CN103608632B - Utilize the LNG being used for fuel with the system and method for the LPG boil-off gas that liquefies - Google Patents

Utilize the LNG being used for fuel with the system and method for the LPG boil-off gas that liquefies Download PDF

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Publication number
CN103608632B
CN103608632B CN201280026200.3A CN201280026200A CN103608632B CN 103608632 B CN103608632 B CN 103608632B CN 201280026200 A CN201280026200 A CN 201280026200A CN 103608632 B CN103608632 B CN 103608632B
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Prior art keywords
lng
vaporizer
bog
lpg
tank
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CN201280026200.3A
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CN103608632A (en
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卡尔·约根·鲁梅尔霍夫
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Wartsila Oil and Gas Systems AS
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Hamworthy Oil and Gas Systems AS
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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
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C1/00—Pressure vessels, e.g. gas cylinder, gas tank, replaceable cartridge
    • 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"
    • F25J1/0045—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 vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • 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
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    • 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
    • F25J1/0224—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 internal quasi-closed 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
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2201/00—Vessel construction, in particular geometry, arrangement or size
    • F17C2201/05—Size
    • F17C2201/052—Size large (>1000 m3)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2205/00—Vessel construction, in particular mounting arrangements, attachments or identifications means
    • F17C2205/03—Fluid connections, filters, valves, closure means or other attachments
    • F17C2205/0302—Fittings, valves, filters, or components in connection with the gas storage device
    • F17C2205/0323—Valves
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    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
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    • F17C2221/035—Propane butane, e.g. LPG, GPL
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    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
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    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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    • F17C2225/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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    • F17C2225/0169—Liquefied gas, e.g. LPG, GPL subcooled
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2260/00—Purposes of gas storage and gas handling
    • F17C2260/02—Improving properties related to fluid or fluid transfer
    • F17C2260/021—Avoiding over pressurising
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2260/00—Purposes of gas storage and gas handling
    • F17C2260/03—Dealing with losses
    • F17C2260/031—Dealing with losses due to heat transfer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • F17C2265/034—Treating the boil-off by recovery with cooling with condensing the gas phase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • F17C2265/035—Treating the boil-off by recovery with cooling with subcooling the liquid phase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/0105—Ships
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • 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
    • F25J2215/66—Butane or mixed butanes
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

Abstract

The present invention relates to the method and system for LPG boil-off gas (BOG) that liquefy, described system comprises LNG fuel system and LPG cargo system, wherein said LNG fuel system comprises at least one LNG fuel tank 23, LNG burning line 5 and the 2nd LNG burning line 13, and wherein said LPG cargo system comprises at least one LPG cargo tank 20, BOG pipeline 1, at least one liquefaction unit 100 and condensate line 3 again; Wherein said system also comprises: be provided at least one vaporizer 15,22 on the LNG burning line 5 between LNG fuel tank 23 and the 2nd LNG burning line 13, at least one vaporizer 15,22 wherein said and described LPG cargo system carry out heat exchange.

Description

Utilize the LNG being used for fuel with the system and method for the LPG boil-off gas that liquefies
Technical field
The present invention relates to for utilizing LNG for fuel with the system and method for LPG boil-off gas (boiloff) that liquefy.
Background technology
current techniques
KR20100102872 disclose be used in complicated ship or Floating Production storage unload a ship on while receive the method for LPG and LNG stream.The invention that KR20100102872 describes solves and how to utilize the low temperature of LNG boil-off gas to carry out condensation LPG boil-off gas to reduce the complexity of LPG liquefaction system again before compression and liquefaction.
KR20100102872 contrary to the present invention uses the sensible heat of LNG boil-off gas with condensation LPG boil-off gas, and described the present invention and LNG fuel gas system combinationally use the latent heat of LNG and the combination of sensible heat with condensation LPG boil-off gas.
US5860294 describes for the method for condensation from the gaseous hydrocarbon (particularly as find in the holding vessel of LPG/LEG ship (LEG=liquefied ethylene gas)) of the mixture of inert gas and gaseous hydrocarbon.
US5860294 first describes the again liquefaction system identical with the liquefaction unit again 100 in the present invention, but it has downstream second condenser system, and object is recovered in the gaseous hydrocarbon in normal goods condenser in uncondensable admixture of gas.
In order to make the second condenser in US5860294 play a role, main goods condenser must run and must take part of the condensate in this interchanger.
In the present invention, the second condenser (22) is positioned at the upstream of goods liquefaction system again, and it does not rely on the operation of main goods condenser.
KR20010077227 describes the method for the LNG boil-off gas that liquefies again, and described LNG boil-off gas outputs to such as national Distribution of Natural network after being liquefied by means of the part LNG stream being transported to vaporizer wherein.With LNG export pipeline, vapor gas condensate is mixed.Condensate is not had to turn back in holding vessel.
Liquid LNG here for controlling the pressure of LNG storage tank before making the LNG of combination and condensate flow vaporization to the heat exchange/absorption in LNG by boil-off gas.
Similar with KR20010077227 in EP1990272 principle, but condensate turns back in holding vessel, and vaporized product is transferred into gas engine as fuel.
US3306660 describes the method and system for storing multicomponent cryogen, captures larger volatile component that natural evaporation is fallen wherein, makes its condensation and leads back in holding vessel again.The cryogenic liquid pumped out is for condensation evaporation gas.
WO2011062505 describes the technique of the boil-off gas retrieved from LNG storage tank, and LNG is transported to the drainer again absorbing LNG boil-off gas wherein wherein.
US2795937 describes for storing the technology and equipment with carrying liquefied gases, and a tank holds liquefied natural gas (LNG) wherein, and a tank holds the liquid of higher.LNG is used as the fuel on ship, and it was vaporized by heat exchange in the tank liquid of higher liquid and is heated before entering combustion engine.US2795937 teaches this heat exchange and prevents any boil-off gas from liquid surface, so there is no description and evaporates liquefaction system again.
US3864918 describes the boil-off gas of catching from LNG product tank wherein and is divided into the method for two component streams.First-classly to be compressed, cool and liquefy.Second is used as the fuel driving ship.
US2006/0053806 describes for supplying boil-off gas as fuel and the system of Stress control product tank on LNG cargo ship peculiar to vessel.
Summary of the invention
The shipowner of existing transport LPG (liquefied petroleum gas) will use slow speed diesel engine to be used for promoting mainly into and use polytype bunker fuel oil to come for engine supply fuel.But new environment restriction (being now called emission control district) limits the release to environment of sulphur, nitrogen oxide and particle.In the future, also expect strict Global emissions restriction.One's own profession is proposed several selections meeting new demand, such as waste gas purification.Alternatively use clean poor (lean) combustion fuel, as methane.For being the large fuel consumption of shipping industry feature and high tradding limit demand, methane must store in its most effective mode (being namely called the liquid condition of LNG (liquefied natural gas)).
LNG fuel system is generally known in this area, and title is disclose a kind of example system in No. 20093272nd, the Norwegian patent applications of " ALNGfueltanksystemforatleastonegasengineusedforshippropu lsion ".
LPG carrying ship has as many as four product tank usually, and wherein said product tank has common vapor atmosphere when the goods of delivery one type.Structure LPG carrying ship makes them can deliver two kinds of different goods simultaneously.This means that the pipe-line system on deck is paired, so that the isolation of two cargo systems can be completed.LPG carrying ship can such as be mounted with propane and be mounted with butane in the 4th product tank in three tanks.Three tanks being mounted with propane have the vapor space communicated, but completely isolated with butane vapor space.Each deck pipe system is connected with multiple liquefaction unit again, ensure that product tank pressure is no more than maximum allowable pressure.Boil-off gas is compressed to enough pressure by liquefaction unit again, can rely on seawater condensing to make gas.Condensate turns back to product tank.In this fashion, product tank pressure is made to remain lower.For fully loaded under maximum environmental temperature condition and the VLGC of navigation, (huge gas carrier, cargo capacity is generally about 82.000m 3), the fuel oil consumption (to generator) of liquefaction boil-off gas is about 1900kg/ days.The solution also not avoiding this fuel oil to consume now.In addition, due to the LNG fact of about 50% less of the density of marine diesel oil, so LNG will need the reservoir volume of twice to maintain the energy of identical amount.Importantly, the fuel storage volume of increase with shipment ability for cost.Another problem relates to transports LPG in such as basin, the North Sea, and here hours underway is short, thus the layover time is total round trip duration significant contribution person, and it is very important for therefore reducing the layover time.
Another operation cost problem is the service and repair of refrigeration compressor, and it is because any slewing all has the service intervals based on running time.Newly-built ship has the interval that lies up of 5 years usually, and meanwhile, refrigeration compressor has the service intervals of about 20000 hours.Therefore, think navigate by water time need service.Therefore, advantageously reduce total run time, thus time extended between service and preferably having and service intervals that the interval that lies up is mated.
Therefore, an object of the present invention is to provide for utilizing LNG for fuel with the system and method for LPG boil-off gas (BOG) that liquefy, its manage to overcome the above problems at least one.
In order to deal with above problem, the invention discloses the system for LPG boil-off gas (BOG) that liquefy, described system comprises LNG fuel system and LPG cargo system, and wherein said LNG fuel system comprises at least one LNG fuel tank 23, LNG burning line 5 and the 2nd LNG burning line 13; Wherein said LPG cargo system comprises at least one LPG cargo tank 20, BOG pipeline 1, at least one liquefaction unit 100 and condensate line 3 again; Wherein said system also comprises: be provided at least one vaporizer 15,22 on the LNG burning line 5 between LNG fuel tank 23 and the 2nd LNG burning line 13, wherein at least one vaporizer 15,22 and LPG cargo system carry out heat exchange.
The invention also discloses the method for LPG boil-off gas (BOG) that to liquefy in the system comprising LNG fuel system and LPG cargo system, wherein said LNG fuel system comprises at least one LNG fuel tank 23, a LNG burning line 5 and the 2nd LNG burning line 13, and wherein said LPG cargo system comprises at least one LPG cargo tank 20, BOG pipeline 1, at least one liquefaction unit 100 and condensate line 3 again; Wherein said method comprises: provide at least one vaporizer 22,15 on the LNG burning line that is positioned between LNG fuel tank and the 2nd LNG burning line 13; By making stream from the LNG vaporization and condensation BOG of LNG fuel tank; And the BOG of condensation is transported to LPG cargo tank with fixed course.Usually, correspond to can the number of simultaneously freight for the number of vaporizer 22,15.These normally two.
Accompanying drawing explanation
With reference to accompanying drawing, other favourable embodiments of the present invention should be understood by dependent patent claims and detailed description hereinafter, wherein:
Fig. 1 is the general introduction figure of the liquefaction unit again of current techniques;
Fig. 2 is the general introduction figure of an embodiment according to system of the present invention;
Fig. 3 is the general introduction figure of another embodiment according to system of the present invention;
Detailed description of the invention
LPG is interpreted as a series of different cultivars or the product of the oil gas storing as liquid goods and transport.In multiple oil gas, propane and butane are main examples; Propane generally includes the ethane of any concentration of 0 volume % to 5 volume %; Butane content in propane is any concentration of 0 volume % to 20 volume %.This mixture formed primarily of propane (being generally 70 volume % to 98 volume %) is called commercial propane, and hereinafter referred to propane.
Butane can be any mixture of the possible fraction of normal butane and iso-butane and unsaturated hydrocarbons, and hereinafter referred to as butane.
Except propane and butane, LPG minimumly should comprise following kind:
Ammonia,
Butadiene,
Butane-propane mixture (any mixture),
Butylene,
Ether,
Propylene,
Vinyl chloride.
The LPG stored at a temperature below ambient and transport is a certain amount of steam of sustained release naturally.The normal method maintaining pressure in product tank extracts this steam, and it is also turned back to product tank with condensate by liquefaction.Liquefaction unit is interpreted as liquefying the refrigeration unit of described steam hereinafter again, and prefix " again " indicates the steam of liquefaction from liquid gas.
LPG to be greater than under atmospheric pressure at a temperature below ambient or its combination transport in liquid form.The present invention relates to the LPG carrying ship of conveying liquified goods LPG at a temperature below ambient, be called full refrigeration-type LPG carrying ship; Be greater than atmospheric pressure and lower than the temperature of environment under the LPG carrying ship of conveying liquified goods LPG.The latter is called half refrigeration-type/half adding pressure type.
Cargo type is any one in above-mentioned LPG kind or product.
Condensate is interpreted as the boil-off gas that liquefies, and wherein boil-off gas is the steam owing to giving off from goods in constant heat leakage to product tank.
Warm goods is the LPG loaded at the temperature higher than LPG saturation temperature under current cargo pressure tank.
Fig. 1 shows the typical current techniques be connected with at least one product tank 20, and liquefaction unit 100 is for reference again.Not shown Container Loading pipeline.Boil-off gas from product tank 20 flow to goods compressor 40 via boil-off gas pipeline 1, the first order of this goods compressor normally compound compressor, wherein by steam compressed to middle pressure.Do not flow to operating unit in parallel by the steam of any amount of the process of liquefaction unit again shown in Fig. 1 via boil-off gas pipeline 51, not shown.
Entering from goods compressor 40 via pipeline 46 boil-off gas out makes boil-off gas close to the economizer (economizer) 43 of its saturation temperature wherein.Then boil-off gas flow to goods compressor 41 via pipeline 47 from economizer 43, and wherein boil-off gas is compressed into the bubble point pressure corresponding to obtaining temperature in goods condenser 42.The second level of goods compressor 41 normally compound compressor.Need the compression stage more than two once in a while, and they are connected with 41 usually.
Then compressed boil-off gas enters goods condenser 42 to rely on seawater or any cooling medium condensation usually above ocean temperature via pipeline 48.Seawater is heat dump (heatsink) the most frequently used for goods condenser 42 up to now, but the mixture of water and low-temperature receiver is also fine.Low-temperature receiver can be the glycol of any appropriate.
Warm condensate (the condensation evaporation gas from goods condenser 42 obtained) leaves goods condenser 42, flow to economizer 43 via pipeline 49.Pipeline 50 is by pipeline 49 branch, and its small portion flows through fluid level control valve 44, and the major part for warm condensate provides the cascade EDFA of needs and excessively cold.Usually, liquid receiver is arranged on pipeline 49, not shown.The warm condensate of residue to one or more product tank 20 to be returned flows through the coil pipe 52 inside economizer 43 by the place of 50 branches and leaves coil pipe 52 with supercooled state.Excessively cold condensate flow back into product tank via pipeline 3 now.Condensate is produced valve 45 and is regulated the amount turning back to the condensate flow of one or more product tank 20.Condensate from the liquefaction unit again of other parallel runnings is connected in pipeline 3, not shown.
Fig. 2 illustrates two system LNG fuel gas supply system (on dotted line) that is different, that separate and LPG cargo systems up to now.LNG fuel gas supply system is configured with one or more LNG fuel tank 23 connected.Fuel gas supply system is also configured with the valve 27 that controlled pressure increases the amount of LNG to be vaporized in heat exchanger 24, to guarantee in fuel tank 23 constant vapour pressure more or less, thus guarantees fuel gas supply pressure enough in burning line 5.According to known principle, make LNG be supplied to vaporizer 25, wherein make LNG vaporize and gained steam flow to superheater 26, steam is heated to preferred fuel gas temperature wherein, is then transferred to sustainer via pipeline 13.Fig. 2 also illustrates vapor line 8 and valve 28, if need the pressure in fuel tank 23 to reduce, then the LNG of evaporation is transported to superheater 26 by its permission.But, in most of the cases, in vapor line 8, there is no air-flow.
Engine fuel gas injection pressure depends on that it is Otto (Otto) engine or Diesel engine, and Otto engine only needs the medium gas injection pressure of 4 bar, and Diesel engine needs the fuel gas injection pressure of 300 to 350 bar.Except high pressure replacement scheme needs the dedicated pump for boost in pressure, this significant difference of pressure has limited impact to the present invention.Not shown other pumping system, because it is generally known for those skilled in the art.
For the Diesel engine needing higher fuel gas pressure, as mentioned above, need the other LNG petrolift be connected with burning line 5 LNG pressure is promoted to required pressure before entering vaporizer 25.In this embodiment, vapor line 8 is sent to home or is alternatively sent to and uses user, does not in most of the cases have air-flow in vapor line 8.
As above with reference to disclosed in Fig. 1, the LPG cargo system configuration of Fig. 2 has liquefaction unit 100 and at least one LPG cargo tank 20 again, makes boil-off gas flow to the BOG pipeline 1 of liquefaction unit 100 again and make condensate turn back to the condensate line 3 of product tank 20 via valve 45.
Consider normal/cruise, the typical VLGC (huge gas carrier) under the maximum environmental temperature condition of delivery propane is about 425kW to the heat leakage in goods can system.The LPG evaporation rate average out to of gained about 3300 to 3800kg/ hour.In addition, the propelling power supply that the upper typical case of VLGC installs is 14MW, and the typical energy consumption under maximum continuous rating is 7500kJ/kWh, and the LNG amount needed under this condition is about 2120kg/ hour.Therefore, put into practice aspect for all, the cooling potential of LNG eliminates needs load term of voyage being run again to liquefaction unit, in particular for lower than design maximum environment temperature and/or maximum continue specified under the needs of speed.In fact, under these conditions, Operation for liquefaction again can be got rid of completely.
Therefore, according to of the present invention for utilizing LNG for fuel with the system of the LPG boil-off gas that liquefies, comprise at least one vaporizer 15,22 on the LNG burning line 5 that is provided between LNG fuel tank 23 and the 2nd LNG burning line 13, at least one vaporizer 15,22 wherein said and LPG cargo system carry out heat exchange, effectively LNG fuel system are incorporated in LPG evaporated gas system.
Being arranged on the special air blast be directly supplied on the boil-off gas line of vaporizer 22 is obvious selection, but when being provided with goods compressor with other equipment for cost.Therefore, this solution may not be preferred, so not shown.Or steam is also fine to flowing freely of vaporizer 22, but, loopback pump (returnpump) should be considered for this combination.
According to the first embodiment of the invention, at least one vaporizer 22 is BOG condenser, and it is adapted to pass through and makes the LNG vaporization of being flowed out from fuel tank 23 via pipeline 5 by pressure carry out condensation BOG.Condensate sends back product tank 20 via pipeline 2.See conversely, LNG relies on boil-off gas to be vaporized, and according to evaporation and the amount of fuel consumption, LNG can be partially vaporized, vaporization or to vaporize completely and overheated completely.Products therefrom leaves 22, enters the vaporizer 25 making any remaining LNG vaporization.Steam from vaporizer 25 flows to the superheater 26 that steam is heated to preferred fuel gas temperature.When the steam that LNG evaporation and the amount of fuel consumption make to leave at least one vaporizer 22 is overheated, both vaporizer 25 and superheater can be omitted.When LNG evaporation and the amount of fuel consumption make the steam leaving at least one vaporizer 22 be completely vaporised, vaporizer 25 can be omitted.
In the above-described embodiment, all LNG flowed out from fuel tank 23 pass through vaporizer 22.But under certain situation (such as, do not have enough gas evaporations or do not have boil-off gas), it may be favourable for controlling by the stream of the LNG of vaporizer.According to one embodiment of the invention, respectively at vaporizer 22 above and arrange two valves 29,30 in parallel with it, make when not having BOG in BOG pipeline 1, valve 29 is opened and valve 30 cuts out, and vice versa.The amount of the LNG flowing to vaporizer 22,15 is adjusted to the amount of available BOG and the current LNG consumption existed in BOG pipeline 1 by valve 29,30.This embodiment ensure that the products therefrom leaving vaporizer 22,15 is completely vaporised, and makes vapor transfer to steam be heated to the superheater 26 of preferred fuel gas temperature.Regulated by known principle, not shown.Make unwanted any excessive LNG in vaporizer 22,15 directly be transferred to vaporizer 25, after excessive LNG is vaporized, be transferred to superheater 26 here.Valve 29,30 can substitute with three tunnels are logical equally well, not shown.Therefore, valve arranges that 29,30 representatives provide any alternative valve of same functionality to arrange.
Around the goods compressor 40,41 liquefied again in Unit 100, arrange that pipe-line system makes it run in single stage compress mode.Arrange that goods compressor 40,41 be apparent and proposed is for those skilled in the art one of several possible solution in single stage compress mode.In single stage compress mode, capacity is higher and usually only need operation compressor, therefore makes total compressor totally to reduce running time.Then, the boil-off gas from LPG cargo tank 20 is flowed directly to goods compressor 40,41 in pipeline 1, makes the moderate pressure of boil-off gas promote in described goods compressor.Pipeline 48 or 49 facilitates position, and boil-off gas is via pipeline 61 branch and flow to vaporizer 22, makes boil-off gas condensation and turn back to product tank 20 via pipeline 2 in described vaporizer.Valve 71 and 72 regulates the position should carrying out boil-off gas branch.
In yet another embodiment of the present invention, at least one vaporizer 15 is condensate subcooler (subcooler), it is provided in the condensate line 3 between liquefaction unit 100 and product tank 20 again, and condensate subcooler 15 is adapted to pass through and makes the LNG vaporization from fuel tank 23 make LPG condensate excessively cold.With reference to BOG condenser 22, can be used alone in embodiment described above condensate subcooler.
In a preferred embodiment of the invention, as following more in detail disclosed in, both vaporizer 15 and vaporizer 22 are provided, add operating flexibility and when applicable to the utilization of refrigerant charge excessive in LNG.In this embodiment, provide valve 16 and 17 can to get around or by vaporizer 15.
According to an exemplary of the present invention, the boil-off gas of discharging from LPG cargo tank 20 is flowed directly to goods compressor 40,41 in pipeline 1, makes the moderate pressure of boil-off gas promote in described goods compressor.Around the goods compressor 40,41 liquefied again in Unit 100, arrange that pipe-line system makes it run in single stage compress mode.The boil-off gas through moderate compression from goods compressor 40,41 flow to vaporizer 22 via pipeline 2, makes boil-off gas condensation and turn back to product tank 20 in described vaporizer.
In vaporizer 22, BOG is condensed by making to flow the LNG vaporization from fuel tank 23 by pressure via pipeline 5.Product tank 20 is transmitted back to via pipeline 2 through the BOG of condensation.See conversely, LNG rely on boil-off gas be vaporized, according to exist evaporation and universal fuel consume amount, LNG can be partially vaporized, completely vaporization or completely vaporization and overheated.Products therefrom leaves vaporizer 22 and enters vaporizer 25, makes any remaining LNG vaporization in described vaporizer.Steam from vaporizer 25 is transferred to superheater (superheater) 26 via pipeline 12, makes steam heated to preferred fuel gas temperature in described superheater.When the steam that LNG evaporation and the amount of fuel consumption make to leave at least one vaporizer 22 is overheated, both vaporizer 25 and superheater can be omitted.When the amount of LNG boil-off gas and fuel consumption makes the steam leaving at least one vaporizer 22 be completely vaporised, vaporizer 25 can be omitted.
In the above-described embodiment, flow from all LNG of fuel tank 23 by vaporizer 22.But under certain situation (such as, do not have enough gas evaporations or do not have boil-off gas), it may be favourable for controlling by the stream of the LNG of vaporizer.According to one embodiment of the invention, respectively at vaporizer 22 above and provide two valves 29,30 in parallel with it, the valve 29 when not having BOG in BOG pipeline 1 is opened and valve 30 cuts out, vice versa.The amount of the LNG flowing to vaporizer 22,15 is also adjusted to the amount of available BOG and the current LNG consumption existed in BOG pipeline 1 by two valves 29,30.The LNG flowing to vaporizer 22,15 is completely vaporised, and vapor transfer is to superheater 26, and in described superheater, steam is heated to preferred fuel gas temperature.Make unwanted any excessive LNG in vaporizer 22,15 directly be transferred to vaporizer 25, after LNG excessive in described vaporizer is vaporized, be transferred to superheater 26.Two valves 29,30 can replace with providing any three tunnel unifiers of same functionality.
Exemplary disclosed is above chiefly directed to the use of load term of voyage system when LNG fuel consumption is higher.But at loading days, boil-off gas speed is its maximum, LNG fuel consumption is low side, and therefore, the amount of the LNG of the BOG that can be used for liquefying is limited.Therefore, liquefaction unit 100 again must be put into operation.
Under these conditions, nature should consider to utilize in as 22 of liquefaction unit forecooler best loading days can the LNG of reduction.But, due to such as in the smog problem of suction port of compressor place (particularly when loading more warm goods), so this is not best solution.
Replace making boil-off gas precooling, the excessively cold flash gas decreased in product tank 20 of condensate is generated, therefore adds systematic function by flash gas recirculation need not be made to get back to goods compressor.
At loading days, all boil-off gas are directly transported to via pipeline 1, make boil-off gas condensation and return liquefaction unit again via pipeline 3 in described liquefaction unit again.Condensate subcooler 15 is positioned on line 3, uses LNG as cooling agent.It is made to turn back to product tank after the temperature of condensate being reduced to preferably be not less than-50 DEG C.Condensate temperature depends on the type of goods, for more warm cargo type its can be higher.
As previously mentioned, structure LPG cargo ship makes them can deliver two kinds of different goods simultaneously, and described two kinds of goods can be propane and butane.Then making vaporizer 22,15 run with series sequence makes first LNG at least one vaporizer 22, rely on propane vaporization, and the LNG then vaporized flow to the pipeline 80 on the parallel units running butane via pipeline 74.The vaporization LNG that gained is more warm turns back to fuel gas system via pipeline 5.Fig. 3 shows such layout, based on its can make one of system canned be loaded with butane and three be cannedly loaded with propane.Usually, four liquefaction unit 100 are again installed, but at term of voyage usual two be for subsequent use, particularly when LNG used according to the invention is as fuel.As can be seen from Figure, the parallel running of vaporizer 22 is also fine.The not shown liquefaction unit more for subsequent use of Fig. 3.
Although illustrate in detail in accompanying drawing and above description and describe the present invention, such illustrating and describe should be thought illustrative or exemplary, instead of restrictive, and is not intended to limit the invention to disclosed embodiment.The fact that only has of some feature quoted from inequality dependent claims does not show that the combination of these features can not be advantageously used.Reference numeral in claim should not be construed as restriction the present invention.

Claims (7)

1. the system for LPG boil-off gas (BOG) that liquefy, described system comprises LNG fuel system and LPG cargo system, wherein said LNG fuel system comprises at least one LNG fuel tank (23), LNG burning line (5) and the 2nd LNG burning line (13), at least one liquefaction unit (100) again that wherein said LPG cargo system comprises at least one LPG cargo tank (20), BOG pipeline (1) and is configured with condensate line (3);
It is characterized in that described system also comprises:
Be provided in the first vaporizer (15) on the described LNG burning line (5) between described LNG fuel tank (23) and described 2nd LNG burning line (13) and the second vaporizer (22), and be arranged at least one the 3rd vaporizer (25) in described first vaporizer (15) and the second vaporizer (22) downstream;
Described second vaporizer (22) above and first valve (29) in parallel with described second vaporizer (22) and the second valve (30), the amount of the LNG flowing through described second vaporizer (22) is made to be adjusted in the middle available BOG of existence of described BOG pipeline (1) and the amount of current LNG fuel consumption;
Wherein:
When described first valve (29) is closed and described second valve (30) is opened, described second vaporizer (22) is adapted to pass through the BOG condenser (22) with the heat exchange of described LPG cargo system, the LNG from described LNG fuel tank (23) being vaporized to carry out condensation BOG; Described system also comprises at least one liquefaction unit (100) again, the goods compressor (40,41) wherein arranged with single stage fashion is arranged in before described BOG condenser (22), be suitable for making stream fully to pressurize to get back to described product tank (20) as condensate transport from the BOG of described product tank (20), described 3rd vaporizer (25) process is not by excessive LNG that described condenser (22) is vaporized; And
When described first valve (29) is opened and described second valve (30) cuts out, described first vaporizer (15) is adapted to pass through the LNG from described fuel tank (23) to be vaporized the condensate subcooler (15) making LPG condensate excessively cold, in the described condensate line (3) described in described condensate subcooler (15) is positioned at again between liquefaction unit (100) and described product tank (20).
2. system according to claim 1, is wherein positioned with loopback pump after described BOG condenser, is suitable for the BOG of condensation to be transported to described product tank (20).
3. the method for LPG boil-off gas (BOG) that liquefies in the system comprising LNG fuel system and LPG cargo system, wherein said LNG fuel system comprises at least one LNG fuel tank (23), a LNG burning line (5) and the 2nd LNG burning line (13), at least one liquefaction unit (100) again that wherein said LPG cargo system comprises at least one LPG cargo tank (20), BOG pipeline (1) and is configured with condensate line (3);
It is characterized in that described method comprises:
-the first vaporizer (15) and the second vaporizer (22) are provided, it is positioned on the described LNG burning line (5) between described LNG fuel tank and described 2nd LNG burning line (13), and provides at least one the 3rd vaporizer (25) being arranged in described first vaporizer (15) and the second vaporizer (22) downstream;
-in BOG condenser by making stream carry out condensation BOG from the LNG of described LNG fuel tank vaporization, described second vaporizer (22) is described BOG condenser;
-arrange the goods compressor (40,41) of at least one liquefaction unit (100) more described, described goods compressor is arranged in before described BOG condenser with single stage fashion, wherein makes stream fully pressurize to transport back described product tank (20) as condensate from the BOG of described product tank (20); And
-BOG of condensation is transported to described LPG cargo tank.
4. method according to claim 3, described LNG stream wherein from described LNG fuel tank (23) is free stream, described method provides loopback pump after being also included in described BOG condenser, and the BOG of described condensation is pumped to described LPG cargo tank (20) by described loopback pump.
5. method according to claim 3, wherein makes the residue LNG received from described first vaporizer (15) and the second vaporizer (22) by least one the 3rd vaporizer (25) vaporization described; And
-provide at least one superheater (26) at least one the 3rd vaporizer (25) downstream described, wherein make the steam heated received from least one the 3rd vaporizer (25) described to preferred fuel gas temperature.
6. method according to claim 3, wherein said method also comprises:
-provide at least two product tank (20) for delivering the first and second different goods simultaneously,
-make first LNG at least one second vaporizer (22), rely on described first goods to be vaporized with series sequence described first vaporizer (15) of operation and the second vaporizer (22), then to flow to the pipeline (80) on the parallel units run on described second goods via pipeline (74) through the LNG of vaporization, and
-via pipeline (5), the LNG through vaporization warm for gained is transmitted back to described LNG fuel system.
7. method according to claim 6, wherein said first goods is propane and described second goods is butane.
CN201280026200.3A 2011-05-30 2012-05-30 Utilize the LNG being used for fuel with the system and method for the LPG boil-off gas that liquefies Active CN103608632B (en)

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