CN107208841A - Cool down the method and device for the method for boil-off gas - Google Patents

Cool down the method and device for the method for boil-off gas Download PDF

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Publication number
CN107208841A
CN107208841A CN201580050405.9A CN201580050405A CN107208841A CN 107208841 A CN107208841 A CN 107208841A CN 201580050405 A CN201580050405 A CN 201580050405A CN 107208841 A CN107208841 A CN 107208841A
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compression
bog
cooling
stream
streams
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CN201580050405.9A
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CN107208841B (en
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马丁·哈尔克罗
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LGE IP Management Co Ltd
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Babcock IP Management Number One Ltd
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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
    • F17C13/00—Details of vessels or of the filling or discharging of vessels
    • F17C13/004—Details of vessels or of the filling or discharging of vessels for large storage vessels not under pressure
    • 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
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J1/0203—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—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
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • 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
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
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    • F17C2250/032—Control means using computers
    • 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
    • F17C2260/05—Improving chemical properties
    • F17C2260/056—Improving fluid characteristics
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    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/031—Treating the boil-off by discharge
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    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
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    • 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
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    • 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
    • F17C2265/037—Treating the boil-off by recovery with 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/038—Treating the boil-off by recovery with expanding
    • 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
    • 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
    • F17C2270/011—Barges
    • 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
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
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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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
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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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
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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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Ocean & Marine Engineering (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The method from the boil-off gas stream for floating the liquefied ethane goods in cargo ship is cooled down, methods described includes at least following steps：In two or more compression stages including at least first stage and terminal stage, the boil-off gas stream from the liquefied ethane goods is compressed to provide the BOG discharge streams of compression, the first stage wherein compressed, there is the first stage to discharge pressure, and the terminal stage compressed has terminal stage suction pressure, and the BOG streams of one or more of middle, optionally cooling down, compressions are provided between the successive stages of compression；The BOG discharge streams of compression are cooled down by one or more of first coolant flows, are flowed with providing the BOG of compression of the first cooling；The BOG streams of the compression of the first cooling are cooled down by least one second coolant flow, are flowed with providing the BOG of compression of the second cooling；The BOG streams of the compression of the second cooling are cooled down by the 3rd coolant flow, are flowed with providing the BOG of compression of the 3rd cooling；A part for the BOG streams of the compression of the 3rd cooling is expanded into the pressure discharged in the first stage between pressure and the pressure of terminal stage suction pressure, flowed with providing the BOG of cooling of the first expansion；BOG using the cooling of the first expansion is flowed as the 3rd coolant flow, is flowed with providing the BOG of heating of the first expansion；Flowed with the BOG for the heating for using the first expansion as second coolant flow or the second coolant flow.

Description

Cool down the method and device for the method for boil-off gas
It is especially re-liquefied the present invention relates to for cooling down, the steaming of the liquefied ethane goods come on comfortable floating cargo ship Get angry body (boil off gas) (BOG) method, and device for the method.
Cargo ship is floated, such as liquefied gas carrier and barge can transport the various goods in liquefaction.Above and below sheet Wen Zhong, liquefaction goods is completely or substantially ethane, is usually>90% ethane or>95% or>96% or>97% or> 98% or>99% ethane.Ethane is the useful products source for various industrial process.
Ethane can be extracted from natural gas production, hydraulic fracturing (fracking), or be produced in crude oil refining.Cause This, ethane can be with various other components, especially methane combination.It it is generally desirable at its source or close to the liquefaction at its source Liquefied ethane in facility, because as liquid, it can more easily be stored with long-distance transportation (usually more than than gas form Normal pipeline distance) because it occupies less volume and need not can stored under high pressure.
When measuring at 1 atmosphere pressure, the long-distance transportation of the liquefied ethane goods with about -87 DEG C of boiling points can be Carried out in suitable liquefied gas carrier, such as with one or more storage tanks to preserve the ocean tanker of liquefied ethane goods.This A little storage tanks can be heat-insulated and/or pressurized canister., may be due to goods during the storage of the loading and liquefied ethane goods of tank Evaporate and produce gas.The goods gas of this evaporation is referred to as boil-off gas (BOG).In order to prevent the BOG in tank accumulate (with And consequential accumulation of pressure problem), system can be aboard ship provided with re-liquefied BOG so that it can be with condensing state (condensed state) returns to storage tank.This can be realized by compressing and cooling down BOG by low-temperature receiver.Ethane is 47.7 There is 32.18 DEG C of critical-temperature so that the seawater at similar temperature will be not suitable as mainly under the pressure of bar (barg) Low-temperature receiver.In many systems, the BOG of compression is cooled and condensed by secondary refrigerant.
In the case where common liquefaction goods can be defined as " pure ", then there is the known formula for re-liquefied BOG Method and device.However, in floating cargo ship the liquefied ethane that will be transported as goods can with and more and more Potentially include the concentration of the other components more than bottom line level (de minimus level).This is at least partially due to The increasing supply of " non-pure " ethane from new sources or new industrial process.
One of possible other components are propane.However, due to when at 1 atmosphere pressure measure when propane have about -40 DEG C boiling point, so the method and apparatus needed for re-liquefied ethane/propane BOG will inherently realize BOG any propane part It is re-liquefied.
The component of another possibility is nitrogen.Because when measuring at 1 atmosphere pressure, its boiling point is about -196 DEG C, because Any nitrogen that this is attempted in the re-liquefied BOG on floating cargo ship is typically unpractical.Therefore, nitrogen is generally recognized For be BOG those parts for being defined as " not condensable " at least key component, i.e. its a little can not (actually) exist It is condensed on floating cargo ship.However, nitrogen is the gas of relative " safety ".
Other main possible important components are methane in liquefied ethane goods.When measuring at 1 atmosphere pressure, Methane has about -162 DEG C to -163 DEG C of boiling point.When measuring at 1 atmosphere pressure, the boiling point is very significantly below ethane Boiling point.Similarly, methane is typically considered " not condensable " component of liquefaction goods so far, i.e., it may be condensed (i.e. It is re-liquefied), but especially special method is needed, methods described may not be that CAPEX and/or OPEX is closed on floating cargo ship Reason.Therefore, the relatively small amount in liquefaction goods (such as being completely or substantially those of propane (i.e. LPG) or the like) Methane be discharged to always in air up to now because conventional LPG BOG method of re-liquefaction and device can not be re-liquefied Methane.
However, methane is considered as one of " greenhouse gases " so that preferably do not discharge it in air increasingly.
In addition, it is presently contemplated that the ethane type transported more and more as liquefied ethane is expected in goods has The methane concentration of incrementss.
In addition, the special of methane has the disadvantage, the small concentration methane in liquefaction goods is also led in BOG not The methane of proportional amount.For example, only 0.5mol% concentration may cause the BOG of liquefied ethane goods to be in the liquid phase 25mol% methane.
Accordingly, it is possible to which all components of the impossible re-liquefied boil-off gas from liquefied ethane goods, especially include Those of lighter component such as methane (with the concentration presence higher than 0.1mol%).Such uncondensable component can be with gas Liquefied ethane goods storage tank is mutually returned to, but this will be accumulated in boil-off gas in closed system, therefore increase with the time Plus concentration.In addition, with the concentration increase of the not condensable components in boil-off gas, it is impossible to the boil-off gas being re-condensed Volume will increase, so as to reduce the available capacity of re-liquefied system.
As mentioned above, not another replacement of the discharge of condensable components such as methane (it is probably greenhouse gases) Scheme in the environment with it is commercial be all undesirable.
WO2012/143699A is related to for making the BOG from liquefaction goods flow re-liquefied method in floating cargo ship And device, the liquefaction goods has the boiling point more than -110 DEG C at 1 atmosphere pressure, wherein potentially including uncondensable The discharge of the cooling of BOG components is flowed carries out heat exchange with compression, a part of of BOG streams for cooling down and then expanding.This is especially fitted Share in the liquefaction goods with more than -110 DEG C of boiling points when measuring at 1 atmosphere pressure, but exist and provide improved cold But (especially re-liquefied as much as possible under rational OPEX and CAPEX) the liquefied ethane goods that comes from is (especially including increase Ratio lighter component such as methane such goods) boil-off gas method the need for.
The present invention solves these problems by triple coolings and using the BOG streams of compression.In this manner, triple cooling streams Will previously uncooled component condensation, can be by re-liquefied and then returned to liquid phase in liquefied ethane product tank.With heat friendship Change medium such as seawater to compare, the BOG streams of the compression of triple coolings provide coming for increased cooling load (cooling duty) Source, it is allowed to BOG stream in lighter component it is re-liquefied.
Therefore, for the compression stage of given quantity, methods and apparatus disclosed herein allows the liquefaction that will be transported Ethane goods has the content of increased lighter component (such as methane), and without increasing, other compression stage or increase are first Before be considered as uncondensable component discharge.Observe in another way, method described herein and device allow to have The compressibility for having the compression stage of given quantity expand to generally can not by it is re-liquefied or condensation component goods.
In a first aspect, the present invention provides the boil-off gas stream of liquefied ethane goods of the cooling in floating cargo ship Method, methods described includes at least following steps：
In two or more compression stages including at least first stage and terminal stage, compression comes from the liquefaction The boil-off gas stream of ethane goods is to provide the BOG discharge streams of compression, wherein the first stage compressed has the first stage Discharge pressure, and the terminal stage compressed has a terminal stage suction pressure, and it is one or more of in the middle of, appoint Selection of land cooling, compression BOG streams are provided between the successive stages of compression；
The BOG discharge streams of compression are cooled down by one or more of first coolant flows, to provide the compression of the first cooling BOG stream；
The BOG streams of the compression of the first cooling are cooled down by least one second coolant flow, to provide the pressure of the second cooling The BOG streams of contracting；
The BOG streams of the compression of the second cooling are cooled down by the 3rd coolant flow, with the BOG for the compression for providing the 3rd cooling Stream；
A part for the BOG streams of the compression of the 3rd cooling is set to be expanded into discharge pressure in the first stage and terminal stage suction Pressure between the pressure of pressure, is flowed with providing the BOG of cooling of the first expansion；
BOG using the cooling of the first expansion is flowed as the 3rd coolant flow, with the BOG for the heating for providing the first expansion Stream；With
BOG streams using the heating of the first expansion are used as second coolant flow or the second coolant flow.
That is, the BOG streams of the cooling of the first expansion are in the heat exchange/exchange for relying on the BOG of the second compression cooled down to flow It is used as the 3rd coolant flow in device, the BOG streams of compression of the heat exchange/cooling of exchanger offer the 3rd and adding for the first expansion The BOG streams of heat are as the 3rd coolant flow of heating, and the 3rd coolant flow of the heating can indirectly, more preferably directly It is used as the second main or secondary coolant flow.
That is, the BOG streams of the heating of the first expansion are in the heat exchange/exchange for relying on the BOG of the first compression cooled down to flow It is used as the second main or secondary coolant flow in device, the heat exchange/exchanger provides the BOG streams of the compression of the second cooling The second coolant flow heated is used as with the BOG streams of the further heating of the first expansion.
As used herein term " first ", " second ", " the 3rd ", " the 4th " etc. are intended to refer to connection or relation, its It can be or can not be direct order, unless wherein clearly stated.That is, can be between " second " and " the 3rd " feature There is other one or more steps or technique or position.These terms be used for be illustrated in stream in or stream heterogeneity or The presence of linked character, and the present invention should not be limited by these terms.
In order to avoid feeling uncertain, the second coolant flow (the BOG streams of the heating of the i.e. first expansion) is in the pressure than the first cooling The BOG stream lower temperatures of contracting；3rd coolant flow (the BOG streams of the cooling of the i.e. first expansion) is in the compression than the second cooling BOG stream lower temperature；And the 3rd coolant flow is in than the second coolant flow lower temperature.
According to another embodiment, method also includes：
BOG streams and the BOG of middle compression as the heating of the first expansion of the second coolant flow of heating are flowed, example Such as the BOG streams of the compression of the first or second centre, preferably merge with the BOG streams of the compression in the middle of first.
According to another embodiment of the invention, the BOG of compression is cooled down by one or more of first coolant flows Discharge stream can be included with providing the step of BOG of the compression of the first cooling flows：
It is cold to provide first by the BOG discharge streams that compression is cooled down as the first cold-producing medium stream of the first coolant flow But the BOG streams of compression.
That is, the first cold-producing medium stream be used as in heat exchange/exchanger by the BOG discharge streams of compression it is a kind of or One kind in more kinds of first coolant flows, the heat exchange/exchanger provide the compression of the first cooling BOG streams and heating the One cold-producing medium stream as heating the first coolant flow.
According to another embodiment of the invention, the BOG of compression is cooled down by one or more of first coolant flows Discharge stream can be included with providing the step of BOG of the compression of the first cooling flows：
It is pre- to provide by the BOG discharge streams that compression is precooled as the precooling coolant flow of the first coolant flow The BOG streams of the compression of cooling；
Flowed by the BOG for the compression that precooling is cooled down as the first cold-producing medium stream of the first coolant flow, to provide the The BOG streams of the compression of one cooling.
That is, precool coolant flow and be used as one kind in heat exchange/exchanger by the BOG discharge streams of compression Or more plant one kind in the first coolant flow, the heat exchange/exchanger provide the compression precooled BOG streams and heating it is pre- Coolant flow is cooled down as the first coolant flow of heating.
That is, the first cold-producing medium stream is used as one in heat exchange/exchanger by the BOG of the compression precooled streams Kind or more plant one kind in the first coolant flow, the heat exchange/exchanger provides the BOG streams of the compression of the first cooling and heated The first cold-producing medium stream as heating the first coolant flow.
According to another embodiment of the invention, it can be open precooling coolant system to precool coolant flow Or a part for the precooling coolant system of closing.Precooling coolant flow can be selected from current, air stream or precooling system Cryogen stream, wherein current or air stream are preferred.Generally, if using open precooling coolant circuit, precooled Coolant flow can be selected from seawater stream and surrounding air stream.Generally, if using the precooling coolant circuit of closing, precooling But coolant flow can be selected from precooling cold-producing medium stream.
According to another embodiment of the invention, by precooling coolant flow to the discharge stream of the compression of precooling Cooling is carried out in heat exchanger such as shell and tube heat exchanger or heat-exchangers of the plate type is precooled.
According to another embodiment of the invention, one or more of first coolant flows include the first cold-producing medium stream, The first refrigerant for example including single refrigerant or refrigerant mixture.First refrigerant should can (i) in compressibility Discharge pressure and compressibility exhaust temperature under, or the discharge pressure and the compression that precools of (ii) in compressibility At a temperature of BOG flows, ethane is condensed.First refrigerant can include one or more of organic compounds, ammonia and especially Hydrocarbon and fluorinated hydrocarbons, such as propane, propylene, difluoromethane and five fluoromethane, including fluorination hydrocarbon mixture R-410A.
According to another embodiment of the invention, by the first cold-producing medium stream to the BOG discharge streams of compression or precooling The cooling of discharge stream of compression be such as shell and tube heat exchanger, heat-exchangers of the plate type or economizer in blowdown exchanger It is middle to carry out.
According to another embodiment of the invention, the BOG discharge streams of all compressions are cold by one or more first But agent stream is cooled down.
In one embodiment of the invention, liquefied ethane goods is included>0.1mol% methane.In fact, liquefaction second Alkane goods can be included>0.4mol% methane, comprising>0.5mol%, 0.6mol%,>0.7mol%,>0.8mol%,> 0.9mol% and>1.0mol% methane.The present invention is extended to 1-5mol% methane, optionally>The liquefaction of 5mol% methane Ethane goods.
The quantity of compression stage is not the limiting factor of the present invention.Optionally, this method includes three or four compression ranks Section.
Optionally, it would be desirable to provide the boil-off gas of total condensation flows as the BOG of the compression of the first cooling, but originally The method that invention expands to the wherein boil-off gas partial condensation after being cooled down by one or more of first coolant flows.
Instant invention overcomes use certain form of heat exchange, especially certain form of heat exchanger, and particularly The difficulty of the conventional shell-coil economizer (shell＆coil economiser) in ground, in conventional shell-coil economizer, temperature Degree method is limited by the composition of the fluid in shell.It is when the composition of the fluid in shell can be one-component, i.e., enough During the gas of " pure ", it is known and extensive by the cooling of the BOG of compression dilation.However, the cooling load exists It is reduction in multicomponent mixture, and in multicomponent mixture (such as especially ethane with significant boiling point difference And methane) in drastically reduce.Therefore, present invention improves over the cooling of the liquefied ethane goods comprising notable methane content circulation The coefficient of performance, i.e., present invention improves over the goods for being presently believed to be bottom line (such as 0.1mol% or less methane) The coefficient of performance, and allow with comprising much higher methane content (e.g., from about or higher than 0.4mol% or 0.5mol% methane) Cargo operation.
The present invention is intended to maintain the use of current boat-carrying equipment and device under its known OPEX and CAPEX, without It is attempt to introduce and how makes using the new equipment required with new operation.
Therefore, according to another embodiment of the invention, by BOG of second coolant flow to the compression of the first cooling The cooling of stream is carried out in economizer.
According to another embodiment of the invention, the BOG streams of the compression of all first coolings rely on the second coolant flow To cool down.
According to another embodiment of the invention, the BOG streams of the compression of all second coolings rely on the 3rd coolant flow To cool down.
In another embodiment of the present invention, this method is further comprising the steps of：
The gaseous effluent stream of the BOG streams of compression from the first cooling is provided；
A part for the BOG streams of the compression of the 3rd cooling is set to expand to form the 4th coolant flow；
Gaseous effluent stream is cooled down by the 4th coolant flow, the 4th cooling agent that the discharge to provide cooling is flowed and heated Stream.
In this manner, it had been considered as previously " not condensable " or " not cold in the BOG of compression that the present invention, which can also be provided, It is solidifying " component it is increased re-liquefied.
Preferably, the 4th coolant flow of heating is BOG recirculation flows or is used as BOG recirculation flows.Therefore, should Method can also include：
4th coolant flow of heating and the BOG of middle compression are flowed, such as in the middle of first or second, preferably first The BOG streams of compression merge.
Optionally, the step of method of the invention is included additionally below：
The discharge stream of cooling is separated, to provide the discharge of discharge discharge stream (vent discharge stream) and cooling BOG returns to stream.
Optionally, the step of method of the invention is included additionally below：
The discharge BOG of cooling is returned throttle, flowed with providing the discharge BOG of cooling of expansion and returning；
The discharge BOG of the cooling of expansion is returned and is streamed to storage tank.
Optionally, the step of this method is included additionally below：
The discharge BOG of cooling is returned throttle, flowed with providing the discharge BOG of cooling of expansion and returning；
The discharge BOG of the cooling of expansion is returned to stream by discharge discharge stream and carry out heat exchange, to provide the row of heat exchange Go out BOG and return to stream, the discharge discharge stream and other discharge discharge stream of cooling；
Expand the discharge discharge stream of cooling, with the discharge discharge stream for the cooling for providing expansion；
The discharge discharge that the discharge BOG of heat exchange is returned to the cooling of stream and expansion is streamed to storage tank.
Optionally, compression stage is the compression stage of multiple stage compressor.
The BOG streams of the compression of first cooling are by the cooling of at least one second coolant flow, to provide the pressure of the second cooling The BOG streams of contracting.Optionally, the BOG streams of the compression of the first cooling are by the second cold of the BOG streams for the heating for only including the first expansion But agent stream is completely or substantially cooled down.Preferably, the second all coolant flows includes the BOG streams of the heating of the first expansion. That is, the BOG streams of the compression of the first cooling can be cooled down by one or more of other second coolant flows, but with There is provided cooling is flowed by using the BOG of the heating of the first expansion to compare, these are secondary or less.
Optionally, the BOG streams of the heating of the first expansion as the second coolant flow include both liquid and gas.It is exactly Say, before as the second coolant flow, it is not necessary that be separated into single gas phase and liquid phase.
Preferably, the liquid and gas of the BOG streams of the heating of the first expansion as the second coolant flow are in the first cooling Compression BOG stream cooling in be separated.The BOG of this compression cooled down preferably by allow to be cooled first The device of stream, preferably economizer are carried out.
According to the second aspect of the invention there is provided a kind of device, liquefaction of the device cooling in floating cargo ship The boil-off gas stream of ethane goods, the boil-off gas stream includes multiple components, and described device is included at least：
Compressibility, to compress the boil-off gas stream from liquefied ethane goods, the compressibility is including two or more Multiple compression stages, compression stage includes at least first stage and terminal stage, to provide the BOG discharge streams of compression, wherein in Between, optionally cool down, compression BOG stream be provided between the successive stages of compression；
One or more first heat exchangers, to cool down the BOG discharge streams of compression to provide the compression of the first cooling BOG flows；
One or more second heat exchangers, will be separated with relying in one or more second heat exchangers Mixed phase coolant flow come further cool down the first cooling compression BOG stream, with the BOG for the compression for providing the second cooling Stream；
One or more 3rd heat exchangers, are flowed with further cooling down the BOG of compression of the second cooling, to provide the 3rd The BOG streams of the compression of cooling.
Optionally, device as herein defined is exercisable using method as herein defined.
Preferably, second heat exchanger is economizer.
According to the other aspect of the present invention there is provided the floating cargo ship for liquefied ethane goods, it has such as this Device defined in literary operates method as herein defined.
The present invention is applied to any floating cargo ship for liquefied ethane goods.The present invention can be used for floating cargo ship In, wherein liquefied ethane goods storage tank is maintained goods by reducing temperature at about atmospheric pressure by complete refrigeration Liquid phase；And the temperature and increased pressure for for the goods in wherein storage tank passing through reduction (relative to environment temperature and pressure) Combination and be maintained in those ships of liquid phase.
In order to obtain the benefit of methods and apparatus disclosed herein, the use of economizer is unwanted.However, some In embodiment, heat exchanger such as economizer can be arranged between the successive stages of compression, such as in the first and second ranks Between section, flowed with cooling down the BOG of compression of centre.In the presence of three or more compression stages, it is allowed to middle The heat exchanger of the cooling of the BOG streams of compression, such as economizer or intercooler (such as seawater intercooler) can be It is provided between second and final compression stage.
For example, intercooler can be located at second and the 3rd between compression stage.Selectively, economizer can be located at Second and the 3rd between compression stage, and between the first and second compression stages.In economizer, the BOG of the compression of cooling Part expansion, optionally further cooling down of stream can carry out heat exchange with the BOG streams of middle compression.In other reality Apply in scheme, the row that part expansion, optionally further cooling down of the BOG of the compression of cooling stream can be with the compression of cooling The part optionally further cooled down released carries out heat exchange.This causes the further improvement and increased cooling of the coefficient of performance (especially re-liquefied) ability.
It is evident that by maintain exist compression stage quantity and add necessary pipeline, valve and controller with The cooling of the BOG streams of the compression of the second cooling, method disclosed herein are carried out by the dilation of the BOG streams of the 3rd cooling Existing floating cargo ship can be applied to as repacking (retro-fit) with device.
As it is used herein, term " multiple compression stages " is defined continuous (in series) in compressibility Two or more compression stages.Each compression stage can be realized by one or more compressors.Each compression rank Section one or more compressors can independently of other compression stages compressor so that they are driven separately.It is optional Select ground, two or more compression stages can using connected compressor, the compressor generally by single driver and Drive shaft and optional transmission device provide power.The compression stage of such connection can be the one of multiple stage compressor Part.
Methods and apparatus disclosed herein needs at least two compression stages.It is each subsequent after the first compression stage Stage provide compared with the pressure at the discharge in previous stage increased pressure.Term " successive stages " refers to adjacent pressure Contracting stage pair, i.e. stage (n) and next (n+1) stage, wherein " n " is greater than 0 integer.Therefore, successive stages are, example Such as, the first and second stage, or second and phase III, or the third and fourth stage.The stream of middle compression is (and in cooling Between compression stream) refer to connection compression successive stages those stream.On used in the stream of the compression of the centre of cooling Term " next compression stage " or " subsequent compression stage " refer to two successive stages of the stream in the middle of restriction numerically Higher numeral (and higher pressure stage).
Heat exchange steps can be indirect, wherein two or more streams for participating in heat exchange are separated and not straight Contact.Selectively, heat exchange can be direct, and in this case, two or more streams for participating in heat exchange can be with It is mixed, so as to produce the stream of merging.
According to the other aspect of the present invention, there is provided a kind of comprehensive Design (integratively designing) dress The method put, the boil-off gas stream of liquefied ethane goods of the described device cooling in floating cargo ship, the boil-off gas Stream includes multiple components, and this method comprises the following steps：
Selection compressibility to compress the boil-off gas stream from liquefied ethane goods, the compressibility include two or More compression stages, compression stage includes at least first stage and terminal stage, to provide the BOG discharge streams of compression, wherein The BOG streams of middle, optionally cooling down, compression are provided between the successive stages of compression,
One or more first heat exchangers are selected to cool down the BOG discharge streams of compression, to provide the pressure of the first cooling The BOG streams of contracting；
Select one or more second heat exchangers, with by will in one or more second heat exchangers quilt The mixed phase coolant flow of separation further cools down the BOG streams of the compression of the first cooling, to provide the compression of the second cooling BOG flows；With
Select one or more 3rd heat exchangers and flowed with the BOG for the compression for further cooling down the second cooling, to provide The BOG streams of the compression of 3rd cooling.
Optionally, methods described is further comprising the steps of：
Run the process simulation for described device；
Determine the validity of methods described；
Change process variable in the process simulation；With
Repetitive process is simulated.
According to the other aspect of the present invention there is provided a kind of method of design technology, the technique comes from for cooling The boil-off gas stream of the liquefied ethane goods in cargo ship is floated, methods described includes at least following steps：
Design compressibility to compress the boil-off gas stream from liquefied ethane goods, the compressibility include two or More compression stages, compression stage includes at least first stage and terminal stage, to provide the BOG discharge streams of compression, wherein The BOG streams of middle, optionally cooling down, compression are provided between the successive stages of compression,
One or more first heat exchangers are designed to cool down the BOG discharge streams of compression, to provide the pressure of the first cooling The BOG streams of contracting；
Design one or more second heat exchangers, with by will in one or more second heat exchangers quilt The mixed phase coolant flow of separation further cools down the BOG streams of the compression of the first cooling, to provide the compression of the second cooling BOG flows；With
Design one or more 3rd heat exchangers and flowed with the BOG for the compression for further cooling down the second cooling, to provide The BOG streams of the compression of 3rd cooling.
Optionally, methods described is further comprising the steps of：
Run the process simulation for the technique；
Determine the validity of methods described；
Change process variable in the process simulation；With
Repetitive process is simulated.
Design method as discussed herein can combine computer assisted procedures, for by related operating equipment (operational equipment) and controller are attached in whole Ship Structure, and can be by related cost, operation Ability parameter is attached in methodology and design.Method described herein can be encoded to suitable for reading and handling on computers Medium on.For example, performing the code of method described herein can be encoded on magnetic medium or optical medium, it can be with Read by personal or mainframe computer and personal or mainframe computer can be copied to.Then can be by using this personal or big The design engineer of type computer performs methods described.
The some features and its design method of the present invention can be described according to one group of numerical upper limits and one group of numerical lower limits. It should be appreciated that any scope formed by any combinations of such limitation is all expected and fallen within the scope of the present invention. Additionally, it is contemplated that whole design includes being used for the selection for combining the additional structure being used together with being particularly limited to herein.In board, Various structure operation parameters can be selected for basis limit or fixed, or be selected for flexible or a variety of behaviour Make purposes.It is therefore intended that the design method covers on including ship within the spirit and scope of the present invention and any Alternative, modification and the equivalent of the master-plan of outboard (off-vessel).
Embodiment of the present invention is now with reference to non-limitative drawings and is only described by way of embodiment, In accompanying drawing：
Fig. 1 shows a kind of schematic diagram of possible known system of the boil-off gas of the re-liquefied product tank in ship；
Fig. 2 is shown in (especially re-liquefied) cargo ship from floating of according to one embodiment of the invention, cooling Liquefied ethane goods boil-off gas system schematic diagram；
Fig. 3 a and 3b are for pure component BOG cooling systems (3a) and wide boiling point multicomponent mixture cooling system (3b) Economizer temperature curve of the temperature to hot-fluid；And
Fig. 4 shows according to another embodiment of the invention, (especially re-liquefied) from floating fortune for cooling down The schematic diagram of the system of the boil-off gas of liquefied ethane goods in defeated ship.
Float re-liquefied system and draw steam, also referred to as boil-off gas from one or more storage tanks, and by boil-off gas Body is sent to compressor, and boil-off gas is compressed within the compressor so that the steam of compression can rely on and be used as thermoreceptor/refrigeration One or more of cooling agents of agent are cooled and condense.For example, seawater can be used in open loop precools loop Precool the steam of (being typically de-superheated) compression.Then, the steam of the compression of precooling can be returned in closed circulation refrigerant It is further cooled in road by refrigerant.
Those lighter components that cannot rely on the compressed vapour of refrigerant condensation are generally discharged to air in vapour form In or be recycled to storage tank.Generally, liquefaction goods in the temperature (relative to environment) of reduction and increased pressure (relative to air Pressure) in one or two under the conditions of be maintained in storage tank.
Fig. 1 shows the schematic diagram of the known system for the re-liquefied boil-off gas from ethane goods.At present, ethane goods Thing tends to transport in the ethene carrying ship of repacking.Liquefied ethane cargo storage is in tank 50a, and tank 50a can be heat-insulated And/or pressurization, ethane is maintained into liquefaction.The evaporation of ethane in tank, such as due to faulty heat insulation Cause, will cause to form ethane gas in tank 50a headroom, and the gas is commonly referred to as boil-off gas (BOG).For The accumulation of the gas is prevented, the gas is removed from tank 50a as boil-off gas stream 01a.All components are all compressed, And generally the component as much as possible of the boil-off gas being removed is cooled down, with before they return to tank 50a by them Condensation.
Boil-off gas stream 01a can be sent to compressibility 60, for example figure 1 illustrates include the first compression stage 65 and second compression stage 75 two benches compressor.Two benches compressibility 60 produces the BOG discharge stream 06a of compression, and it can Heat exchanger 100 is precooled to be sent to, the BOG discharge streams 06a compressed wherein is cooled by seawater stream 102.Precooling But heat exchanger 100 produces the BOG stream 07a of the compression precooled and the seawater stream 104 of heating.Precooling heat exchanger 100 can So that the BOG discharge streams 06a of compression is de-superheated.
The BOG streams 07a of the compression of precooling can be sent to refrigerant heat exchanger 250, the pressure precooled wherein The BOG stream 07a of contracting are cooled by cold-producing medium stream 252.Refrigerant be able to should be condensed under the discharge pressure of compressibility 60 Ethane.Refrigerant can be propane or propylene.Cold-producing medium stream 252 can include refrigerant heat exchanger 250, refrigerant compression A part for machine and the refrigerant loop (not shown) of refrigerant cooler.Refrigerant loop can be the refrigerant system of closing System.Such refrigerant loop, also referred to as refrigerant bag, are known.
Refrigerant heat exchanger 250 produces the BOG stream 08a of the compression of cooling and the cold-producing medium stream 254 of heating.The pressure of cooling The BOG streams 08a of contracting is the stream of at least partly condensation, and it is included under the discharge pressure of the second compression stage 75 can be by refrigeration Those components of the boil-off gas of agent " re-liquefied " (condensing).
Cannot rely within the system refrigerant it is re-liquefied and can include as discussed herein it is " not condensable (non-condensable) " " uncooled " component of component and " not condensing (in-condensable) " component, can be from refrigeration Agent heat exchanger 250 or the associated pressure build-up device (associated accumulator) positioned at the downstream of refrigerant heat exchanger 250 It is removed in (not shown) as discharge stream 49, discharge stream 49 is vapor stream.After atmospheric pressure is expanded to, discharge stream 49 leads to Often it is discharged in air.
The BOG streams 08a of the compression of cooling can be sent to other heat exchanger 80, to provide the Returning fluid of cooling Stream 18, it is typically the stream of total condensation.
Then, the Returning fluid stream 18 of cooling can be sent to return pressure regulating equipment 22, such as expander or joule-soup The inferior valve of nurse, with the Returning fluid stream 24 for the cooling for providing expansion.Typically, pressure regulating equipment 22 is returned by the Returning fluid stream of cooling BOG discharge stream 06a of 18 pressure from the BOG discharge streams 06a of compression pressure or close to compression pressure, which is reduced to, to be approached The pressure of the pressure, such as pressure just above the BOG in tank of liquid ethane and BOG in tank 50a, the pressure is enough really The Returning fluid stream 24 of the cooling expanded is protected to tank 50a appropriate flowing.The pressure of the Returning fluid stream 24 of the cooling of expansion is low In the pressure of the discharge pressure of the first compression stage 65.
Compressibility 60 is returned to, the first compression stage 65 provides the BOG stream 02a of the compression in the middle of first, and it is transmitted To other heat exchanger 80.The BOG streams 02a of compression in the middle of first can be in other heat exchanger 80 by cooling The BOG streams 08a of compression dilation 8b carries out heat exchange, and the BOG of the compression in the middle of first to provide cooling flows 03a, its Then at the suction that the second compression stage 75 can be sent to.The compression of first centre of the compression cooling of second stage 75 BOG flows 03a, to provide the BOG discharge streams 06a of compression.
Fig. 3 a are turned to, this illustrates the representative temperature for the cooling for being used for " pure " material in conventional shell-coil economizer Curve, wherein ' xxxx ' lines represent shell-side, and ' oooo ' lines represent pipe or coil temperature.As can be seen that shell-side temperature It is " flat " so that shell-side temperature does not change with increased hot-fluid.This represents the cooling for example pure ethane of " pure " material.
However, Fig. 3 b are shown for the multicomponent mixing with " wide boiling point " (such as the boiling point difference of ethane and methane) Temperature curve in the identical economizer (and using identical lines form) of thing.Fig. 3 b are shown, are difficult to for pipe side Realize stationary temperature.There is the efficiency declined on all hot-fluids is it will be evident that so that for multicomponent mixture, cooling effect Rate is determined by heavier component, and which reduce the potential cooling that can be realized in such equipment.
However, it is still preferred that maintaining the use of such equipment under its known CAPEX.
Methods and apparatus disclosed herein attempts the method and apparatus for providing improved re-liquefied BOG.Disclose in fig. 2 The embodiment of the method according to the invention and device.In appropriate circumstances, with those identical streams in Fig. 1 and component Title and identical reference numeral have been used for corresponding stream and component in remaining figure.
Fig. 2 shows the liquefied ethane goods storage tank 50 in floating cargo ship, such as ethane cargo ship.Liquefied ethane goods Ethane and methane can be included.In order to cool down the goods of the evaporation of (especially re-liquefied) from storage tank 50, include the goods of evaporation The boil-off gas stream 01 of thing is sent to the compressibility 60 with two or more compression stages.Boil-off gas stream 01 can be with With in the pressure (" BOG pressure ") in the range of higher than 0kPa to 500kPa gauge pressures.Compressibility 60 can include two The multiple stage compressor in individual or more stage.According to " multiple stage compressor ", it refers to each compression rank within the compressor Section is driven by identical drive shaft.Selectively, compressibility 60 can include the independent driving for each compression stage Compressor.When compressibility 60 is multiple stage compressor, it is typically reciprocating compressor.
Fig. 2 embodiment shows the compression with first stage 65 and second stage 70 and the 3rd and terminal stage 75 System 60, but method described herein and device are equally applicable to two benches or more than triphasic compressor.Compression First stage 65 and terminal stage 75 lowpressure stream and high-pressure spray are provided at their discharge respectively.
The Compression Evaporation gas stream 01 of compressibility 60, to provide the BOG discharge streams 06 of compression.The BOG discharge streams 06 of compression Can have in from 1.5MPa to 3.2MPa or higher, such as pressure (" terminal stage pressure ") in the range of up to 6MPa.
The BOG discharge streams 06 of compression are in one or more first heat exchangers 200,300 by one or more First coolant flow 202,302 is cooled down, with the BOG streams 08 for the compression for providing the first cooling.In the embodiment of fig. 2, press The BOG discharge streams 06 of contracting can be sent to as the precooling heat exchange of one in one or more first heat exchangers Device 200.The BOG discharge streams 06 of compression rely on and are used as a kind of precooling cooling agent in one or more of first coolant flows Stream is pre-cooled.It can be air stream or current, such as surrounding air stream or seawater stream to precool coolant flow 202.Precool Heat exchanger 200 can be shell and tube heat exchanger or heat-exchangers of the plate type.Precooling heat exchanger can arrange the BOG of compression 06 is released to be de-superheated.Precool heat exchanger 200 and the BOG streams 07 of the compression precooled and the precooling coolant flow of heating are provided 204.Typically, will have+36 DEG C or lower, more typically+32 DEG C or lower temperature as the seawater for precooling cooling agent.
It is optional in methods and apparatus disclosed herein to precool heat exchange/exchanger 200.This be it is favourable, because The cooling load of subsequent cooling step is reduced for it.However, this aspect not necessarily so that in selectable embodiment party In case, the BOG discharge streams 06 of compression can be directly transferred to blowdown exchanger 300 via pipeline 06 ' so that can omit By the equipment shown in mark 210.In this case, the cooling capacity of blowdown exchanger 300 will have to increasing and be compensated for The missing of precooling.
Then the BOG streams 07 of the compression of precooling can be sent to as in one or more first heat exchangers Another blowdown exchanger 300.Blowdown exchanger 300 is by as another in one or more of first coolant flows The first a kind of cold-producing medium stream 302 cools down the BOG streams 07 of the compression of precooling.Blowdown exchanger 300 provides first and cooled down Compression BOG stream 08 and heating the first cold-producing medium stream 304.
First cold-producing medium stream 304 of the first cold-producing medium stream 302, blowdown exchanger 300 and heating can be the first refrigeration A part for agent system (not shown).This first refrigerant system can also include the first coolant compressor, for compressing First cold-producing medium stream 304 of heating is to provide the first cold-producing medium stream of compression；First refrigerant cooler, makes for cooling down first Cryogen is to provide the first cold-producing medium stream of the compression of cooling；With the first refrigerant bloating plant, the compression for expanding cooling First cold-producing medium stream is to provide the first cold-producing medium stream 302.First refrigerant system can be closed system.First refrigerant can be with Including one or more of organic compounds, especially hydrocarbon and fluorinated hydrocarbons, such as propane, propylene, difluoromethane and five fluoromethane, Including fluorination hydrocarbon mixture R-410A, and one or more of inorganic compound such as ammonia.
The BOG streams 08 of the compression of first cooling can be partial condensation, the BOG streams of compression, including can be in compression Those components for the boil-off gas being condensed under the discharge pressure of terminal stage by the first refrigerant.Any uncooled component It can be removed, or be removed from discharge receiver (not shown) from blowdown exchanger 300 as discharge stream (not shown), be arranged Put receiver and play a part of gas/liquid separator positioned at the downstream of blowdown exchanger 300.Suitable for gas and liquid group The blowdown exchanger of the separation divided is shell and tube heat exchanger, wherein, and the BOG of the compression of cooling is located at shell-side.
Any discharge receiver can be accumulator, and can operate to maintain liquid in blowdown exchanger 300 Sealing and/or the maintenance discharge pressure at the terminal stage 75 of compression.
Blowdown exchanger 300 can be that steam and condensation can not be mutually sufficiently separated into the type individually flowed, for example Board-like and finned type heat exchanger.In this case, discharge receiver is incited somebody to action positioned at the downstream of blowdown exchanger 300 Uncondensed components are used as discharge flow separation.
Then the BOG streams 08 of the compression of first cooling are cooled down for the second time.This can pass through the compression cooled down first BOG streams 08 are sent to second heat exchanger 180 to realize.Second heat exchanger 180 can be any types, and for cooling down In the interstage of the stream 08 of the compression of the middle cooling of BOG streams 02 or 04 and first, especially first stage economizer is in Fig. 2 In show.
The cooling of the BOG streams 08 of the compression of first cooling is by the second coolant flow to provide the compression of second cooling BOG streams 34.Optionally, first cooling compression BOG stream 08 it is a part of can transmit into second heat exchanger (180) it It is preceding to be used elsewhere, but in the present invention, it is preferred that the completely or generally compression of all first coolings BOG streams 08 enter first heat exchanger 180.
The effect of second cooling agent described below is to provide the BOG streams 34 of the compression of the second cooling.Again, the stream 34 A part can be used elsewhere, but preferably completely or generally BOG streams 34 of the compression of all second coolings Into the 3rd heat exchanger 195, with the BOG streams 34 for the compression for further cooling down the second cooling, and to provide the 3rd cooling The BOG streams 35 of compression.
3rd heat exchanger 195 can be any kind of, such as economizer, but it is preferred that counterflow heat exchanger, example Board-like and finned type heat exchanger as known in the art.
In the present invention, a part for the BOG streams 35 of the compression of the 3rd cooling is expanded to discharges pressure in the first stage Pressure between terminal stage suction pressure, 33a is flowed to provide the BOG of cooling of the first expansion.The effect can be with ability Mode known to domain is carried out by pressure regulating equipment 80 such as Joule-Thomson valve or expander.
The BOG streams 33a of the cooling of first expansion is used as the 3rd cooling agent in the 3rd heat exchanger 195, and the heat is handed over Change the BOG streams 35 for the compression that the 3rd cooling is provided and the 3rd coolant flow 33b as heating the first heating expanded BOG flows 33b, and the 3rd coolant flow 33b of the heating can indirectly or more preferably directly be used as the second coolant flow 33b.The BOG of the heating of first expansion flows the/the second coolant flow 33b and not divided before being used as the second coolant flow 33b From (to separate gas phase and liquid phase), with the BOG for the heating that the first expansion is made full use of after the use in the 3rd heat exchanger 195 All remaining cooling effects of stream.
The BOG of the heating of first expansion flows the/the second coolant flow 33b and is transferred into second heat exchanger 180 so that with The heat exchange of the BOG streams 08 of the compression of first cooling provides the BOG streams 34 of the compression of the second cooling in second heat exchanger 180 With the second cooling agent of heating.Second cooling agent of heating can include steam and liquid component, and the steam and liquid component exist It is conveniently separated, and is will be discussed in detail below in second heat exchanger 180.Second coolant flow of heating, it is first The BOG streams of the further heating of expansion, can be sent to the BOG streams of the compression of the centre with appropriate pressure.In Fig. 2 reality Apply in scheme, the second coolant flow of heating merges with the BOG streams 02 of the compression in the middle of first.
The part for being not used for providing the BOG streams 35 of the compression of the BOG streams 33a of the cooling of the first expansion the 3rd cooling can be with As stream is returned, return to stream 36 as the BOG of the cooling of expansion via pressure regulating equipment 82 and return in a manner known in the art Product tank 50.
It is characterized in the property based on first heat exchanger 200,300 and second heat exchanger 180 that one of the present invention is specific Matter does not need CAPEX to change so that operator can be continuing with " conventional " shell economizer as second heat exchanger 180, and the present invention can realize simply by adding the 3rd heat exchanger 195.This allows the whole re-liquefied systems of BOG Controlled by the controller of the existing level at least second heat exchanger 180, so that avoid may be due to using different BOG composition the different stages between temperature controlled potential problems caused by pressure.
In fact, for the methane (in the liquid phase) containing higher than bottom line level, and even above 0.4mol% Or the ethane goods of 0.5mol% methane, for the goods that liquefies BOG method of re-liquefaction and device refrigerating capacity 10%- 15% improvement is possible.When providing the ethane of new or other sources, such liquefied ethane goods containing methane May be more and more universal, but the demand of purification ethane (by reducing or eliminating any methane content) is not before transportation Cost-effective, or be not local possible in some cases.
Fig. 4 shows the other embodiments of methods and apparatus of the present invention.As Fig. 2, Fig. 4 shows liquefied ethane goods Thing storage tank 50, including the boil-off gas stream 01 of the goods of evaporation are sent to compressibility 60 from the storage tank 50, the compression system System 60 has three stage compressions, i.e. first stage 65, second and interstage 70 and the 3rd and terminal stage 75.First stage 65 provide the BOG streams 02 of the compression in the middle of first, and BOG streams 02 enter in first of second heat exchanger 180 to provide cooling Between BOG streams 03, BOG streams 03 enter the intermediate compression stage 70 to provide the BOG streams 04 of the compression in the middle of second, BOG streams 04 enters at the suction of the terminal stage 75 of compression.
Compressibility 60 provides the BOG discharge streams 06 of compression, and the discharge stream 06 can be sent to as one or more In the precooling heat exchanger 200 of one in individual first heat exchanger, in the previously described manner by as in seawater stream A kind of first cooling agent of seawater in 202 is cooled down, with the BOG streams 07 for the compression for providing precooling.
Then the BOG streams 07 of the compression of precooling can be sent to as one or more in the previously described manner Another blowdown exchanger 300 in first heat exchanger.Blowdown exchanger 300 provides the compression of the first cooling BOG streams 08 and the first cold-producing medium stream 304 of heating.
The BOG streams 08 of the compression of first cooling can be directly provided, or optionally transport through discharge reception It is provided after device 305, as shown in Figure 4.
In the case where the BOG of the compression of cooling flows 08 non-total condensation, the conduct of self-discharging heat exchanger 300 is also provided for Flow 51a's and/or carry out self-discharging receiver 305 as stream 51b gaseous effluent stream 51.Although Fig. 4 shows two kinds of streams 51a, 51b It is separated, but these streams can be provided distinctively dividually or in combination or without any, this depends on discharge heat and handed over The property and structure of parallel operation 300 and discharge receiver 305.The offer of these streams or a variety of streams is known in the art.
Gaseous effluent stream 51 can include " not condensable " component and " not condensing " component.Non-condensing component is typically considered to It is that can not actually be compressed and condensed forever in the specifically limitation of floating cargo ship BOG cooling systems and operating parameter Component, and relate generally to nitrogen.
Generally, it is considered that main not condensable components are methane, its boiling point at 1 atmosphere pressure is substantially less than ethane Boiling point, and it is taken as that its condensation is generally also unrealistic in the limitation of floating cargo ship and operating parameter.
In WO2012/143699A, show the amount or ratio of the condensation for increasing gaseous effluent stream to increase its time The method and apparatus of yield.
In the present invention, as shown by by example in Fig. 4, method and apparatus can also include making the 3rd cooling Compression BOG streams 35 part expansion to form the 4th coolant flow 33c the step of, the step is generally the 3rd cold by making But a part for the BOG streams 35 of compression is with a certain amount by pressure-reducing valve 87, and the amount allows the BOG of the compression of the 3rd cooling to flow 35 The part serve as the 4th cooling agent 33c in the 4th heat exchanger 197 (such as discharging heat exchanger).
Such as 4th heat exchanger 197 can be any types, but it is preferred that counterflow heat exchanger, board-like and finned Arrangement.As shown in Figure 4, gaseous effluent stream 51 can be cooled down by the 4th coolant flow 33c, to provide cooling Discharge stream 53 and the 4th coolant flow 38 of heating.
Optionally, the 4th coolant flow 38 of heating is BOG recirculation flows, and it can enter second heat exchanger 180, make A part for the BOG streams 03 that must be used as from its steam in the middle of the first of cooling.
The cooling of gaseous effluent stream 51 in discharge heat exchanger 197 can be condensed can not be in blowdown exchanger 300 A part for the component of the middle boil-off gas being condensed by the first refrigerant such as propane or propylene.The discharge stream 53 of cooling leads to It is often the stream of at least partly condensation.
In one embodiment, the discharge stream 53 of cooling can be sent to discharge stream pressure regulating equipment 61 (dotted line), example Such as Joule-Thomson valve or expander, the discharge stream 63 that wherein its pressure is lowered the further cooling to provide expansion is (empty Line).Expansion further cooling discharge stream 63 can have be in or a little higher than liquefied ethane goods storage tank 50 pressure Pressure so that it may return to tank, for example, return to stream 36 by being added to the cooling BOG of expansion to provide the expansion of merging Cooling BOG return stream 11.
In Fig. 4 in another shown embodiment, the discharge stream 53 of cooling can be sent to discharge flow separation Device 150, such as gas/liquid separation.Discharge stream separator 150 provide be completely or generally non-condensing component discharge discharge stream 55, it typically is vapor stream；And the discharge BOG of cooling returns to stream 57, it typically is the stream of condensation, is included in the 4th heat exchange Those components for the boil-off gas being condensed in device 197.The pressure of discharge discharge stream 55 can be lowered, for example, be reduced to and be suitable to The pressure of storage tank 50 is returned to, for the storage elsewhere or for discharging.
The discharge BOG of cooling, which returns to stream 57 and can be transmitted through discharge and return, flows (such as joule-the Tom of pressure regulating equipment 58 Inferior valve or expander), return to stream 59 to provide the discharge BOG of cooling of expansion.The discharge BOG of the cooling of expansion returns to stream 59 can To be sent to storage tank 50, for example, stream 36 is returned to by the BOG for the cooling for being added to expansion.
The part the 3rd that pressure regulating equipment 80 and 87 is not transferred to provide the third and fourth coolant flow 33a, 33c is cold But offer BOG return stream 10, the BOG returns stream 10 of BOG streams 35 of compression can be expanded to by pressure-reducing valve 82 to be in or connects The pressure of nearly storage tank 50 returns to stream 36 as the BOG of the cooling of expansion.Then storage tank 50 can be returned to.
It will be understood by those skilled in the art that without departing from the scope of the appended claims, the present invention can be with Many different modes are implemented.For example, the present invention covers the group of one or more optional or preferred features disclosed herein Close.

Claims (27)

1. a kind of method for the boil-off gas stream (01) for cooling down the liquefied ethane goods in floating cargo ship, methods described bag Include at least following steps：
In two or more compression stages including at least first stage (65) and terminal stage (75), compression is from described The boil-off gas stream (01) of liquefied ethane goods is to provide the BOG discharge streams (06) of compression, wherein the first stage compressed (65) there is the first stage to discharge pressure, and the terminal stage (75) compressed has terminal stage suction pressure, and The BOG streams (02,03,04) of in the middle of one or more of, optionally cooling down, compression are carried between the successive stages of compression For；
The BOG discharge streams (06) of the compression are cooled down by one or more of first coolant flows (202,302), to provide the The BOG streams (08) of the compression of one cooling；
The BOG that the compression of first cooling is cooled down by least one second coolant flow flows (08), to provide the second cooling Compression BOG stream (34)；
The BOG that the compression of second cooling is cooled down by the 3rd coolant flow flows (34), to provide the 3rd compression cooled down BOG flows (35)；
It is expanded into a part for the BOG streams (35) of the compression of the 3rd cooling and discharges pressure and described in the first stage Pressure between the pressure of terminal stage suction pressure, (33a) is flowed to provide the BOG of cooling of the first expansion；
Using the BOG streams (33a) of first cooling expanded as the 3rd coolant flow, to provide adding for the first expansion The BOG streams (33b) of heat；With
BOG streams (33b) using first heating expanded are used as second coolant flow or the second coolant flow.
2. according to the method described in claim 1, wherein the liquefied ethane goods is included>0.1mol% methane.
3. method according to claim 2, wherein the liquefied ethane goods is included>0.5mol% methane.
4. the method according to any one of preceding claims, including three or four compression stages.
5. the method according to any one of preceding claims, wherein, by second coolant flow to described The cooling of the BOG streams (08) of the compression of one cooling is carried out in economizer (180).
6. the method according to any one of preceding claims, wherein, the BOG of the compression of all first cooling Stream (08) is cooled down by second coolant flow (33a).
7. the method according to any one of preceding claims, wherein, the BOG of the compression of all second cooling Stream (34) is cooled down by the 3rd coolant flow (33a).
8. the method according to any one of preceding claims, further comprising the steps of：
The gaseous effluent stream (51) of the BOG streams (08) of compression from the described first cooling is provided；
A part for the BOG streams (35) of the compression of the 3rd cooling is set to expand to form the 4th coolant flow (33c)；With
Cool down the gaseous effluent stream (51) by the 4th coolant flow (33c), with provide cooling discharge stream (53) and 4th coolant flow (38) of heating.
9. method according to claim 8, the 4th coolant flow (38) including the use of the heating is recycled as BOG Stream.
10. the method according to any one of claim 8 to 9, including additionally below the step of：
Expand the discharge stream (53) of the cooling, with the discharge stream (63) for the further cooling for providing expansion；With
The discharge stream (63) of the further cooling of the expansion is sent to storage tank (50).
11. the method according to any one of claim 8 to 9, including additionally below the step of：
The separation discharge stream (53) further cooled down, is flowed with providing the discharge BOG of discharge discharge stream (55) and cooling and returning (57)。
12. method according to claim 11, including additionally below the step of：
The discharge BOG of the cooling is returned to stream (57) expansion, stream (59) is returned to provide the discharge BOG of cooling of expansion；With
The discharge BOG of the cooling of the expansion is returned into stream (59) and is sent to storage tank (50).
13. the method according to any one of preceding claims, wherein, by one or more of first coolant flows (202,302) the BOG discharge streams (06) of the compression cooled down flowed with the BOG for the compression for providing the first cooling the step of (08) Including：
The BOG discharge streams (06) of the compression are precooled by the precooling coolant flow (202) as the first coolant flow, with The BOG streams (07) of the compression precooled are provided；With
The BOG that the compression of the precooling is cooled down by the first cold-producing medium stream (302) as the first coolant flow flows (07), with The BOG streams (08) of the compression of first cooling are provided.
14. method according to claim 13, wherein the precooling coolant flow (202) is in following group It is one or more of：Seawater stream, air stream, more particularly surrounding air stream and/or cold-producing medium stream.
15. the method according to any one of claim 13 or claim 14, wherein first cold-producing medium stream (302) it is one or more in the group selected from propane and propylene.
16. the method according to any one of preceding claims, wherein compression stage (65,75) are multiple stage compressors Compression stage.
17. the method according to any one of preceding claims, wherein all second coolant flows include institute State the BOG streams (33b) of the heating of the first expansion.
18. the method according to any one of preceding claims, wherein described as second coolant flow The BOG streams (33b) of the heating of one expansion include both liquid and gas.
19. method according to claim 18, wherein the heating of first expansion as second coolant flow BOG stream (33b) the liquid and gas described first cooling compression BOG stream (08) the cooling in divided From.
20. a kind of device for the boil-off gas stream (01) for cooling down the liquefied ethane goods in floating cargo ship, the evaporation Gas stream (01) includes multiple components, and described device is included at least：
Compressibility (60), to compress the boil-off gas stream (01) from liquefied ethane goods, the compressibility includes two Or more compression stage, the compression stage includes at least first stage (65) and terminal stage (75) to provide compression BOG discharge streams (06), wherein in the middle of, optionally cool down, compression BOG stream (02,03,04) compression successive stages it Between be provided；
One or more first heat exchangers (200,300), to cool down the BOG discharge streams (06) of the compression to provide first The BOG streams (08) of the compression of cooling；
One or more second heat exchangers (180), will be in one or more second heat exchanger with dependence Separated mixed phase coolant flow (33b) flows (08) further to cool down the BOG of the compression of first cooling, to provide the The BOG streams (34) of the compression of two coolings；With
One or more 3rd heat exchangers (195), (34) are flowed further to cool down the BOG of compression of second cooling, (35) are flowed with the BOG for the compression for providing the 3rd cooling.
21. device according to claim 20, it is that usage right requires that the method described in any one of 1 to 19 can be grasped Make.
22. the device according to claim 20 or claim 21, wherein the second heat exchanger (180) is section heat Device.
23. one kind floating cargo ship, for the liquefied ethane goods in floating cargo ship, the floating cargo ship, which has, such as to exist Device defined in any one of claim 20 to 22 is used as defined in any one of claim 1 to 19 Method.
24. a kind of method of comprehensive Design device, the steaming of liquefied ethane goods of the described device cooling in floating cargo ship Get angry body stream (01), the boil-off gas stream (01) includes multiple components, the described method comprises the following steps：
Compressibility (60) is selected, to compress the boil-off gas stream (01) from liquefied ethane goods, the compressibility includes Two or more compression stages, the compression stage includes at least first stage (65) and terminal stage (75) to provide compression BOG discharge streams (06), wherein in the middle of, optionally cool down, compression BOG stream (02,03,04) in the successive stages of compression Between be provided；
One or more first heat exchangers (200,300) are selected, to cool down the BOG discharge streams (06) of the compression with offer The BOG streams (08) of the compression of first cooling；
One or more second heat exchangers (180) are selected, will be in one or more the second heat exchange with dependence The mixed phase coolant flow (33b) being separated in device flows (08) further to cool down the BOG of the compression of first cooling, to carry (34) are flowed for the BOG of the compression of the second cooling；With
One or more 3rd heat exchangers (195) are selected, are flowed with further cooling down the BOG of compression of second cooling (34) (35), are flowed with the BOG for the compression for providing the 3rd cooling.
25. method according to claim 24, further comprising the steps of：
Run the process simulation for described device；
Determine the validity of methods described；
Change process variable in the process simulation；With
Repeat the process simulation.
26. a kind of method of design technology, the technique is used for the steaming for cooling down the liquefied ethane goods in floating cargo ship Get angry body stream (01), methods described includes at least following steps：
Compressibility (60) is designed, to compress the boil-off gas stream (01) from liquefied ethane goods, the compressibility includes Two or more compression stages, the compression stage includes at least first stage (65) and terminal stage (75) to provide compression BOG discharge streams (06), wherein in the middle of, optionally cool down, compression BOG stream (02,03,04) in the successive stages of compression Between be provided；
One or more first heat exchangers (200,300) are designed, to cool down the BOG discharge streams (06) of the compression with offer The BOG streams (08) of the compression of first cooling；
One or more second heat exchangers (180) are designed, will be in one or more the second heat exchange with dependence The mixed phase coolant flow (33b) being separated in device flows (08) further to cool down the BOG of the compression of first cooling, to carry (34) are flowed for the BOG of the compression of the second cooling；With
One or more 3rd heat exchangers (195) are designed, are flowed with further cooling down the BOG of compression of second cooling (34) (35), are flowed with the BOG for the compression for providing the 3rd cooling.
27. method according to claim 26, further comprising the steps of：
Run the process simulation for the technique；
Determine the validity of methods described；
Change process variable in the process simulation；With
Repeat the process simulation.
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