、液体窒素吐出配管32、熱交換器12、窒素ガス戻り配管36、気液分離タンク26によって構成されている。
窒素ガス保存タンク53の上流側には、モータ54aによって回転駆動される圧縮機54が設けられている。圧縮機54としては、スクリュー式が好適に用いられる。この圧縮機54にて昇圧された窒素ガスは、窒素ガス吐出配管55を通過し、分岐点55aにて、第1窒素ガス供給配管13及び第2窒素ガス供給配管57へと導かれる。
第1窒素ガス供給配管13を介して導かれた窒素ガスは、上述したように、予冷熱交換器14にてBOGによって予冷された後に、熱交換器12の直近に位置する窒素ガス戻り配管36上流側に合流するようになっている。
第2窒素ガス供給配管57を介して導かれた窒素ガスは、戻りガス予冷熱交換器38の上流側の直近に位置するガス戻り配管36下流側に合流するようになっている。
気液分離タンク26にて貯留された液体窒素は、搬送ポンプ22によって、同タンク26の下端から液体窒素流出配管30を介して取り出され、液体窒素吐出配管32を介して熱交換器12へと導かれる。熱交換器12へと導く液体窒素の圧力は、圧力制御弁32aによって調整される。
熱交換器12へと導かれた液体窒素は、バイパスライン9へと導かれたBOGと熱交換する。すなわち、熱交換器12にて液体窒素はBOGへ蒸発潜熱を与え、蒸発気化する。一方、BOGは、液体窒素の蒸発潜熱によって冷却され、凝縮液化する。凝縮液化したBOGは、再液化されたLNGとして、LNG返送配管16を介して各カーゴタンク3へと返送される。
図示しない窒素ガス発生装置から導かれた窒素は、窒素ガスドライヤ51にて水分及び炭酸ガスが除去された後に、窒素ガス保存タンク53へと導かれる。モータ54aによって駆動される圧縮機54にて昇圧され、窒素ガス保存タンク53から導かれた窒素ガスは、分岐点55aにて、第1窒素ガス供給配管13及び第2窒素ガス供給配管57へと導かれる。
第1窒素ガス供給配管13へと導かれた窒素ガスは、予冷熱交換器14にてBOGの顕熱によって予冷され、窒素ガス戻り配管36へと導かれる。予冷熱交換器14にて冷熱を与えた後のBOGは、図示しない燃焼手段によって燃焼処理された後に、大気へと放出される。なお、このようにBOGの一部を焼却処理するのは、カーゴタンク3内に滞留して濃縮される窒素分を排出するためである。
第2窒素ガス供給配管57へと導かれた窒素ガスは、窒素ガス戻り配管36の下流側に合流した後に、戻りガス予冷熱交換器38によって冷却される。
BOGを凝縮液化する熱交換器12をカーゴタンク3の近傍に設けることとしたので、カーゴタンク3にて発生したBOGをカーゴタンク3の近傍にて液化することができる。したがって、カーゴタンク3から離れた遠隔部に設置された冷却装置までBOGを導くための配管等の系統を可及的に排除することができる。これにより、BOGを冷却装置まで輸送する間にBOGが侵入熱によって温度上昇してしまうことを避けることができ、BOGを液化するための冷却動力を低減することができる。また、カーゴタンク3の近傍にて再液化するので、再液化したLNGをカーゴタンク3へと返送する際にはLNG返送配管16のみで済み、冗長な配管等の系統を排除することができる。
また、第2窒素ガス供給配管57から導かれる常温の窒素ガスを戻りガス予冷熱交換器38によって予冷することとしたので、窒素ガスを冷却液化するための動力を低減することができる。
次に、本発明の第二実施形態について、図3を用いて説明する。
本実施形態は、第1実施形態のように冷凍機群20によって液体窒素を過冷却する強制循環方式に代えて、冷凍機群20によって窒素ガスを冷却して凝縮液化する自然循環凝縮方式とした点が大きく異なる。したがって、第1実施形態と共通する構成要素については同一の符号を付すとともにその説明を省略する。
気液分離タンク26にて貯留された液体窒素は、搬送ポンプ22によって、同タンク26の下端から液体窒素流出配管30を介して取り出され、液体窒素吐出配管32を介して熱交換器12へと導かれる。
熱交換器12へと導かれた液体窒素は、バイパスライン9へと導かれたBOGと熱交換する。すなわち、熱交換器12にて液体窒素はBOGへ蒸発潜熱を与え、蒸発気化する。一方、BOGは、液体窒素の蒸発潜熱によって冷却され、凝縮液化する。凝縮液化したBOGは、再液化されたLNGとして、LNG返送配管16を介して各カーゴタンク3へと返送される。
BOGを凝縮液化する熱交換器12をカーゴタンク3の近傍に設けることとしたので、カーゴタンク3にて発生したBOGをカーゴタンク3の近傍にて液化することができる。したがって、カーゴタンク3から離れた遠隔部に設置された冷却装置までBOGを導くための配管等の系統を可及的に排除することができる。これにより、BOGを冷却装置まで輸送する間にBOGが侵入熱によって温度上昇してしまうことを避けることができ、BOGを液化するための冷却動力を低減することができる。また、カーゴタンク3の近傍にて再液化するので、再液化したLNGをカーゴタンク3へと返送する際にはLNG返送配管16のみで済み、冗長な配管等の系統を排除することができる。
また、再液化するガスとしてLNGを一例として説明したが、本発明はこれに限定されるものではなく、LNGに代えて、LPG、アンモニア等に対しても適用できる。
また、二次冷媒として窒素を一例として説明したが、本発明はこれに限定されるものではなく、窒素に代えてアルゴン等の不活性ガスといった他のガスでもよい。
また、バイパスライン9内に熱交換器12を配置する構成としたが、本発明はこれに限定されるものではなく、例えば、図1の符号Aで示したように、ベイパーヘッダーライン7内に(好ましくは、各カーゴタンク3間に1つずつ)、熱交換器12を複数設けることとしてもよい。これにより、バイパスライン9をも省略することができ、より一層構成を簡便化することができる。もちろん、この構成は、図3に示した第2実施形態に対しても適用可能である。
また、熱交換器12を、バイパスライン9やベイパーヘッダーライン7内に挿入する構成を具体例として説明したが、これ以外の構成ももちろん可能である。例えば、カーゴタンク3またはカーゴタンク3の付属配管やフィッティングに液体窒素が流れる配管を巻き付けた構成としても良い。
また、二次冷媒の蒸発によってBOGの凝縮が行われるように二次冷媒の組成および/または圧力が設定可能とされていることが好ましい。これにより、熱交換手段へ循環させる二次冷媒の量を大幅に低減することができる。
また、カーゴタンク3内に設置された温度計、圧力計およびポンプ吐出流量計の少なくともいずれかの計測結果に基づいて、パルスチューブ冷凍機21の運転台数の制御、及び/又は、各パルスチューブ冷凍機21の冷凍能力の制御を行うようにされていることが好ましい。
Claims (11)
- 液化ガス貯蔵タンク内の液化ガスから気化したボイルオフガス(以下「BOG」という。)を再液化して前記液化ガス貯蔵タンクの内圧上昇を抑えるための液化ガス再液化装置において、
前記BOGの凝縮温度よりも融点が低い液体である二次冷媒が循環する二次冷媒循環流路に設けられ、該二次冷媒を液化する冷却手段と、
該冷却手段によって冷却された液化二次冷媒を前記二次冷媒循環流路内で搬送する液化二次冷媒搬送手段と、
前記二次冷媒循環流路に設けられ、前記液化二次冷媒搬送手段によって搬送された液化二次冷媒と前記BOGとを熱交換させて該BOGを凝縮液化させる熱交換手段と、を備え、
該熱交換手段は、前記液化ガス貯蔵タンクの近傍に設けられていることを特徴とする液化ガス再液化装置。 - 前記熱交換手段は、前記液化ガス貯蔵タンクの上方に設けられていることを特徴とする請求項1に記載の液化ガス再液化装置。
- 前記熱交換手段は、複数の前記液化ガス貯蔵タンクの上方に設けられたヘッダ配管内に設けられていることを特徴とする請求項2に記載の液化ガス再液化装置。
- 前記二次冷媒循環流路に供給される二次冷媒を、前記BOGによって予冷する予冷手段が設けられていることを特徴とする請求項1から3のいずれかに記載の液化ガス再液化装置。
- 液化二次冷媒搬送手段は、搬送する液化二次冷媒の流量を変更可能とされていることを特徴とする請求項1から4のいずれかに記載の液化ガス再液化装置。
- 前記冷却手段は、複数のパルスチューブ冷凍機を備えていることを特徴とする請求項1から5のいずれかに記載の液化ガス再液化装置。
- 前記液化ガス貯蔵タンク内に設置された温度計、圧力計およびポンプ吐出流量計の少なくともいずれかの計測結果に基づいて、前記パルスチューブ冷凍機の運転台数の制御、及び/又は、各前記パルスチューブ冷凍機の冷凍能力の制御を行うことを特徴とする請求項6に記載の液化ガス再液化装置。
- 二次冷媒の蒸発によってBOGの凝縮が行われるように二次冷媒の組成および/または圧力が設定可能とされていることを特徴とする請求項1に記載の液化ガス再液化装置。
- 液化ガス貯蔵タンクと、
該液化ガス貯蔵タンク内の液化ガスから気化したBOGを再液化する請求項1から6のいずれかに記載された液化ガス再液化装置と、
を備えていることを特徴とする液化ガス貯蔵設備。 - 液化ガス貯蔵タンクと、
該液化ガス貯蔵タンク内の液化ガスから気化したBOGを再液化する請求項1から6のいずれかに記載された液化ガス再液化装置と、
を備えていることを特徴とする液化ガス運搬船。 - 液化ガス貯蔵タンク内の液化ガスから気化したBOGを再液化する液化ガス再液化方法において、
BOGの凝縮温度よりも融点が低い液体である二次冷媒が循環する二次冷媒循環流路に設けられ、該二次冷媒を液化する冷却手段と、
該冷却手段によって冷却された液化二次冷媒を前記二次冷媒循環流路内で搬送する液化二次冷媒搬送手段と、
前記二次冷媒循環流路に設けられ、前記液化二次冷媒搬送手段によって搬送された液化二次冷媒と前記BOGとを熱交換させて該BOGを凝縮液化させる熱交換手段と、を備え、
該熱交換手段による熱交換が、前記液化ガス貯蔵タンクの近傍にて行われることを特徴とする液化ガス再液化方法。
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US12/670,693 US8739569B2 (en) | 2008-02-27 | 2009-02-26 | Liquefied gas reliquefier, liquefied-gas storage facility and liquefied-gas transport ship including the same, and liquefied-gas reliquefaction method |
EP09715741.6A EP2196722B1 (en) | 2008-02-27 | 2009-02-26 | Device for re-liquefaction of liquefied gas, liquefied gas storage facility and liquefied gas carrying vessel equipped with the device, and method of re-liquefaction of liquefied gas |
KR1020107002140A KR101136709B1 (ko) | 2008-02-27 | 2009-02-26 | 액화 가스 재액화 장치, 이것을 구비한 액화 가스 저장 설비 및 액화 가스 운반선 및 액화 가스 재액화 방법 |
CN2009800005799A CN101796343B (zh) | 2008-02-27 | 2009-02-26 | 液化气再液化装置、具有该装置的液化气贮藏设备及液化气运输船、以及液化气再液化方法 |
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Also Published As
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KR20100043199A (ko) | 2010-04-28 |
US20100170297A1 (en) | 2010-07-08 |
EP2196722A1 (en) | 2010-06-16 |
US8739569B2 (en) | 2014-06-03 |
JP2009204080A (ja) | 2009-09-10 |
CN101796343B (zh) | 2012-07-11 |
EP2196722A4 (en) | 2017-10-18 |
JP5148319B2 (ja) | 2013-02-20 |
KR101136709B1 (ko) | 2012-04-19 |
EP2196722B1 (en) | 2021-04-14 |
CN101796343A (zh) | 2010-08-04 |
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