CN113767246B - System for controlling pressure in liquefied natural gas container - Google Patents

System for controlling pressure in liquefied natural gas container Download PDF

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Publication number
CN113767246B
CN113767246B CN202080032115.2A CN202080032115A CN113767246B CN 113767246 B CN113767246 B CN 113767246B CN 202080032115 A CN202080032115 A CN 202080032115A CN 113767246 B CN113767246 B CN 113767246B
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China
Prior art keywords
heat exchanger
gas
tank
control system
refrigerant
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Application number
CN202080032115.2A
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Chinese (zh)
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CN113767246A (en
Inventor
B.奥恩
P.博里塞维奇
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Gaztransport et Technigaz SA
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Gaztransport et Technigaz SA
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • 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
    • 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
    • F17C13/02—Special adaptations of indicating, measuring, or monitoring equipment
    • 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
    • F17C3/00—Vessels not under pressure
    • F17C3/02—Vessels not under pressure with provision for thermal insulation
    • F17C3/025—Bulk storage in barges or on 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
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • 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
    • F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • 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
    • F25J1/0203—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
    • F25J1/0204—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 as a single flow SCR cycle
    • 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
    • F25J1/0228—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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
    • 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
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2201/00—Vessel construction, in particular geometry, arrangement or size
    • F17C2201/05—Size
    • F17C2201/052—Size large (>1000 m3)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/04—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by other properties of handled fluid before transfer
    • F17C2223/042—Localisation of the removal point
    • F17C2223/043—Localisation of the removal point in the 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/04—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by other properties of handled fluid before transfer
    • F17C2223/042—Localisation of the removal point
    • F17C2223/046—Localisation of the removal point in the liquid
    • F17C2223/047—Localisation of the removal point in the liquid with a dip tube
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0146—Two-phase
    • F17C2225/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2225/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0146—Two-phase
    • F17C2225/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2225/0169—Liquefied gas, e.g. LPG, GPL subcooled
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/033—Small pressure, e.g. for liquefied 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/035—High pressure, i.e. between 10 and 80 bars
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/036—Very high pressure, i.e. above 80 bars
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/04—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by other properties of handled fluid after transfer
    • F17C2225/042—Localisation of the filling point
    • F17C2225/043—Localisation of the filling point in the gas
    • F17C2225/044—Localisation of the filling point in the gas at several points, e.g. with a device for recondensing gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/04—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by other properties of handled fluid after transfer
    • F17C2225/042—Localisation of the filling point
    • F17C2225/046—Localisation of the filling point in the liquid
    • F17C2225/047—Localisation of the filling point in the liquid with a dip tube
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2227/0135—Pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2227/0157—Compressors
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
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    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0171—Arrangement
    • F17C2227/0178—Arrangement in the vessel
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0171—Arrangement
    • F17C2227/0185—Arrangement comprising several pumps or compressors
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0306—Heat exchange with the fluid by heating using the same fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F17C2227/0323—Heat exchange with the fluid by heating using another fluid in a closed loop
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0337—Heat exchange with the fluid by cooling
    • F17C2227/0339—Heat exchange with the fluid by cooling using the same fluid
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0337—Heat exchange with the fluid by cooling
    • F17C2227/0341—Heat exchange with the fluid by cooling using another fluid
    • F17C2227/0355—Heat exchange with the fluid by cooling using another fluid in a closed loop
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • 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
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • 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
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/04—Indicating or measuring of parameters as input values
    • F17C2250/0404—Parameters indicated or measured
    • F17C2250/043—Pressure
    • 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
    • F17C2250/06—Controlling or regulating of parameters as output values
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    • F17C2250/0626—Pressure
    • 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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    • F17C2250/0636—Flow or movement of content
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2260/00—Purposes of gas storage and gas handling
    • F17C2260/02—Improving properties related to fluid or fluid transfer
    • F17C2260/021—Avoiding over pressurising
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/02—Mixing fluids
    • F17C2265/022—Mixing fluids identical fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • F17C2265/034—Treating the boil-off by recovery with cooling with condensing the gas phase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/037—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
    • F17C2265/06—Fluid distribution
    • F17C2265/066—Fluid distribution for feeding engines for propulsion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/0105—Ships
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Abstract

The invention relates to a system (100) for controlling the pressure in a vessel (200) mounted on a vessel, the vessel (200) being configured to accommodate a gaseous cargo (GN), and the pressure control system (100) comprising-at least one cold production unit (110) comprising at least one first heat exchanger (113) and at least one second heat exchanger (115), the first heat exchanger (113) being configured to evaporate liquid Gas (GN) received by the first heat exchanger (113), the second heat exchanger (115) being configured to cool the Gas (GN) and to regulate the pressure in the vessel (200), the first heat exchanger (113) being configured to supply the evaporated Gas (GN) to a device (210, 220) that consumes the Gas (GN); -at least one unit for condensing (120) the Gas (GN) evaporated by the first heat exchanger (113), the unit comprising at least one heat exchanger (121) configured to operate a heat exchange between a portion of the Gas (GN) evaporated by the first heat exchanger (113) and the Gas (GN) withdrawn in liquid form in the vessel (200).

Description

System for controlling pressure in liquefied natural gas container
Technical Field
The present invention relates to the field of ships whose propulsion engines are supplied with natural gas and are also used for containing or transporting liquefied natural gas.
Background
Such vessels therefore typically comprise tanks containing liquid natural gas. Natural gas is liquid at temperatures below-163 ℃ and atmospheric pressure. These tanks are never perfectly insulated, so that the natural gas therein is at least partially vaporized. Thus, these tanks contain both liquid and gaseous natural gas. Such gaseous natural gas forms a vapor space, the pressure of which must be controlled in order not to damage the tank. At the same time, the natural gas contained in these tanks is used to supply engines or the like for propulsion of the ship.
Systems for controlling the pressure in these tanks already exist, but are not entirely satisfactory. Systems are particularly known in which gaseous natural gas is taken from the vapor space and used for particularly supplying engines of propulsion vessels. Such systems thus rely on the consumption of these propulsion engines and the pressure control system becomes ineffective when, for example, the ship is stopped and the gaseous natural gas consumed by these engines is zero or nearly zero.
The present invention falls in this context by proposing a system for controlling the pressure in a tank which makes it possible to regulate both the pressure in the vapor space and to effectively manage the supply of propulsion engines.
Disclosure of Invention
Accordingly, one subject of the present invention relates to a pressure control system for controlling the pressure in a tank equipped with a ship, the tank being configured to contain liquid gas cargo, and the pressure control system comprising:
-at least one cold production unit comprising at least one first heat exchanger configured to evaporate liquid gas received by the first heat exchanger and at least one second heat exchanger configured to cool the gas and to regulate the pressure in the tank, the first heat exchanger being configured to supply the evaporated gas to a gas consuming device;
-at least one condensing unit for condensing the gas evaporated by the first heat exchanger, and comprising at least one heat exchanger configured to provide a heat exchange between a portion of the gas evaporated by the first heat exchanger and the gas withdrawn from the tank in liquid state.
According to the invention, the tank is a tank for storing and transporting liquid gas. The tank is a tank of liquid gas, which is the fuel of the gas consumer.
According to the invention, the system for controlling the pressure in a vapor space according to the invention comprises at least two different modes of operation.
In the first mode of operation, the gas cooled by the second heat exchanger is taken out of the vapor space in the gaseous state, that is to say from the part of the tank in which the gas is in gaseous form. The gas in the gaseous state is cooled as it passes through the second heat exchanger, and is thereby reinjected into the bottom of the tank in the liquid state or at least in the two-phase state, that is to say the portion of the tank in which the natural gas is present in the liquid state. According to this first mode of operation, the pressure reduction in the vapor space is thus performed by directly withdrawing gas from the vapor space.
In the second mode of operation, the gas cooled by the second heat exchanger is withdrawn from the tank in liquid form and then injected into the vapor space. Advantageously, such a cooled injection of liquid natural gas enables cooling of the vapour space, resulting in a condensation of a portion of the gas located therein and thus a drop to the bottom of the tank, while at the same time reducing the pressure of the vapour space.
According to any of these modes of operation, the gas vaporized by the first heat exchanger makes it possible to supply at least one device that consumes the vaporized gas. For example, it may be an engine for propelling a watercraft or a heat engine for a generator. According to an exemplary application of the invention, the gas transported in the tanks and used for supplying the various engines of the ship is natural gas, that is to say a gas with a methane content of more than 80%.
When the amount of the gas evaporated by the first heat exchanger is greater than the amount of the evaporated gas required for the at least one device consuming the evaporated gas, a portion of the gas evaporated by the first heat exchanger is directed to a condensing unit in which the gas is condensed by heat exchange with the gas taken out of the tank in a liquid state. In other words, the gas evaporated by the first heat exchanger releases heat to the gas taken out in the liquid state and is transferred to the heat exchanger so that the gas taken out in the liquid state is heated, and the gas evaporated by the first heat exchanger is cooled and becomes liquid again, thereby being able to be refilled into the tank without increasing the pressure of the vapor space. For example, the heat exchanger may comprise at least one first channel in which the natural gas fluid vaporized by the first heat exchanger is circulated in a liquid state from the tank and at least one second channel in which the heat exchanger is configured to provide heat exchange between the vaporized natural gas circulated in the first channel and the liquid natural gas circulated in the second channel.
According to the invention, more particularly, according to a second operating mode of the pressure control system, the tank comprises a spray bar connected to the output of the second heat exchanger. More specifically, the spray bar is disposed in the vapor space.
According to any of the modes of operation just described, the pressure control system according to the invention comprises at least one conduit extending from the output of the second heat exchanger to the interior of the tank. The conduit may thus re-inject the gas cooled by the second heat exchanger into the tank, that is to say the cooled gas is mixed with the liquid gas already present in the tank. According to one example, the conduit may be present near the bottom of the tank, or in the center of height of the liquid gas, or even near the liquid/gas limit of the cargo, but still present in the liquid part.
According to a first mode of operation of the pressure control system of the invention, the gas fed to the input of the second heat exchanger is taken from the vapor space by the compression means. For example, the compression device may be a compressor configured to increase the pressure of the gas taken out in the gaseous state to a pressure of at most 6 bar.
According to the invention, the pressure control system comprises at least one passage arranged between the output of the heat exchanger and the bottom of the tank. It will be appreciated that the passage allows the gas condensed by the heat exchanger to be re-injected into the bottom of the tank, that is to say the at least one passage is in fluid connection with the first channel of the heat exchanger.
Advantageously, the gas heated by the heat exchanger and the evaporated gas cooled by the heat exchanger are mixed before being distributed to the bottom of the tank. In other words, an additional passage is provided between the other output of the heat exchanger and the passage for the gas condensed by the heat exchanger to be reinjected at the bottom of the tank. Thus, the additional passage is fluidly connected on one side to the second passage of the heat exchanger and on the other side to the passage, which passage itself is fluidly connected to the first passage of the heat exchanger. It will then be appreciated that this passage makes it possible to direct both the gas condensed by the heat exchanger and the liquid gas heated by the heat exchanger to the bottom of the tank.
According to a feature of the invention, at least one low pressure pump is arranged upstream of the first heat exchanger. For example, the low-pressure pump is configured to increase the pressure of the gas withdrawn in the liquid state to a pressure of 6bar to 40bar, advantageously in the range of 6bar to 17 bar.
According to a feature of the invention, at least one high-pressure pump is arranged between the low-pressure pump and the input of the first heat exchanger. Advantageously, the use of such a high-pressure pump makes it possible to supply a device that consumes high-pressure boil-off gas. For example, the high pressure pump is configured to increase the pressure of the boil-off gas by more than 300bar.
According to a first embodiment of the invention, the first heat exchanger comprises a first channel, which is directly supplied by the low pressure pump, and a second channel, which is supplied by the high pressure pump arranged between the low pressure pump and the input of the first heat exchanger. Advantageously, the first channel of the first heat exchanger thus makes it possible to supply a first device consuming the vaporised gas at a low pressure, while the second channel of the first heat exchanger makes it possible to supply a second device consuming the vaporised gas at a high pressure. Alternatively, each channel of the first heat exchanger may be supplied by a low pressure pump specific to it. It should be understood that this is only one exemplary embodiment and that the first heat exchanger may also only supply equipment consuming the boil-off gas at low pressure without departing from the scope of the invention. In the latter case, the second passage is devoid of a high pressure pump.
According to a second embodiment of the invention, the first heat exchanger is configured to supply two devices consuming gas, and the at least one expansion member is arranged between the first heat exchanger and one of the devices consuming evaporating gas. In other words, it can be appreciated that at the output of the first heat exchanger, two branches are formed: a first branch supporting the at least one expansion member so that a first device consuming the boil-off gas may be supplied; and a second branch, without the at least one expansion member, so that a second device consuming the boil-off gas can be supplied, the first and second devices consuming the boil-off gas being distinguished from each other by the pressure of the boil-off gas they are supplied to. Thus, the first branch makes it possible to supply a device that consumes the evaporation gas at a voltage, while the second branch makes it possible to supply a device that consumes the evaporation gas at a high voltage. Again, this is only one exemplary embodiment and the first heat exchanger may also only supply equipment consuming the boil-off gas at low pressure without departing from the scope of the invention. In the latter case, the first branch is devoid of expansion members.
According to a feature of the invention, the cold production unit comprises a refrigerant circuit on which at least one compression member for compressing the refrigerant, at least a first heat exchanger, at least one expansion device and at least a second heat exchanger are arranged. It will thus be appreciated that the first heat exchanger is configured to provide heat exchange between liquid gas withdrawn from the tank and refrigerant, while the second heat exchanger itself is configured to provide heat exchange between liquid gas withdrawn from the tank or gaseous gas withdrawn from the vapor space and refrigerant. For example, the refrigerant includes nitrogen.
Advantageously, the cold production unit thus allows cold production by heat exchange provided by the second heat exchanger, while heat production by heat exchange provided by the first heat exchanger. Advantageously, the cold product is used to reduce the pressure in the vapor space, while the hot product allows for the evaporation of the gas, thereby supplying gas consuming equipment on board the vessel, such as propulsion engines.
According to a third embodiment of the invention, the first heat exchanger is configured to supply a first device consuming low pressure evaporation gas, the control system comprises at least one third heat exchanger configured to supply a second device consuming high pressure evaporation gas, at least one high pressure pump is arranged between the low pressure pump and an input of the third heat exchanger, the third heat exchanger is configured to provide heat exchange between gas taken from the tank in liquid state and refrigerant compressed by the compression member.
According to a feature of the third embodiment of the invention, the refrigerant leaving the third heat exchanger is fed into the first heat exchanger. Advantageously, the refrigerant leaving the third heat exchanger and the refrigerant flowing in the first heat exchanger thus have equal or substantially equal temperatures when mixed.
According to a fourth embodiment of the invention, at least one internal heat exchanger is arranged on the refrigerant circuit, the internal heat exchanger comprising at least one first channel in which the refrigerant compressed by the compression member circulates and at least one second channel in which the refrigerant expanded by the expansion device circulates.
According to a feature of this fourth embodiment, the first heat exchanger is arranged on the refrigerant circuit between the compression member and the internal heat exchanger, while the second heat exchanger itself is arranged on the refrigerant circuit between the expansion device and the internal heat exchanger.
The invention also relates to a ship for transporting liquefied gas, comprising at least one gas cargo tank, at least one device for consuming boil-off gas and at least one system according to the invention for controlling the pressure in the tank.
The invention also relates to a method for managing the pressure in a tank equipped with a ship, which method implements a pressure control system according to a second mode of operation of the pressure control system of the invention, and which method comprises at least the steps of:
-withdrawing liquid gas from the tank;
-evaporating a first portion of the liquid gas withdrawn from the tank by heat exchange with a refrigerant in a first heat exchanger to supply at least one device consuming the evaporated gas;
-cooling a second portion of the liquid gas withdrawn from the tank by heat exchange with the refrigerant in a second heat exchanger and injecting at least a portion of the cooled gas into the vapor space.
As previously mentioned, injecting cooled gas into the vapor space may reduce its temperature, thereby causing the gas present in the vapor space to condense and thus reduce the pressure of the vapor space.
The invention also relates to a method for managing the pressure in a tank equipped with a ship, which method implements a pressure control system according to a first mode of operation of the pressure control system of the invention, and which method comprises at least the steps of:
-withdrawing liquid gas and gaseous gas from the tank and the vapor space, respectively;
-evaporating the liquid gas withdrawn from the tank by heat exchange with a refrigerant in a first heat exchanger to supply at least one device consuming the evaporated gas;
-condensing gaseous gas withdrawn from the tank by heat exchange with the refrigerant in a second heat exchanger and injecting the condensed gas into the bottom of the tank.
According to either of the first or second modes of operation described above, the step of withdrawing gas may be preceded by the steps of:
-measuring the pressure of the vapor space of the tank, comparing the measured pressure value with a reference value, and determining the amount of liquid and/or gaseous gas to be removed from the tank when the measured pressure value is lower than or equal to the reference value;
-determining a boil-off gas demand of the at least one device consuming boil-off gas.
According to the invention, if the amount of liquid and/or gaseous gas to be withdrawn is greater than the amount of boil-off gas required by the at least one device consuming boil-off gas when the measured pressure value is lower than or equal to the reference value, the at least one device consuming boil-off gas is supplied by a first portion of the gas evaporated by the first heat exchanger, a second portion of the gas evaporated by the first heat exchanger is condensed in the heat exchanger by heat exchange with the liquid gas withdrawn from the tank, and the so cooled second portion of the boil-off gas is mixed with the withdrawn liquid gas heated by passing through the heat exchanger before being re-injected into the bottom of the tank.
The invention also comprises a system for loading or unloading liquid gas comprising at least one land-based device and at least one vessel according to the invention for transporting liquid gas.
The invention finally relates to a method for loading or unloading liquid gas from a gas-transporting vessel according to the invention.
Drawings
Other features, details and advantages of the invention will emerge more clearly from a reading of the following description, on the one hand, and from several exemplary embodiments, given in an indicative and non-limiting manner with reference to the accompanying drawings, in which:
fig. 1 schematically shows a system for controlling the pressure in a liquefied gas tank according to a first embodiment and a first mode of operation of the present invention;
fig. 2 schematically illustrates a system for controlling pressure in a liquefied gas tank according to a first embodiment and a first mode of operation of the present invention;
fig. 3 schematically illustrates a system for controlling the pressure in a liquefied gas tank according to a first embodiment and a second mode of operation of the present invention;
fig. 4 schematically illustrates a system for controlling pressure in a liquefied gas tank according to a second embodiment and a first mode of operation of the present invention;
fig. 5 schematically illustrates a system for controlling pressure in a liquefied gas tank according to a second embodiment and a second mode of operation of the present invention;
fig. 6 schematically shows a system for controlling the pressure in a liquid gas tank according to a third embodiment and according to a variant of the second mode of operation;
Fig. 7 schematically shows a system for controlling the pressure in a liquefied gas tank according to a fourth embodiment and according to a second mode of operation;
fig. 8 is a schematic cross-sectional view of a methane tanker tank and a terminal for loading and/or unloading the tank.
Detailed Description
The features, alternatives, and various embodiments of the invention may be associated with each other in various combinations as long as they are not incompatible or mutually exclusive. In particular, alternative forms of the invention are contemplated which include only a selection of the features described below, without the other features described, if such selection of features is sufficient to confer technical advantages or to distinguish the invention from the prior art.
In the following description, the terms "upstream" and "downstream" are understood in terms of the direction of flow of natural gas or refrigerant through the relevant elements. The solid line represents a loop conduit through which refrigerant or natural gas flows, while the dashed line represents a loop conduit through which fluid does not flow. Finally, the narrowest line represents the loop conduit through which the refrigerant flows, while the thickest line represents the loop conduit through which natural gas flows, whether the natural gas is in gaseous, liquid or two-phase form.
Fig. 1 to 5 show different embodiments and different modes of operation of a control system 100 according to the invention for controlling the pressure in a gas tank 200. Common features of all these embodiments and modes of operation of the invention will first be described. The following description gives a specific example of the application of the invention, wherein the tank 200 contains natural gas GN. It should be understood that this is only one example of an application and that the pressure control system 100 according to the present invention may be used with other types of gases, such as hydrocarbon gases or hydrogen.
Thus, the control system 100 according to the invention comprises a cold production unit 110, a condensation unit 120 and at least one control unit 130, wherein the control unit 130 is configured to measure the pressure in the steam space 201 of the tank 200. "vapor space" is understood to mean the portion of tank 200 in which natural gas GN is in the gaseous state. The natural gas GN in the remainder of the tank 200 is in a liquid state and the amount of natural gas GN present in the vapor space 201 in a gaseous state depends on the level of evaporation of the liquid portion of the natural gas GN contained in the tank 200.
As shown in fig. 1 to 5, the cold production unit 110 comprises an air conditioning circuit, that is to say a circuit 111 of the refrigerant FR, on which at least one compression member 112, one first heat exchanger 113, one expansion device 114 and one second heat exchanger 115 are arranged. According to any of the embodiments and/or modes of operation illustrated herein, the first heat exchanger 113 is configured to provide heat exchange between the refrigerant FR and the liquid natural gas GN withdrawn from the tank 200. The first heat exchanger 113 thus acts as a condenser with respect to the refrigerant, as the refrigerant transfers its heat to the natural gas GN taken out of the tank 200, thereby evaporating it.
The second heat exchanger 115 is then configured to provide heat exchange between the liquid or gaseous natural gas GN and the refrigerant FR withdrawn from the tank 200 or vapor space 201, respectively, to cool the natural gas GN. In other words, the second heat exchanger 115 acts as an evaporator with respect to the refrigerant because it cools the natural gas GN and condenses the natural gas GN if it is in the gaseous state.
When the pressure control system 100 is operating, the refrigerant FR, after acquiring heat from the natural gas GN, leaves the second heat exchanger 115 in a gaseous or two-phase state and then reaches the first heat exchanger 113. The refrigerant FR then exits the first heat exchanger 113 in a gaseous state, and then reaches the compression member 112, where its pressure increases. The refrigerant FR then returns to the first heat exchanger 113 where it releases heat significantly to the liquid natural gas GN delivered to the first heat exchanger 113. Thus, the refrigerant FR leaves the first heat exchanger 113 this time in liquid state, it passes the expansion device 114, its pressure is reduced in the expansion device 114, and it finally reaches the second heat exchanger 115, in which second heat exchanger 115 it can again extract heat from the gaseous or liquid natural gas GN flowing in the second heat exchanger 115.
The above-described cycle provides for the refrigerant to pass directly in the first heat exchanger 113 after passing in the second heat exchanger 115. In other words, a passage is provided in the first heat exchanger 113 before the refrigerant enters the compression device 112.
The present invention also includes a cycle wherein refrigerant exiting the second heat exchanger 115 enters the compression device 112 directly without passing through the first heat exchanger 113.
The natural gas GN vaporized by the first heat exchanger 113 is then directed to at least one device 210, 220 that consumes the vaporized natural gas. According to the example shown here, the natural gas GN evaporated by the first heat exchanger 113 makes it possible to supply two devices 210, 220 consuming the evaporated gas.
As will be described in more detail below, the first device 210 consuming the vaporised gas is configured to be supplied by low-pressure gas, that is to say at a pressure in the range of 6bar to 40bar, advantageously in the range of 6bar and 17bar, and the second device 220 consuming the vaporised gas is configured to be supplied by high-pressure gas, that is to say at a pressure of at least 300bar. It should be understood that these are merely exemplary embodiments and that other types of devices that consume the boil-off gas may be used without departing from the scope of the present invention. For example, a single plant consuming vaporized natural gas may be supplied with vaporized natural gas through a first heat exchanger, or two plants consuming vaporized natural gas may consume vaporized natural gas at a low pressure.
For withdrawing the liquefied natural gas GN from the tank 200 and delivering it to the first heat exchanger 113, the control system 100 comprises at least one low-pressure pump 140, that is to say, at the output of this pump, the liquefied natural gas GN is pressurized to a pressure of 6 to 40bar, advantageously 6 to 17bar.
The second heat exchanger 115 is configured to provide heat exchange between the liquid or gaseous natural gas GN and the refrigerant FR withdrawn from the tank 200 or vapor space 201, respectively. Thus, as will be described in greater detail below, according to a first mode of operation of the present invention, natural gas GN delivered to the second heat exchanger 115 is withdrawn from the vapor space 201 in a gaseous state, and according to a second mode of operation of the present invention, natural gas GN delivered to the second heat exchanger 115 is withdrawn from the tank 200 in a liquid state.
According to one or the other of these modes of operation, the natural gas GN exits the second heat exchanger 115 at a temperature lower than when the natural gas GN entered the second heat exchanger 115. According to any of the embodiments or modes of operation described and illustrated herein, the conduit 119 is arranged between the output of the second heat exchanger 115 and the interior of the tank 200 such that the natural gas GN cooled by the second heat exchanger 115 is re-injected into the tank 200 and thus mixed with the liquid natural gas GN already present in the tank 200.
As previously described, the pressure control system 100 according to the present invention includes the control unit 130. The control unit 130 is configured to measure the pressure in the vapor space 201, for example using the pressure sensor 132, to compare the pressure value thus measured with a reference value, and to determine the amount of liquid and/or gaseous natural gas GN to be taken out of the tank 200, so that the pressure value measured in the vapor space 201 is lower than or equal to the reference value.
As schematically represented, the control unit 130 also receives information 133 about its need to vaporize natural gas GN from the equipment 210, 220 consuming vaporized natural gas.
The control unit 130 is configured to control the start-up of the cold production unit 110 when at least one of the devices 210, 220 consuming vaporized natural gas or the measured pressure value in the vapor space 201 is higher than a reference value has a non-zero demand for vaporized natural gas GN, regardless of the mode of operation or embodiment of the present invention.
As far as the condensing unit 120 is concerned, it comprises at least one heat exchanger 121, which heat exchanger 121 is configured to provide a heat exchange between at least a portion of the natural gas GN evaporated by the first heat exchanger 113 and the natural gas GN withdrawn in liquid form from the tank 200. According to the invention, natural gas GN is taken out of tank 200 in liquid form and then delivered to heat exchanger 121 using low pressure pump 141. According to the example shown here, the low pressure pump 141 is different from the low pressure pump 140 of the cold production unit 110, which low pressure pump 140 makes it possible to deliver the liquefied natural gas GN to the first heat exchanger 113, but it should be understood that the two low pressure pumps 140, 141 may be one and the same low pressure pump without departing from the scope of the invention.
It will thus be appreciated that the liquid natural gas GN taken from tank 200 by low pressure pump 141 is delivered to heat exchanger 121 via line 125. Once in the heat exchanger 121, the liquefied natural gas GN taken out of the tank 200 absorbs calories released by the natural gas GN evaporated by the first heat exchanger 113. This heat exchange works in such a way that the natural gas GN leaves the heat exchanger 121 in a liquid or two-phase state. According to the example shown, the heat exchanger 121 comprises at least one first channel 121a and at least one second channel 121b, the natural gas GN evaporated by the first heat exchanger 113 being circulated in the first channel 121a, the natural gas withdrawn in liquid form from the tank 200 being circulated in the second channel 121 b.
A passage 123 is also arranged between the output of the heat exchanger 121 and the tank bottom 200, allowing the properly condensed natural gas GN to be returned to the tank 200. It will also be noted that an additional passage 124 is also provided between the other output of the heat exchanger 121 and the channel 123. Thus, the natural gas GN heated by the heat exchanger 121 and the natural gas GN cooled by the heat exchanger 121 are combined and simultaneously returned to the bottom of the tank 200.
As will be described in more detail below, a valve 122 is arranged upstream of the heat exchanger 121 in order to direct or inhibit the flow of natural gas GN evaporated by the first heat exchanger 113 to this heat exchanger 121. In other words, the valve 122 is disposed between the first heat exchanger 113 and the heat exchanger 121, and at least partially controls the operation of the condensing unit 120. The valve 122 is driven by, for example, a control unit 130 via a control line 134. Thus, the control unit 130 is further configured to determine the larger of the two values of the minimum vaporized natural gas GN demand of the device 210, 220 consuming vaporized natural gas and the minimum amount of natural gas GN to be taken out of the tank 200 to be recovered to the so-called reference pressure. According to the present invention, when the amount of natural gas GN to be taken out in liquid and/or gas is greater than the amount of vaporized natural gas GN required for the device 210, 220 consuming vaporized natural gas in the case that the measured pressure value is lower than or equal to the reference value, the control unit 130 opens the valve 122 to allow the condensing unit 120 to condense the excessively vaporized natural gas GN, thereby allowing the condensed natural gas GN to be returned to the tank 200. On the other hand, when the amount of evaporated natural gas GN required by the equipment 210, 220 consuming the evaporated natural gas is lower than the amount of natural gas GN to be taken out from the tank 200 to be recovered to the reference pressure, the control unit 130 closes the valve 122, thereby forcing all the natural gas GN evaporated by the first heat exchanger 113 to reach the equipment 210, 220 consuming the evaporated natural gas.
Fig. 1 to 3 schematically show a control system 100 for controlling the pressure in a natural gas tank 200 according to a first embodiment of the invention, fig. 1 and 2 show a first operation mode of the control system 100, and fig. 3 shows a second operation mode of the control system 100.
According to this first embodiment, the first heat exchanger 113 comprises at least two channels 116, 117. The first channel 116 of the first heat exchanger 113 is configured to supply a first device 210 consuming the boil-off gas and the second channel 117 of the second heat exchanger 113 is configured to supply a second device 220 consuming the boil-off gas. As previously described, according to an exemplary application of the present invention, the second device 220 that consumes the boil-off gas may be a device that consumes the high-pressure gas. Thus, according to the example shown here, the high-pressure pump 118 is arranged upstream of the second channel 117 of the first heat exchanger 113, that is to say between the low-pressure pump 140 and the input of the first heat exchanger 113. In other words, according to the example shown in fig. 1 to 3, the natural gas GN leaves the first passage 116 of the first heat exchanger 113 at a pressure lower than or equal to 40bar, advantageously at a pressure lower than or equal to 17bar, while the natural gas GN leaves the second passage 117 of the first heat exchanger 113 at a pressure higher than or equal to 300 bar.
It should be understood that this is only one example of an application of the present invention and that the first heat exchanger 113 may be configured to supply only low pressure gas at the device consuming the low pressure gas without departing from the scope of the present invention, and that the second passage does not have a high pressure pump.
Fig. 1 and 2 show a first mode of operation of the pressure control system 100 according to the first embodiment just described. According to this first mode of operation, the compression means 131 is arranged upstream of the second heat exchanger 115, that is to say between the steam space 201 and this second heat exchanger 115. The compression device 131 may thus take gaseous natural gas GN from the vapor space 201 by suction to convey it to the second heat exchanger 115.
Thus, according to the first operation mode of the pressure control system 100 according to the first embodiment of the invention, the control unit 130 detecting an excessive pressure in the vapor space 201 activates the cold production unit 110 and the compression device 131 in order to reduce the pressure by withdrawing the gaseous natural gas GN present in the vapor space 201. The gaseous natural gas GN then reaches the second heat exchanger 115, where it releases heat to the refrigerant FR, which also circulates in the second heat exchanger 115 as previously described. Thus, natural gas GN reappears in a liquid or two-phase state from the second heat exchanger 115 and is injected into the bottom of the tank 200 through the conduit 119 described above.
As previously described, the natural gas GN evaporated by the first heat exchanger 113 is sent to the gas consuming device 210, 220. And then distinguish between the two cases shown in fig. 1 and 2, respectively.
In the first case shown in fig. 1, the boil-off gas demand of the device 210, 220 consuming boil-off gas is lower than the amount of natural gas effectively evaporated by the first heat exchanger 113, and furthermore the amount of natural gas effectively evaporated by the first heat exchanger 113 depends on the pressure in the vapour space 201 as described before. In this case, the valve 122 of the condensing unit 120 is opened and the low pressure pump 141 of the condensing unit 120 is activated so as to be able to condense a portion of the vaporized natural gas, so that this condensed natural gas can be returned to the tank 200 through the passage 123, as previously described. It should be noted that the condensing unit 120 of the pressure control system 100 according to the first embodiment is connected to the first passage 116 of the first heat exchanger 113. In other words, the heat exchanger 121 is supplied with the vaporized natural gas GN at a low pressure.
In the second case shown in fig. 2, the evaporated natural gas consumption of the device 210, 220 consuming the evaporated gas is greater than or equal to the amount of gas effectively evaporated by the first heat exchanger 113. Thus, in the second case, the valve 122 is closed and the low pressure pump 141 of the condensing unit 120 is stopped. In other words, in the second case, no fluid circulates in the condensing unit 120.
Fig. 3 shows a second mode of operation of the pressure control system 100 according to the first embodiment described above. According to this second mode of operation, natural gas GN delivered to the second heat exchanger 115 is withdrawn from tank 200 in liquid form by low pressure pump 142. According to the example shown here, this low pressure pump 142 is different from the low pressure pump 140 of the cold production unit 110 and the low pressure pump 141 of the condensation unit 120, but it should be understood that it may also be the same low pressure pump without departing from the scope of the invention.
As described above, the liquefied natural gas GN releases heat to the refrigerant FR flowing through the second heat exchanger 115, so that the natural gas GN is cooled by the second heat exchanger 115. The conduit 119 arranged between the output of the second heat exchanger 115 and the interior of the tank 200 containing liquid natural gas has a bypass 150 extending between the conduit 119 and the vapour space 201, that is to say that one end of the bypass 150 is present in the vapour space 201. As schematically shown, this end of the bypass 150 carries a spray bar 151. Thus, at least a portion of the natural gas GN cooled by the second heat exchanger 115 is injected into the vapor space 201. The flow of cooled natural gas GN to the boom 151 relies on a valve 152 (e.g., a three-way valve) disposed on the conduit 119 at the beginning of the bypass 150.
It will then be appreciated that when the control unit 130 measures a pressure in the vapour space 201 that is too high relative to the reference value, it activates the low pressure pump 142 such that liquid natural gas GN is injected into the vapour space 201 by the injection lance 151. Such injection makes it possible to reduce the temperature of the vapor space 201, resulting in condensation of a portion of the natural gas GN present in the vapor space 201 in the gaseous state, which makes it possible to reduce the pressure of the vapor space 201 to a value lower than the reference value.
According to a variant of the second operating mode of the pressure control system according to the invention, not shown, the spray bar can be replaced by a gravity heat exchanger as described in document FR 3049331. The contents of this document regarding gravity heat exchangers are incorporated by reference. According to this variant, on the one hand, the natural gas present in the vapor space in the gaseous state is then pumped by the gravity heat exchanger, and on the other hand, the natural gas cooled by the second heat exchanger is added to the gravity heat exchanger. The gaseous natural gas drawn by the gravity heat exchanger is thus cooled by the natural gas cooled by the second heat exchanger so that it condenses before falling into the vapor space and then enters the tank, thereby reducing the pressure in the vapor space.
The description of the operation of the condensing unit of the second operation mode of the pressure control system according to the first embodiment of the present invention is the same as that just described with reference to the first operation mode, and the description given with reference to fig. 1 and 2 applies to the second operation mode mutatis mutandis.
Fig. 4 and 5 show a pressure control system 100 according to a second embodiment of the invention, these fig. 4 and 5 respectively show a first mode of operation of the pressure control system 100 and a second mode of operation of the pressure control system 100.
The pressure control system 100 according to the second embodiment of the present invention is different from the pressure control system 100 according to the first embodiment in that the first heat exchanger 113 does not have a first passage. Thus, natural gas GN is withdrawn from tank 200 in liquid form by low pressure pump 140 and its pressure is increased by high pressure pump 118 upstream of first heat exchanger 113. However, as previously described, the natural gas GN vaporized by the first heat exchanger 113 must be able to simultaneously supply the first device 210 consuming the low-pressure vaporized gas and the second device 220 consuming the high-pressure vaporized gas.
According to a second embodiment of the invention, the first device 210 and the second device 220 are then supplied by two different branches 211, 221, which are separated downstream of the first heat exchanger 113. Thus, the first branch 211 makes it possible to supply the first device 210, while the second branch 221 makes it possible to supply the second device 220. To supply low pressure vaporized natural gas to the first apparatus 210, the first branch 211 carries an expansion member 212, which expansion member 212 enables the pressure of the vaporized natural gas GN to be reduced to a pressure suitable for the operation of the first apparatus 210.
It should be understood that this is only one exemplary embodiment and that for example two devices consuming the vaporised gas may be provided to consume the low pressure gas, in which case the cold production unit will not have a high pressure pump.
In a similar manner to what has been described, when the device 210, 220 consuming the boil-off gas does not consume all the natural gas effectively evaporated by the first heat exchanger 113, the valve 122 is opened and the low pressure pump 141 of the condensing unit 120 is activated to allow the remaining boil-off gas to condense, allowing it to return into the tank 200 without increasing the pressure of the vapour space 201. As previously mentioned, the heat exchanger 121 is also supplied with vaporized natural gas GN at low pressure. In other words, the condensing unit 120 is connected to the first branch 211 downstream of the expansion member 212, that is to say between this expansion member 212 and the first device 210.
Furthermore, the pressure control system 100 shown in fig. 4 operates according to the first operating mode described and shown in fig. 3, that is to say the second heat exchanger 115 is supplied with natural gas GN taken out in the gaseous state. Accordingly, the description of this first mode of operation given with reference to FIG. 3 may be directly transferred to the pressure control system 100 shown in FIG. 4.
Fig. 5 shows a second mode of operation of the pressure control system 100 according to the second embodiment just described. The description of this second embodiment just given with reference to fig. 4 applies mutatis mutandis to the pressure control system 100 shown in fig. 5.
The description of the second mode of operation of the pressure control system 100 has also been described above and the description given with reference to fig. 3 applies mutatis mutandis to fig. 5.
Fig. 6 shows a pressure control system 100 according to a third embodiment and according to a variant of the second mode of operation.
The variation of the second operation mode shown in fig. 6 differs from the above-described second operation mode in that the low-pressure pump 141, which enables the supply of the heat exchanger 121, is also configured to supply the liquid gas GN to the second heat exchanger 115. Thus, as shown, additional lines 126 extend between lines 125, which allow liquid gas GN taken out of tank 200 to be delivered to heat exchanger 121 and second heat exchanger 115 of condensing unit 120. The additional line 126 comprises at least one valve 127 driven by the control unit 130, the valve 127 being configured to assume at least one open position, in which it allows the passage of the gas GN in the additional line 126, and at least one closed position, in which it inhibits the passage of the gas GN in the additional line 126. Thus, according to this variant of the second operating mode, when the control unit 130 measures that the pressure of the vapour space 201 is too high with respect to the reference value, it sets the valve 127 in its open position, so that the liquid natural gas GN pumped out of the tank by the low-pressure pump 141, which also enables the supply of the condensing unit 120, can be injected into the vapour space 201 by the spray boom 151.
It should be appreciated that this variation of the second mode of operation may be applied to any of the above-described exemplary embodiments operating in accordance with the second mode of operation without departing from the scope of the present invention.
Further, this fig. 6 shows a third embodiment of a pressure control system 100. This third mode of operation differs from the first and second embodiments just described in that the first heat exchanger 113 has no second channels thereof. Thus, natural gas GN is withdrawn from tank 200 in liquid form by low pressure pump 140 and reaches first heat exchanger 113 without undergoing any other pressure changes. The natural gas GN leaves the first heat exchanger 113 in gaseous form and can then be supplied to the first plant 210 which consumes the low pressure boil-off gas. In order to be able to supply the second device 220 consuming high-pressure boil-off gas, the pressure control system 100 according to the third embodiment comprises a third heat exchanger 160, which third heat exchanger 160 is configured to provide heat exchange between the gas GN taken out from the tank 200 in liquid state and the refrigerant FR flowing in the above-mentioned refrigerant FR circuit 111, and to supply the second device 220 consuming gas.
Thus, a first portion FR1 of the refrigerant exiting the compression member 112 is directed to the first heat exchanger 113 as previously described, while a second portion FR2 of the refrigerant exiting the compression member 112 is directed to the third heat exchanger 160. In other words, the third heat exchanger 160 comprises at least one first channel 161 and at least one second channel 162, the liquid natural gas GN coming from the tank 200 circulates in the first channel 161, and the second portion FR2 of the refrigerant compressed by the compression member 112 circulates in the second channel 162. The third heat exchanger 160 is also configured to supply gas to the second device 220 consuming gas, that is to say the gas GN flowing in the first channel 161 of the third heat exchanger must leave the third heat exchanger in gaseous form, which is allowed due to the heat exchange provided in the third heat exchanger 160 with the second portion FR2 of compressed refrigerant, and at high pressure. To allow such a supply of the second device 220 consuming gas, the high pressure pump 118 is arranged upstream of the third heat exchanger 160, more specifically upstream of the first channel 161 of the third heat exchanger 160. In other words, the high pressure pump 118 is disposed between the low pressure pump 140 and the first passage 161 of the third heat exchanger 160, the low pressure pump 140 being disposed in the tank 200 and configured to draw the liquid gas GN from the tank 200.
It should be appreciated that the temperature of the natural gas GN is higher than the temperature of the natural gas GN reaching the first heat exchanger 113 due to the pressure increase that the gas GN experiences before reaching the third heat exchanger 160. In other words, the temperature difference between the gas GN flowing in the third heat exchanger 160 and the second portion FR2 of the refrigerant is lower than the temperature difference between the gas GN flowing in the first heat exchanger 113 and the first portion FR1 of the refrigerant. As a result, the temperature of the second portion FR2 of the refrigerant exiting the third heat exchanger 160 is higher than the temperature of the first portion FR1 of the refrigerant exiting the first heat exchanger 113. Advantageously, according to this third embodiment, the second portion FR2 of the refrigerant leaving the third heat exchanger 160 is reintegrated into the first heat exchanger 113 upstream of the output of this first heat exchanger 113. More specifically, when the first portion FR1 and the second portion FR2 of the refrigerant have similar temperatures, this reintegration makes it possible to mix the two portions again. The second portion FR2 of the refrigerant therefore also releases a portion of its heat to the gas GN circulating in the first heat exchanger 113.
Fig. 7 shows a pressure control system 100 according to a fourth embodiment and a second mode of operation. This fourth embodiment differs from the above-described embodiment in that it allows only the second device 220 consuming gas, that is, the device consuming high-pressure gas, to be supplied. In other words, according to this fourth embodiment, the first heat exchanger 113 does not have its first passage. The first heat exchanger 113 is more specifically configured to provide heat exchange between the gas GN taken out of the tank 200 in a liquid state by the low-pressure pump 140 and then compressed by the high-pressure pump 118 and the refrigerant FR compressed by the compression member 112. More specifically, according to the fourth embodiment, a single refrigerant flowing in the first heat exchanger 113 is pre-compressed by the compression member 112.
This fourth embodiment also differs from the other embodiments previously described in that the refrigerant FR circuit 111 comprises an internal heat exchanger 163, that is to say a heat exchanger configured to provide heat exchange between the two ducts of the refrigerant FR circuit 111. As shown, the internal heat exchanger 163 is more specifically configured to provide heat exchange between the refrigerant FR compressed by the compression member 112 and the refrigerant FR expanded by the expansion device 114. In other words, the internal heat exchanger 163 includes at least one first passage 164 and at least one second passage 165, the refrigerant FR compressed by the compression member 112 circulates in the first passage 164, the refrigerant FR expanded by the expansion device 114 and partially heated by heat exchange with the liquid gas GN taken out of the tank 200 provided in the second heat exchanger 115 circulates in the second passage 165.
As described above, when the amount of the natural gas GN taken out in the liquid and/or gas state is greater than the amount of the evaporated natural gas GN required for the device 210, 220 consuming the evaporated natural gas in the case that the measured pressure value is lower than or equal to the reference value, the control unit 130 opens the valve 122 to allow the condensing unit 120 to condense the excessively evaporated natural gas GN, thereby allowing the condensed natural gas GN to be returned into the tank 200. On the other hand, when the amount of evaporated natural gas GN required by the apparatus 210, 220 consuming the evaporated natural gas is smaller than the amount of natural gas GN to be taken out from the tank 200 to be recovered to the reference pressure, the control unit 130 closes the valve 122, thereby forcing all the natural gas GN evaporated by the first heat exchanger 113 to reach the apparatus 210, 220 consuming the evaporated natural gas. These operating steps are compared to those applicable to the fourth embodiment shown in fig. 4, except that the valve 122 is replaced by an expansion device 122' in order to reduce the pressure of the boil-off gas GN leaving the first heat exchanger 113 at high pressure, that is to say, the pressure of the second plant 220 adapted to supply the consumed gas, which is then sent to the condensing unit 120.
Alternatively, the evaporator 166 may be arranged downstream of the first heat exchanger 113, that is to say between this first heat exchanger 113 and the second device 220 consuming high-pressure gas. Advantageously, such an evaporator 166 can terminate the evaporation started in the first heat exchanger 113, if desired, ensuring that only the gaseous gas GN reaches the second plant 220 consuming the gas. It should be appreciated that the evaporator 166 may also be added to the pressure control system 100 according to any of the foregoing embodiments, as well as upstream of the second gas-consuming device and upstream of the first gas-consuming device, without departing from the scope of the present invention.
Finally, fig. 8 is a cross-sectional view of the vessel 15, showing a natural gas storage tank 200 mounted in a double hull 16 of the vessel 15, formed by a set of at least one primary sealing membrane, one secondary sealing membrane arranged between the primary sealing membrane and the double hull 16 of the vessel 15, and two thermal insulation barriers formed between the primary sealing membrane and the secondary sealing membrane and between the secondary sealing membrane and the double hull 16, respectively.
The loading and/or unloading piping 17 arranged on the upper deck of the ship 15 may be connected to the marine or harbour terminal 18 by means of suitable connectors in order to transfer the liquefied natural gas cargo from the tank 200 or to the tank 200.
Of course, the invention is not limited to the examples just described, but many modifications can be made to these examples without departing from the scope of the invention.
As described above, the present invention clearly achieves the objects set therefor, and makes it possible to propose a system for controlling the pressure in a natural gas tank for a ship. Given that, according to the invention, the variants not described here comprise means according to aspects of the invention, these variants can be implemented without departing from the context of the invention.

Claims (20)

1. A control system (100) for controlling pressure in a tank (200) equipped with a vessel (15), the tank (200) being configured to hold Gas (GN) cargo in a liquid state, and the control system (100) comprising:
at least one cold production unit (110) comprising at least one first heat exchanger (113) configured to evaporate a Gas (GN) received by the first heat exchanger (113) and at least one second heat exchanger (115) configured to cool the Gas (GN) and to regulate a pressure in the tank (200), the first heat exchanger (113) being configured to supply the evaporated Gas (GN) to at least one device (210, 220) consuming the Gas (GN);
At least one condensing unit (120) for condensing the Gas (GN) evaporated by the first heat exchanger (113), and comprising at least one heat exchanger (121) configured to provide a heat exchange between a portion of the Gas (GN) evaporated by the first heat exchanger (113) and the Gas (GN) withdrawn from the tank (200) in liquid state,
characterized in that the cold production unit (110) comprises a refrigerant (FR) circuit (111) on which at least one compression member (112) for compressing the refrigerant (FR), at least the first heat exchanger (113), at least one expansion device (114) and at least the second heat exchanger (115) are arranged.
2. The control system (100) according to claim 1, comprising at least one conduit (119) extending from the output of the second heat exchanger (115) to the interior of the tank (200).
3. The control system (100) according to claim 1 or 2, wherein the Gas (GN) fed to the input of the second heat exchanger (115) is taken out of the vapor space (201) by a compression device (131).
4. The control system (100) according to claim 1 or 2, wherein the tank (200) comprises a boom (151) connected to the output of the second heat exchanger (115).
5. The control system (100) according to claim 1 or 2, comprising at least one passage (123) arranged between the output of the heat exchanger (121) and the bottom of the tank (200).
6. The control system (100) according to claim 5, wherein the Gas (GN) heated by the heat exchanger (121) and the evaporated Gas (GN) cooled by the heat exchanger (121) are mixed and then distributed to the bottom of the tank (200).
7. The control system (100) according to claim 1 or 2, wherein at least one low pressure pump (140) is arranged upstream of the first heat exchanger (113).
8. The control system (100) of claim 7, comprising at least one high pressure pump (118) arranged between the low pressure pump (140) and an input of the first heat exchanger (113).
9. The control system (100) according to claim 8, wherein the first heat exchanger (113) comprises at least one first channel (116) and one second channel (117), the first channel (116) being directly supplied by the low pressure pump (140), the second channel (117) being supplied by the high pressure pump (118) arranged between the low pressure pump (140) and an input of the first heat exchanger (113).
10. The control system (100) according to claim 8, wherein the first heat exchanger (113) is configured to supply two devices (210, 220) consuming Gas (GN), at least one expansion member (212) being arranged between the first heat exchanger (113) and one of the devices (210, 220) consuming evaporating Gas (GN).
11. The control system (100) according to claim 7, wherein the first heat exchanger (113) is configured to be supplied at a first device (210) consuming the evaporation Gas (GN) at a low pressure, the control system (100) comprising at least one third heat exchanger (160) configured to be supplied at a second device (220) consuming the evaporation Gas (GN) at a high pressure, at least one high pressure pump (118) being arranged between the low pressure pump (140) and an input of the third heat exchanger (160), the third heat exchanger (160) being configured to provide a heat exchange between the Gas (GN) withdrawn in liquid form from the tank (200) and the refrigerant (FR) compressed by the compression member (112).
12. The control system (100) according to claim 11, wherein refrigerant (FR) leaving the third heat exchanger (160) is fed into the first heat exchanger (113).
13. The control system (100) according to claim 8, wherein at least one internal heat exchanger (163) is arranged on the refrigerant (FR) circuit (111), the internal heat exchanger (163) comprising at least one first channel (164) and at least one second channel (165), the refrigerant (FR) compressed by the compression member (112) flowing in the first channel (164), the refrigerant (FR) expanded by the expansion device (114) flowing in the second channel (165).
14. The control system (100) according to claim 13, wherein the first heat exchanger (113) is arranged on the refrigerant (FR) circuit (111), between the compression member (112) and the internal heat exchanger (163), and wherein the second heat exchanger (115) is arranged on the refrigerant (FR) circuit (111), between the expansion device (114) and the internal heat exchanger (163).
15. A ship (15) for transporting liquefied Gas (GN) comprising at least one tank (200) for liquefied Gas (GN) cargo, at least one device (210, 220) for consuming boil-off Gas (GN), and at least one control system (100) for controlling the pressure in the tank (200) as claimed in any one of the preceding claims.
16. A system for loading or unloading liquid Gas (GN) in combination with at least one onshore device and at least one vessel (15) for transporting liquid Gas (GN) as claimed in claim 15.
17. A method for managing pressure in a tank (200) equipped with a ship (15), the method implementing a pressure control system (100) according to any one of claims 1 or 2 or 4 to 14, and the method comprising at least the steps of:
withdrawing liquid Gas (GN) from the tank (200);
evaporating a first portion of the liquid Gas (GN) withdrawn from the tank (200) by heat exchange with a refrigerant in the first heat exchanger (113) to supply at least one device (210, 220) consuming the evaporated Gas (GN);
by exchanging heat with the refrigerant (FR) in the second heat exchanger (115), a second part of the liquid Gas (GN) taken out of the tank (200) is cooled and at least a part of the cooled Gas (GN) is injected into the vapor space (201).
18. A method for managing pressure in a tank (200) equipped with a ship (15), the method implementing a pressure control system (100) according to any one of claims 1 to 3 or 5 to 14, and the method comprising at least the steps of:
Withdrawing liquid and gaseous Gases (GN) from the tank (200);
evaporating the liquid Gas (GN) withdrawn from the tank (200) by heat exchange with a refrigerant (FR) in a first heat exchanger (113) to supply at least one device (210, 220) consuming the evaporated Gas (GN);
by exchanging heat with the refrigerant (FR) in the second heat exchanger (115), the gaseous Gas (GN) taken out from the tank (200) is condensed, and the condensed Gas (GN) is injected into the tank (200).
19. The method according to claim 17 or 18, wherein the step of withdrawing the Gas (GN) is preceded by the steps of:
measuring the pressure of the vapor space (201) of the tank (200) and comparing the measured pressure value with a reference value and determining the amount of liquid and/or gaseous gas to be removed from the tank when the measured pressure value is lower than or equal to the reference value;
determining a boil-off gas demand of the at least one device consuming boil-off gas;
wherein, if the amount of liquid and/or gaseous gas to be withdrawn is greater than the amount of boil-off gas required by the at least one device consuming boil-off gas when the measured pressure value is lower than or equal to the reference value, a first portion of the Gas (GN) evaporated by the first heat exchanger (113) is supplied to the at least one device (210, 220) consuming the boil-off Gas (GN), a second portion of the Gas (GN) evaporated by the first heat exchanger (113) is condensed in the heat exchanger (121) by heat exchange with the liquid Gas (GN) withdrawn from the tank (200), and the thus cooled second portion of the boil-off Gas (GN) is mixed with the withdrawn liquid Gas (GN) heated by passing through the heat exchanger (121) and is then re-injected at the bottom of the tank (200).
20. Method for loading or unloading a vessel (15) for transporting Gas (GN) according to claim 15 with liquid Gas (GN).
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PCT/FR2020/050528 WO2020188199A1 (en) 2019-03-15 2020-03-12 System for controlling pressure in a liquefied natural gas vessel

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FR3093785A1 (en) 2020-09-18

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