CN116710725A - Gas supply system for high-pressure and low-pressure gas consumers - Google Patents

Gas supply system for high-pressure and low-pressure gas consumers Download PDF

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Publication number
CN116710725A
CN116710725A CN202280009865.7A CN202280009865A CN116710725A CN 116710725 A CN116710725 A CN 116710725A CN 202280009865 A CN202280009865 A CN 202280009865A CN 116710725 A CN116710725 A CN 116710725A
Authority
CN
China
Prior art keywords
gas
heat exchanger
supply system
tank
return line
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN202280009865.7A
Other languages
Chinese (zh)
Inventor
B·奥恩
R·纳尔梅
J-L·苏厄兹
A·迪乌夫
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gaztransport et Technigaz SA
Original Assignee
Gaztransport et Technigaz SA
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Filing date
Publication date
Application filed by Gaztransport et Technigaz SA filed Critical Gaztransport et Technigaz SA
Publication of CN116710725A publication Critical patent/CN116710725A/en
Pending legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63H—MARINE PROPULSION OR STEERING
    • B63H21/00—Use of propulsion power plant or units on vessels
    • B63H21/38—Apparatus or methods specially adapted for use on marine vessels, for handling power plant or unit liquids, e.g. lubricants, coolants, fuels or the like
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B11/00—Interior subdivision of hulls
    • B63B11/04—Constructional features of bunkers, e.g. structural fuel tanks, or ballast tanks, e.g. with elastic walls
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
    • B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
    • B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
    • B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
    • B63B25/16—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed heat-insulated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B27/00—Arrangement of ship-based loading or unloading equipment for cargo or passengers
    • B63B27/24—Arrangement of ship-based loading or unloading equipment for cargo or passengers of pipe-lines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63J—AUXILIARIES ON VESSELS
    • B63J2/00—Arrangements of ventilation, heating, cooling, or air-conditioning
    • B63J2/12—Heating; Cooling
    • B63J2/14—Heating; Cooling of liquid-freight-carrying tanks
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
    • F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
    • F02M21/0203—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels characterised by the type of gaseous fuel
    • F02M21/0206—Non-hydrocarbon fuels, e.g. hydrogen, ammonia or carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
    • F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
    • F02M21/0203—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels characterised by the type of gaseous fuel
    • F02M21/0209—Hydrocarbon fuels, e.g. methane or acetylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
    • F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
    • F02M21/0218—Details on the gaseous fuel supply system, e.g. tanks, valves, pipes, pumps, rails, injectors or mixers
    • F02M21/0245—High pressure fuel supply systems; Rails; Pumps; Arrangement of valves
    • 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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—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
    • 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
    • F25J1/0275—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
    • 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
    • F17C2225/03—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
    • F17C2225/04—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
    • 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
    • F17C2227/0135—Pumps
    • 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
    • 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
    • F17C2227/0367—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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T70/00—Maritime or waterways transport
    • Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system

Abstract

The invention relates to a gas supply system (1) for a high-pressure gas consumer (4) and a low-pressure gas consumer (5) of a floating structure, the supply system (1) comprising: a first supply circuit (2) for supplying gas to the high-pressure gas consuming device (4) and a second supply circuit (3) for supplying gas to the low-pressure gas consuming device (5); a gas return line (14); a first heat exchanger (6) and a second heat exchanger (7) performing heat exchange between the gas of the first supply circuit (2) and the gas circulating in the return line (14), characterized in that the first supply circuit (2) comprises a main line (40) and a line (41) for bypassing a portion (50) of the main line (40).

Description

Gas supply system for high-pressure and low-pressure gas consumers
Technical Field
The present invention relates to the field of liquid gas storage and/or transport vessels, and more particularly to a gas supply system for a consumer device comprised in such a vessel.
Background
In a journey made by a vessel comprising a tank of liquid gas for consumption and/or delivery to a destination, the vessel is able to use at least a portion of the liquid gas to supply at least one of its engines through a gas supply system. This is the case for vessels equipped with propulsion engines of the ME-GI type. In order to supply this type of engine, the gas must be compressed to very high pressure by a special compressor capable of compressing the gas to 300 bar, but this compressor is expensive, adds considerable maintenance costs and causes vibrations inside the ship.
An alternative to installing these high pressure compressors is to evaporate the liquid gas at a pressure of 300 bar before delivering the gas to the propulsion engine. This operation may be performed by a high pressure evaporator. This solution makes it impossible to eliminate the gas in vapor form (or BOG, representing "boil-off gas") that naturally develops in the tank at least partially containing the cargo, and a low-pressure compressor may be installed in order to supply an auxiliary engine capable of consuming the gas in vapor form at low pressure. On the other hand, in this configuration, if the gas in vapor form is present in an amount too large, or more generally in an amount greater than that required for consumption by the auxiliary engine, the gas in vapor form not consumed by the auxiliary engine accumulates in a tank in pressure form within certain limits and is then eliminated by combustion, or as a final means by release thereof into the atmosphere. This type of elimination causes waste of fuel and harmful consequences to the environment.
In order to continuously improve the performance of such a supply system, it is an object to avoid wasting fuel while saving energy for certain components of the supply system.
Disclosure of Invention
The present invention may eliminate such losses by proposing a gas supply system for at least one high pressure gas consumer and at least one low pressure gas consumer of a floating structure, the supply system comprising at least one tank configured to contain gas, the supply system comprising:
at least a first gas supply circuit of the high pressure gas consumer comprising at least one pump configured to pump collected liquid gas into the tank,
at least one high pressure evaporator configured to evaporate gas flowing in the first gas supply circuit,
at least one second circuit for supplying gas to the low-pressure gas consuming device, comprising at least one compressor configured to compress the gas extracted in vapor state in the tank to a pressure compatible with the requirements of the low-pressure gas consuming device,
at least one gas return line connected to the second supply circuit downstream of the compressor and extending to the tank,
at least one first heat exchanger and a second heat exchanger, each configured to exchange heat between the gas flowing in the return line and the gas flowing in the first supply loop,
wherein the first supply circuit comprises a main path and a bypass path arranged in parallel with at least a portion of the main path, the second heat exchanger being configured to exchange heat between gas flowing in the return line and gas flowing in the bypass path.
The presence of the bypass path thus makes it possible to circulate the gas through the second heat exchanger only when necessary, for example in case of an excess of gaseous gas present in the tank. The gas may also circulate throughout the main path, including a portion of the main path arranged in parallel with the bypass path, and be directly treated by the high pressure evaporator after having passed through the first heat exchanger. Thus, the gas collected in the tank and intended to be supplied to the high pressure gas consuming device has several flow patterns, which prevents the flow of surplus gas and may also limit the amount of energy associated with the use of the high pressure evaporator and/or the second heat exchanger.
Furthermore, with such a supply system, the gaseous gas present in the tank and not used for consumption by the low-pressure gas consuming device can be recondensed and thus returned to the tank in liquid state, instead of being eliminated. Thus, at least the loss of excess gas in the vapor state present in the tank is reduced.
Thus, the first gas supply circuit makes it possible to meet the fuel requirements of the high-pressure gas consuming device. The apparatus may for example be a device for propelling a floating structure, such as an ME-GI engine. The first supply circuit extends from the tank to the high pressure gas consuming device. The pump is mounted at the bottom of the tank and ensures the pumping of the liquid gas so that it can circulate in the first supply circuit.
Since the gas must be in a vapor state to be supplied to the high-pressure gas consuming apparatus, the high-pressure vaporizer ensures that the gas is vaporized before being supplied to the high-pressure gas consuming apparatus. The high-pressure evaporator is a place where heat exchange is performed between the gas flowing in the first supply circuit and a heat transfer fluid (e.g., glycol water, seawater, or steam). Such heat transfer fluids must be at a sufficiently high temperature to produce a change in gas state to enter a vapor or supercritical state and be supplied to the high pressure gas consuming device.
The gas circulated in the first supply circuit passes through the first heat exchanger and then, optionally, the second heat exchanger, depending on the chosen configuration. The gas may then be vaporized by a high pressure vaporizer. Thus, if the configuration of the first supply circuit allows, the temperature of the gas will rise before it passes through the high pressure evaporator. Thus, if the gas takes a bypass path, the gas flowing in the first supply circuit may be in a two-phase, vapor, liquid or supercritical state at the outlet of the second heat exchanger.
In general, the gas contained in the tank may naturally become in a vapor state or be forced into a vapor state by the floating structure. In order to avoid the occurrence of overpressure in the tank, the gas in the tank that becomes in the vapor state must be vented.
This function is provided by the second gas supply circuit of the low-pressure gas consumer. The second supply circuit extends from the tank to the low pressure gas consumer. The device may be, for example, an auxiliary motor, such as a generator. The compressor arranged on the second supply circuit is responsible for extracting the gas present in the tank space in order to be able to supply both the low-pressure gas consuming device and to regulate the pressure in the tank. The second supply circuit is structurally separate from the first supply circuit, except for the fact that both supply circuits are connected to the tank.
At the outlet of the compressor, the gas in vapor state may be supplied to the low-pressure gas consuming device or circulated through the return line if the low-pressure gas consuming device does not require fuel intake. Since the return line is connected downstream of the compressor, the gas in vapor state, which is sucked in by the compressor, can circulate therein.
The gas in vapor state flowing in the return line passes first through the second heat exchanger and then through the first heat exchanger before being returned to the tank. Depending on the circulation of the gas in the first supply circuit, the heat exchange may take place in both heat exchangers or only in the first heat exchanger.
As a result of the heat exchange between the gas flowing in the first supply circuit and the gas flowing in the return line, the temperature of the gaseous gas is reduced by flowing through both heat exchangers until said gas condenses and returns substantially to the liquid state upon leaving the first heat exchanger. The recondensed gas is then passed to a tank.
According to one feature of the invention, the main path comprises an additional pump located between the first heat exchanger and the high pressure evaporator. It is the additional pump that makes it possible to increase the pressure of the gas circulated in the first supply circuit so that it has a compatible pressure for supplying the high-pressure gas consumer.
The positioning of the additional pump is particularly advantageous. In practice, the placement of an additional pump upstream of the first heat exchanger causes the pressure and temperature of the liquid gas to rise as it passes through the first heat exchanger, which is detrimental to the condensation of the gaseous gas flowing in the return line and passing through the first heat exchanger. Thus, the optimal arrangement consists in placing an additional pump downstream of the first heat exchanger.
According to one feature of the invention, the bypass path starts at a split point provided on the main path, the split point being located between the additional pump and the high pressure evaporator. From the tapping point, the first supply circuit is split between a portion of the main path and the bypass path. Depending on the configuration of the first supply circuit, the gas circulated therein may be circulated in a portion of the main path after having passed through the first heat exchanger, for subsequent direct treatment by the high pressure evaporator, and/or in a bypass path for passing through the second heat exchanger.
The tapping point is located downstream of the additional pump, and thus the second heat exchanger is also located downstream of the additional pump. In particular, the gas circulating in the bypass path may be in a vapour, liquid, two-phase or supercritical state at the outlet of the second heat exchanger, and the placement of an additional pump downstream of the second heat exchanger may adversely affect its correct operation, since the additional pump only allows pumping of fluid in the liquid state.
According to one feature of the invention, the first supply circuit comprises a distribution device configured to control the distribution of the gas towards the portion of the main path and/or the circulation of the bypass path. The distribution device may be remotely controlled such that the gas circulation within the first supply circuit is optimal for the gas consumption by the consumer and the condensation of the gas circulating in the return line.
According to one feature of the invention, the bypass path ends at a convergence point provided between the split point and the high pressure evaporator on the main path. This configuration corresponds to the first embodiment of the supply system according to the invention. In this first embodiment, the portion of the main path and the convergence point of the bypass path are arranged downstream of the split point and upstream of the high pressure evaporator. In other words, the gas flowing in the bypass path passes through the second heat exchanger and then is added to the main path before being treated by the high pressure evaporator. Therefore, all the gas flowing in the first supply circuit is treated by the high-pressure evaporator according to the first embodiment. The latter thus allows the gas to pass through the second heat exchanger and/or bypass it.
According to one feature of the invention, the dispensing device comprises a first valve configured to manage the passage of gas in the bypass path and a second valve arranged in said portion of the main path. The valves may be remotely controlled to switch to an open or closed position to determine the flow of gas through the first supply circuit.
The first valve may be disposed in the bypass path upstream or downstream of the second heat exchanger. As for the second valve, it is arranged in a portion of the main path arranged in parallel with the bypass path.
The first valve makes it possible to control the flow of gas in the bypass path, while the second valve makes it possible to control the flow of gas in the portion of the main path arranged in parallel with the bypass path. If the first valve is closed and the second valve is open, gas circulates throughout the main path. If the first valve is open and the second valve is closed, the gas is circulated entirely through the bypass flow and then the main path is added upstream of the high pressure evaporator. The two valves may also be opened so that the gas is divided into two parts, one part directly entering the high-pressure evaporator via said part of the main path and the other part being circulated in the bypass path via the second heat exchanger.
According to one feature of the invention, the bypass path and the first valve are configured to maintain the gas flowing between the tapping point and the second heat exchanger in a liquid state. In other words, the only function of the first valve is to allow or prevent the gas to circulate in the bypass path without causing any change of state, for example by expanding the gas circulating in the bypass path. The gas flowing in the bypass path thus remains in a liquid state until it passes through the second heat exchanger. At the outlet of the second heat exchanger, the gas circulated in the bypass path may be discharged from the second heat exchanger in a liquid, vapor, two-phase or supercritical state, depending on the flow rate of the gas circulated in the return line and its influence on heat exchange.
According to one feature of the invention, the bypass path ends at a convergence point arranged downstream of the high-pressure evaporator on the main path. This configuration corresponds to the second embodiment of the supply system according to the invention. In this embodiment, the bypass path makes it possible to bypass the high pressure evaporator. The latter is thus located in the portion of the main path that is arranged in parallel with the bypass path.
According to a second embodiment, the gas flowing in the first supply circuit is treated by the high pressure evaporator if the gas flows in said portion of the main path and by the second heat exchanger if the gas flows in the bypass path. At the outlet of the high pressure evaporator or the second heat exchanger, the gas has characteristics suitable for consumption by high pressure gas consuming equipment, for example in a steam or supercritical state. The second embodiment thus makes it possible to distribute the state-changing load of the gas flowing in the first supply circuit while cooling the gas flowing in the return line by means of heat exchange in the second heat exchanger.
According to one feature of the invention, the dispensing device comprises a dispensing valve. The distribution valve makes it possible to control the flow of gas circulating in said portion of the main path and/or the bypass path. For example, the valve may have a degree of opening, the distribution of the gas flowing between said part of the main path and/or the bypass path being dependent on the degree of opening of the distribution valve.
According to one feature of the invention, a distribution valve is arranged in said portion of the main path. In this configuration, the greater the opening degree of the distribution valve, the greater the proportion of gas flowing in the main path portion. Conversely, the smaller the opening degree of the distribution valve, the greater the proportion of gas flowing through the bypass path. If the distribution valve is fully open, gas circulates only in said part of the main path. If the distribution valve is closed, the gas circulates only in the bypass path. The distribution valve may be located between the split point and the high pressure evaporator or between the high pressure evaporator and the convergence point.
According to another feature of the invention, the distribution valve is arranged on the bypass path. In this configuration, the greater the opening degree of the distribution valve, the greater the proportion of the gas flowing in the bypass path. Conversely, the smaller the opening of the distribution valve, the greater the proportion of gas circulating in said portion of the main path. If the dispensing valve is fully open, gas is circulated only in the bypass path. If the distribution valve is closed, the gas circulates only in said portion of the main path. The distribution valve may be located between the split point and the second heat exchanger or between the second heat exchanger and the convergence point.
According to one feature of the invention, the return line comprises an expansion member arranged between the first heat exchanger and the tank, the expansion member being configured to regulate the flow of the gas circulating in the return line, the expansion member and the distribution valve being configured to cause the gas circulating in the bypass path to change from a liquid state to a gaseous or supercritical state.
As described above, the gas flowing in the first supply circuit is treated by the high-pressure evaporator or the second heat exchanger. In other words, unlike the first embodiment, the gas circulated in the bypass path must be in a state suitable for consumption by the high-pressure gas consuming apparatus, for example, in a steam or supercritical state, at the outlet of the second heat exchanger. It is therefore important that the gas flowing in the bypass path is entirely in a vapour or supercritical state at the outlet of the second heat exchanger.
The flow rate of the gas flowing in the bypass path may be proportional to the flow rate of the gas flowing in the return line, so that during heat exchange all the gas flowing in the bypass path is in a vapour or supercritical state at the outlet of the second heat exchanger. Thus, the expansion member arranged on the return line makes it possible to control the flow rate of the gas flowing in the return line, while the distribution valve makes it possible to control the flow rate of the gas flowing in the bypass path. Thus, by means of the control by the expansion member and the distribution valve, the gas flowing in the bypass path leaves the second heat exchanger in a state adapted to the consumption thereof by the high-pressure gas consuming apparatus without being treated by the high-pressure evaporator.
According to one feature of the invention, the first heat exchanger is configured to condense the gas circulating in the return duct. The first heat exchanger is an exchanger through which the liquid gas of the first supply circuit passes when it is at its lowest temperature. The heat exchange taking place in the first heat exchanger will thus change the state of the gas flowing in the return line, thereby changing it from gaseous to liquid.
According to one feature of the invention, the second heat exchanger is configured to pre-cool the gas circulating in the return line. At the outlet of the first heat exchanger, the gas flowing in the first supply circuit is not as cold as at the inlet of the first heat exchanger, heat exchange having been used to condense the gas flowing in the return line. The liquid gas is then compressed by the additional pump and then reaches the tapping point. Depending on the configuration of the first or second embodiment, the gas may then pass through the second heat exchanger. If so, there is also a heat exchange in the second heat exchanger, allowing pre-cooling of the gaseous gas in the return line.
According to one feature of the invention, the return line may comprise a split-flow zone dividing the return line into a first section and a second section, both extending from the split-flow zone to the tank, the first heat exchanger being configured to exchange heat between gas circulating in gaseous form in the first section of the return line and gas circulating in liquid form in the first supply circuit, while the second section bypasses the first heat exchanger. The gaseous gases present in the tank and not used for consumption by the low-pressure gas consuming device can be condensed by circulation through the first section of the return line and thus returned to the storage tank in liquid state, instead of being eliminated.
When the flow of liquid gas flowing in the first supply circuit is insufficient to condense all gaseous gas flowing in the return line, an excess portion of the gas may be directed to the second section of the return line for direct return to the tank. This occurs when a floating structure equipped with a supply system according to the invention does not require a large amount of liquid gas for propulsion, for example when the floating structure is moving at a reduced speed.
The inventors have determined that the gaseous gas flowing in the return line can be completely condensed only when the amount of liquid gas flowing in the first supply circuit is greater than or equal to six times the amount of gaseous gas flowing in the return line. Such an example is applicable when the compressor compresses gaseous gas to about 10 bar, but the ratio may vary depending on the pressure delivered by the compressor. If this condition is met, the gaseous gas circulates in the first section of the return line so as to be condensed. If the quantity of liquid gas flowing in the first supply circuit is less than six times the quantity of gaseous gas flowing in the return line, it is advantageous to at least partially ventilate the gaseous gas in the second section of the return line and then to pass a portion of the gaseous gas in the first section in such a quantity that the condensation is complete.
The gaseous gas flowing in the return line can flow in the first or second section starting from the split point. As mentioned above, if the gaseous gas flows through in the first stage, it first passes through the second heat exchanger and then through the first heat exchanger before returning to the tank. If the gaseous gas is circulated in the second stage, it passes through the second exchanger and then returns directly to the tank. According to this configuration, the temperature of the gaseous gas is reduced due to the heat exchange performed in the second heat exchanger, however it is not condensed. Thus, the gas returns to the tank in a vapor state, but is still cooled.
Thus, the second section of the return line comprises an end immersed in the liquid contained in the tank. The second section may comprise a spray member arranged at the submerged end. The injection means make it possible, in particular, to expand the gaseous gas flowing in the second section of the return line before it is dispersed into the tank. The expansion of the gaseous gas is associated with the fact that the submerged end is preferably arranged at the bottom of the tank, so that at least part of the gaseous gas may liquefy when it is returned to the tank, also resulting in an increase in the temperature of the liquid gas present in the tank. The spraying means may be, for example, a sprayer or a frothing device.
According to one feature of the invention, the supply system comprises an auxiliary supply line connected to the first supply circuit upstream of the first heat exchanger and extending to the second supply circuit downstream of the compressor, the supply system comprising a low pressure evaporator configured to evaporate the gas circulating in the auxiliary supply line. Such auxiliary supply lines are used when the low-pressure gas consuming device needs to be supplied with gaseous gas, but not in sufficient quantity in the tank space. The auxiliary supply line thus enables a portion of the liquid gas flowing in the first supply circuit to be led out. Then, according to the operation similar to the high-pressure evaporator, this portion is evaporated by the low-pressure evaporator, that is, by heat exchange with a heat transfer fluid such as ethylene glycol water, sea water or water vapor. The low pressure evaporator thus causes a heat exchange between the liquid gas flowing in the auxiliary supply line and the heat transfer fluid.
Once in the vapor state, the gas circulates in the auxiliary supply line and then joins the second supply circuit to supply the low pressure gas consuming device.
If a sufficient amount of gaseous gas is present in the tank space, the auxiliary supply line is not used, and may be closed, for example, by a valve.
The invention also includes a floating structure for storing and/or transporting liquid gas comprising at least one tank containing liquid gas, at least one high pressure gas consuming device, at least one low pressure gas consuming device and at least one gas supply system for supplying gas to these devices.
The invention also includes a liquefied gas loading or unloading system incorporating at least one land and/or port facility and at least one floating structure for storing and/or transporting liquefied gas.
Finally, the invention comprises a method of loading or unloading liquid gas from a floating structure for storing and/or transporting gas, wherein a pipe for loading and/or unloading liquid gas arranged on the upper deck of the floating structure can be connected to a marine terminal or port terminal by means of a suitable connector for transporting liquid gas out of or to a tank.
Drawings
Other features and advantages of the invention will appear from the following description and from the several exemplary embodiments, given for illustrative purposes and not limited to the accompanying schematic drawings in which:
FIG. 1 shows a first embodiment of a supply system according to the present invention;
FIG. 2 shows a first embodiment of a feed system comprising a return line divided into two sections;
FIG. 3 shows a second embodiment of a supply system;
figure 4 is a schematic cross-sectional view of a tank of a floating structure and a quay for loading and/or unloading the tank.
Detailed Description
Fig. 1 to 3 show a gas supply system 1 arranged on a floating structure. The supply system 1 makes it possible to flow gas in liquid, vapor, two-phase or supercritical state from the storage and/or transport tank 8 to the high-pressure gas consumer 4 and/or the low-pressure gas consumer 5 in order to supply said devices with fuel.
The floating structure may be, for example, a vessel that can store and/or transport liquid gas. In this case, the supply system 1 is able to supply the high-pressure gas consuming device 4, which may be for example a propulsion engine, and the low-pressure gas consuming device 5, which may be for example a generator powering the floating structure, with liquid gas stored and/or transported by the floating structure.
In order to ensure that the gas contained in the tank 8 is circulated to the high-pressure gas consumer 4, the supply system 1 is provided with a first gas supply circuit 2. The first supply circuit 2 comprises a pump 9 arranged in a tank 8. The pump 9 enables the liquid gas to be pumped and circulated in particular in the first supply circuit 2. By pumping the liquid gas, the pump 9 increases its pressure to a value between 6 and 17 bar.
The first supply circuit 2 comprises a main path 40 and a bypass path 41. The main path 40 extends from the pump 9 to the high-pressure gas consumer 4. As for the bypass path 41, it is arranged in parallel with a portion 50 of the main path 40. Therefore, the gas flowing in the first supply circuit 2 may flow through the portion 50 of the main path 40 or through the bypass path 41.
The gas flowing in the first supply circuit 2 flows in the main path 40 in the flow direction from the tank 8 to the high-pressure gas consumer 4, is pumped by the additional pump 10 through the first heat exchanger 6 and reaches the diversion point 42 so as to flow in the portion 50 of the main path 40 or the bypass path 41. The control of the gas flow in the portion 50 of the main path 40 and/or in the bypass path 41 is managed by a distribution device 60, the distribution device 60 ensuring that the gas is distributed according to factors and/or requirements which will be described in detail below. If the gas circulates in the bypass path 41, the gas passes through the second heat exchanger 7. Details regarding the two heat exchangers 6, 7 will be described below. The bypass path 41 comprises a first portion 41a extending between the split point 42 and the second heat exchanger 7, and a second portion 41b extending between the second heat exchanger 7 and the convergence point 43.
Both the portion 50 of the main path 40 and the bypass path 41 extend from the diversion point 42 to the convergence point 43. From there, the gas flows again to the high-pressure evaporator 11 in the main path 40. The high-pressure evaporator 11 makes it possible to change the state of the gas flowing in the first supply circuit 2 so as to change it into a vapor state. This state allows the gas to be compatible with the supply of the high pressure gas consuming device 4, for example by being in a steam or supercritical state. The evaporation of the liquid gas may be performed, for example, by heat exchange with a heat transfer fluid at a sufficiently high temperature to evaporate the liquid gas, in this case ethylene glycol water, sea water or water vapour.
When pumping liquid gas, an increase in gas pressure is ensured by the additional pump 10. The additional pump can increase the pressure of the liquid gas to a value between 30 and 400 bar, in particular for ammonia or hydrogen; when used for liquefied petroleum gas, can be increased to a value between 30 and 70 bar; for ethane, ethylene or liquefied natural gas consisting mainly of methane, it can be increased to values between 150 and 400 bar.
By means of the combination of the additional pump 10 and the high-pressure evaporator 11, the gas is in a pressure and compatible state for the supply of the high-pressure consumer 4. This configuration makes it possible to avoid the installation of a high-pressure compressor on the first supply circuit 2, which has cost constraints and generates strong vibrations.
To determine the gas flow configuration within the first gas supply circuit 2, the distribution device 60 comprises a first valve 44 arranged on the bypass path 41 and a second valve 45 arranged on the portion 50 of the main path 40. Thus, depending on whether the two valves 44, 45 are open or closed, gas flows from the split point 42 to the convergence point 43 via the portion 50 or via the bypass path 41 as desired. These valves may be remotely controlled according to the desired flow pattern.
In fig. 1, the first valve 44 is provided at the first portion 41a of the bypass path 41. Alternatively, the first valve 44 may also be arranged on the second portion 41b of the bypass path 41.
In the tank 8, part of the gas cargo may naturally be converted into a vapor state and spread into the space of the tank 12. In order to avoid overpressure in the tank 8, the vapour phase gas contained in the tank space 12 has to be vented. However, the first supply circuit 2 is configured to supply the high-pressure gas consuming device 4 with liquid gas.
The supply system 1 thus comprises a second gas supply circuit 3 which supplies a low-pressure gas consumer 5 with a vapour state gas. The second supply circuit 3 extends between the tank space 12 and the low-pressure gas consumer 5. The first supply circuit 2 and the second supply circuit 3 are structurally separate from each other, except for being connected to the tank 8. For sucking in the gas in the vapor state contained in the tank space 12, the second supply circuit 3 comprises a compressor 13. In addition to the intake of gaseous gas, the compressor 13 also enables the gaseous gas flowing in the second supply circuit 3 to be compressed to a pressure of 6 to 20 bar absolute, so that the gaseous gas is at a compatible pressure for supplying the low-pressure gas consuming device 5. The second supply circuit 3 thus makes it possible to supply the low-pressure gas consuming device 5 while the pressure in the tank 8 is regulated by sucking in the gas in the vapor state present in the tank space 12.
The presence of excess vapor state gas in tank space 12 results in an overpressure in tank 8. Therefore, in order to reduce the pressure in the tank 8, it is necessary to discharge the gaseous gas. Excess vapor state gas may then be eliminated, for example, by the burner 18. However, the supply system 1 according to the invention comprises a return line 14 extending from the second supply circuit 3 to the tank 8.
The return line 14 is connected to the second supply circuit 3 downstream of the compressor 13 with respect to the flow direction of the vapor state gas flowing in the second supply circuit 3. Depending on the direction of flow of the gaseous gas flowing in the return line 14, said gas passes in a first step through the second heat exchanger 7 and then through the first heat exchanger 6. Therefore, the heat exchange performed in the first heat exchanger 6 and the second heat exchanger 7 is performed between the gas flowing in the first supply circuit 2 and the gas flowing in the return line 14. More specifically, the heat exchange performed in the second heat exchanger 7 is performed between the gas flowing through the bypass path 41 and the gas flowing through the return line 14. The purpose of this heat exchange via the second heat exchanger 7 and then via the first heat exchanger 6 is to condense the gaseous gas in the return line 14 so that it is converted into a liquid state and returned to the tank 8 in this state, instead of being eliminated by the burner 18.
The inlet of the first heat exchanger 6 is where the liquid gas in the first supply circuit 2 has the lowest temperature. Thus, after having passed through the first heat exchanger 6, the gas flowing in the return line 14 is condensed. The gas in the return line 14 is thus in a vapour state at the inlet of the first heat exchanger 6 and leaves in liquid state after heat exchange has taken place in the first heat exchanger 6.
In order to match the pressure 14 of the gas flowing in the return line with the pressure in the tank 8, the return line 14 may comprise an expansion member 15 which may reduce the gas pressure to 1 to 3 bar absolute. The expansion member 15 is also capable of adjusting the flow rate of the gas flowing in the return line 14. Once the gas is condensed, it is passed to tank 8. Thus, the first heat exchanger 6 acts as a condenser.
The second heat exchanger 7 is located downstream of the first heat exchanger 6 in the gas flow direction in the first supply circuit 2 and upstream of the first heat exchanger 6 in the gas flow direction in the return line 14. The second heat exchanger 7 thus ensures pre-cooling of the gaseous gas flowing in the return line 14 before the gas condenses in the first heat exchanger 6, provided that the gas flowing in the first supply circuit 2 passes through the bypass path 41. At the bypass path 41, the gas at the inlet of the second heat exchanger 7 has previously passed through the first heat exchanger 6 and has been pumped by the additional pump 10, which thus increases its temperature and pressure. Therefore, after the heat exchange in the second heat exchanger 7, the gas flowing in the first supply circuit 2 may leave the second heat exchanger 7 in a liquid, vapor, two-phase or supercritical state. Thus, the temperature of the gas flowing in the return line 14 is reduced after passing through the second heat exchanger 7, achieving the above-mentioned pre-cooling.
If at least the first valve 44 is closed, the gas will not circulate in the bypass path 41 and the gas circulating in the return line 14 will pass the second heat exchanger 7 without pre-cooling therein. The passage of gas through the portion 50 of the main path 40 may also be preferred when there is no condensation of the gas flowing in the return line 14. However, the heat exchange performed within the second heat exchanger 7 makes it possible to increase the temperature of the gas flowing in the bypass path 41, and thus makes it possible to limit the energy that must be supplied to the heat transfer fluid flowing in the high-pressure evaporator 11 in order to evaporate the gas that has previously passed through the second heat exchanger 7.
If the gas flows via the bypass path 41, the additional pump 10 is advantageously arranged downstream of the first heat exchanger 6 and upstream of the second heat exchanger 7. By means of the expansion member 15, the regulation of the flow rate of the gas flowing in the return line 14 ensures that the gas flowing in the first supply circuit 2 and passing through the first heat exchanger 6 remains liquid at the outlet of the first heat exchanger 6. The additional pump 10 then sucks in the gas which remains in the liquid state without the risk of being damaged by at least a part of the gaseous gas.
Furthermore, the presence of the additional pump 10 downstream of the first heat exchanger 6 ensures an increase in the pressure of the liquid gas without interfering with the heat exchange taking place in the first heat exchanger 6. Thus, the condensation of the gaseous gas flowing in the return line 14 is optimally performed.
The supply system 1 further comprises an auxiliary supply line 16, the auxiliary supply line 16 extending from the first supply circuit 2 to the second supply circuit 3 via a tap between the pump 9 and the first heat exchanger 6, being connected to the second supply circuit 3 between the compressor 13 and the low-pressure gas consumer 5. The auxiliary supply line 16 makes it possible to power the low-pressure gas consumer 5 in the event of insufficient gas flow in the vapor state formed in the tank space 12.
When the amount of gas in the vapor state present in the tank space 12 is insufficient, the liquid gas pumped by the pump 9 can circulate in this auxiliary supply line 16 for supplying the low-pressure gas consuming apparatus 5. For this purpose, the auxiliary supply line 16 passes through the low-pressure evaporator 17, so that the liquid gas flowing in the auxiliary supply line 16 becomes a vapor state. The operation of the low pressure evaporator 17 may for example be the same as the operation of the high pressure evaporator 11, i.e. the gas is evaporated by heat exchange with a heat transfer fluid at a sufficiently high temperature to evaporate the liquid gas. At the outlet of the low-pressure evaporator 17, the gas in vapor state circulates in the auxiliary supply line 16 and then joins the second supply circuit 3 in order to supply the low-pressure gas consumer 5.
From the above, it follows that the auxiliary supply line 16 is only used when there is not enough vapor state gas in the tank space 12. Thus, the auxiliary supply line 16 includes a valve 19, the valve 19 controlling the flow of gas in the auxiliary supply line 16 when the use of gas in the auxiliary supply line 16 is not required.
Fig. 2 shows a first embodiment of the feed system 1, the return line 14 of which is divided into two separate sections. The return line 14 thus comprises a main section 56, which main section 56 starts at the connection with the second supply circuit 3 and extends to the diversion zone 53. At the splitting zone 53, the return line 14 is divided into a first section 51 and a second section 52, both sections extending from the splitting zone 53 to the tank 8.
The split area 53 is arranged downstream of the second heat exchanger 7. Thus, the main section 56 of the return line 14 passes through the second heat exchanger 7.
At the outlet of the second heat exchanger 7, the gaseous gas is circulated to the splitting area 53 and may then be circulated in the first section 51 or the second section 52. The first section 51 passes through the first heat exchanger 6, while the second section 52 extends to the tank 8 by bypassing the first heat exchanger 6. In other words, the gaseous gas may circulate in the first section 51 and be condensed due to the heat exchange occurring in the first heat exchanger 6, or it may circulate in the second section 52 and be returned to the tank 8 in gaseous state.
The choice of the section in which the gaseous gas circulates depends inter alia on the flow rate of the liquid gas circulating in the first supply circuit 2, which must be sufficient to completely condense the gaseous gas circulating in the return line 14. Thus, when the amount of liquid gas flowing in the first supply circuit is greater than or equal to six times the amount of gaseous gas flowing in the return line, gaseous gas can be directed to the first section 51, so that condensation thereof can be achieved.
If the quantity of liquid gas flowing in the first supply circuit is less than six times the quantity of gaseous gas flowing in the return line, the quantity of the first portion of gaseous gas flowing in the first section 51 is such that it is completely condensed in the first exchanger 6, while the second portion of gaseous gas corresponding to the quantity of gaseous gas not flowing in the first section 51 is flowing in the second section 52, so as to be returned directly to the tank 8. With little or no liquid gas flowing in the first supply circuit 2, all gaseous gas is then circulated in the second section 52 to return directly to the tank 8 to avoid pressure drops due to passage through the first heat exchanger 6. In this case, the gas is returned to the tank 8 in a vapor state. This situation occurs when liquid gas is rarely used for supplying the high-pressure gas consuming apparatus 4.
To regulate the flow in the return line 14, an expansion member 15 is arranged at the first section 51 downstream of the first heat exchanger 6, while the second section 52 comprises a flow regulating member 54. The expansion member 15 and the flow regulating member 54 may also provide the function of expanding the gas flowing in either segment.
Advantageously, the gas flowing in it is returned to the bottom of the tank 8, or at least to the zone where the gas is liquid, both for the first section 51 and for the second section 52. More specifically, the gas flowing in the vapor state in the second section 52 is returned to the bottom of the tank in the vapor state. Thus, the temperature and density of the liquid gas present in tank 8 are such that gaseous gas leaving second section 52 can be condensed. To facilitate such condensation of the gaseous gas, the second section 52 may comprise a spray member 55, which spray member 55 is arranged at one end of the second section 52 immersed in the liquid content of the tank 8. The injection member 55 allows to expand the gaseous gas circulating in the second section 52 in order to facilitate its condensation in the tank 8. The spray member 55 may be, for example, a sprayer or a frothing device. The return of gaseous gas to tank 8 via second section 52 causes the temperature of the liquid gas present in tank 8 to rise.
Since undescribed features of the supply system 1 shown in fig. 2 are the same as those of the supply system 1 shown in fig. 1, a description of elements common to both embodiments will be made with reference to the description of fig. 1.
Fig. 3 shows a second embodiment of a supply system 1 according to the invention. The second embodiment differs from the first embodiment in the configuration of the main path 40 and the bypass path 41. Thus, for those concepts common to both embodiments, reference will be made to the description of fig. 1 and 2.
According to a second embodiment of the supply system 1, in this case the convergence point 43 is arranged downstream of the high-pressure evaporator 11. In other words, the bypass path still comprising the second heat exchanger 7 is configured to bypass the high pressure evaporator 11. The latter is thus arranged within the portion 50 of the main path 40. Therefore, if the gas circulates in the bypass path 41, it reaches the convergence point 43 and then flows to the high-pressure gas consuming apparatus 4 without being treated by the high-pressure evaporator 11. If the first supply circuit 2 is configured such that the gas circulates entirely within the main path 40, it is directly treated by the high-pressure evaporator 11 by circulating within the portion 50 after having passed through the first heat exchanger 6 and the additional pump 10.
According to a second embodiment, the dispensing device 60 comprises a dispensing valve 47 arranged in the first portion 41a of the bypass path 41. Alternatively, the distribution valve 47 may be arranged in the second portion 41b of the bypass path 41, or on the portion 50 of the main path 40, between the split point 42 and the high pressure evaporator 11 or between the high pressure evaporator 11 and the convergence point 43.
The distribution of the gas flowing through the portion 50 of the main path 40 and/or the bypass path 41 is performed according to the opening degree of the distribution valve 47.
In fig. 3, a distribution valve 47 is provided on the bypass path 41. Accordingly, the greater the opening degree of the distribution valve 47, the greater the proportion of the gas flowing through the bypass path 41. By controlling the degree of opening of the distribution valve 47, the distribution of gas in the portion 50 of the main path 40 and/or the bypass path 41 can thus be managed.
Since the gas flowing through the bypass path 41 is not treated by the high pressure evaporator 11, the characteristics of the gas after having passed through the second heat exchanger 7 must be adapted to its use as fuel for the high pressure gas consuming device 4, for example by corresponding to a steam or supercritical state. The distribution valve 47 is thus controlled so as to allow a quantity of gas to circulate in the bypass path 41, so that the heat exchange taking place in the second heat exchanger 7 is sufficient to convert all said quantity of gas into a vapour or supercritical state for compatibility with the high-pressure gas consuming apparatus 4. The expansion member 15 of the return line 14 can also influence this situation by controlling the flow of gas flowing in the return line 14.
Similar to the first embodiment, the gas flowing in the return line 14 is pre-cooled in the second heat exchanger 7, provided that at least a part of the gas flowing in the first supply circuit 2 passes through the bypass path 41.
Advantageously, the second embodiment allows the evaporation of the gas circulating in the first supply circuit 2 to be distributed between the portion 50 passing through the high-pressure evaporator 11 and the bypass path 41 passing through the second heat exchanger 7. This parallel evaporation makes it possible to limit the activity of the high-pressure evaporator 11 and thus to partially save the energy required for its operation when all the gases circulating in the first supply circuit 2 are treated by the high-pressure evaporator 11.
When no gas flowing in the return line 14 is condensed and no heat exchange takes place in the second heat exchanger 7, the distribution valve 47 is closed so that the gas flows completely in the section 50, whereby it is treated by the high-pressure evaporator 11.
Similar to the first embodiment, and more specifically, as shown in FIG. 2, the return line 14 may include a main section 56, which is then split from the split area 53 into a first section 51 and a second section 52. This zone is always located downstream of the second heat exchanger 7. The operation of the return line 14 as shown in fig. 3 is the same as described in fig. 2.
Fig. 4 is a cross-sectional view of floating structure 20 showing tank 8 containing gas in both liquid and vapor states, the tank 8 being generally prismatic in shape and mounted in a double hull 22 of floating structure 20. The walls of tank 8 comprise a primary sealing membrane intended to be in contact with the liquid gas contained in tank 8, a secondary sealing membrane arranged between the primary sealing membrane and the double hull 22 of floating structure 20, and two thermal insulation barriers arranged between the primary sealing membrane and the secondary sealing membrane and between the secondary sealing membrane and the double hull 22, respectively.
The liquid gas handling tubes 23 arranged on the upper deck of the floating structure 20 may be connected to a marine terminal or port terminal by suitable connectors to transfer liquid gas cargo from the tanks 8 or to the tanks 8.
Fig. 4 also shows an example of a marine or harbour terminal comprising loading and/or unloading equipment 25, a submarine pipeline 26 and an onshore and/or harbour facility 27. The onshore and/or harbor facilities 27 may for example be arranged on a dock of a harbor or according to another example on a concrete gravity platform. The onshore and/or harbor installation 27 comprises a tank 30 for liquid gas and a connection pipe 31 connected to the loading and unloading device 25 by means of the underwater pipe 26.
In order to generate the pressure required for the transport of the liquid gas, pumps equipped with onshore and/or harbour facilities 27 and/or pumps equipped with floating structures 20 are implemented.
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 previously stated, the present invention clearly achieves its own set aim and makes it possible to provide a gas supply system for a high-pressure or low-pressure gas consumer, the pressurization of which is achieved by a pump and an evaporator, comprising means for condensing gaseous gas before the gas is returned to the tank, and comprising high-pressure gas supply means which allow optimizing the energy for pressurizing said gas. Variations not described herein may be implemented without departing from the invention, as they comprise a supply system according to the invention.

Claims (18)

1. A supply system (1) for supplying gas to at least one high pressure gas consuming device (4) and at least one low pressure gas consuming device (5) of a floating structure (20), the floating structure comprising at least one tank (8) configured to contain gas, the supply system (1) comprising:
at least a first gas supply circuit (2) of the high-pressure gas consumer (4) comprising at least one pump (9) configured to pump collected liquid gas into the tank (8),
At least one high-pressure evaporator (11) configured to evaporate the gas circulating in the first gas supply circuit (2);
-at least one second circuit (3) supplying gas to the low-pressure gas consuming device (5), comprising at least one compressor (13) configured to compress the gas extracted in vapor state from the tank (8) to a pressure compatible with the requirements of the low-pressure gas consuming device (5);
-at least one gas return line (14) connected to the second supply circuit (3) downstream of the compressor (13) and extending to the tank (8);
at least a first heat exchanger (6) and a second heat exchanger (7), each configured to exchange heat between the gas flowing in the return line (14) and the gas flowing in the first supply circuit (2), characterized in that the first supply circuit (2) comprises a main path (40) and a bypass path (41) arranged in parallel with at least one portion (50) of the main path (40), the second heat exchanger (7) being configured to exchange heat between the gas flowing in the return line (14) and the gas flowing in the bypass path.
2. Supply system (1) according to claim 1, wherein the main path (40) comprises an additional pump (10) placed between the first heat exchanger (6) and the high pressure evaporator (11).
3. The supply system (1) according to claim 2, wherein the bypass path (41) starts at a branching point (42) arranged on the main path (40), which branching point is located between the additional pump (10) and the high pressure evaporator (11).
4. Supply system (1) according to any one of the preceding claims, wherein the first supply circuit (2) comprises a distribution device (60), the distribution device (60) being configured to control the distribution of the gas flow to the portion (50) of the main path (40) and/or the bypass path (41).
5. A supply system (1) according to claim 3, wherein the bypass path (41) ends at a convergence point (43) arranged on the main path, the convergence point being located between the split-flow point (42) and the high pressure evaporator (11).
6. Supply system (1) according to claim 5 in combination with claim 4, wherein the distribution device (60) comprises a first valve (44) and a second valve (45), the first valve (44) being configured to manage the gas circulation within the bypass path (41), the second valve (45) being arranged on the portion (50) of the main path (40).
7. A supply system (1) according to claim 3, wherein the bypass path (41) ends at a convergence point (43) provided on the main path (40), downstream of the high pressure evaporator (11).
8. Supply system (1) according to claim 7 in combination with claim 4, wherein the dispensing device (60) comprises a dispensing valve (47).
9. Supply system (1) according to claim 8, wherein the distribution valve (47) is arranged on the portion (50) of the main path (40).
10. Supply system (1) according to claim 8, wherein the distribution valve (47) is arranged on the bypass path (41).
11. The supply system (1) according to any one of claims 8 to 10, wherein the return line (14) comprises an expansion member (15), the expansion member (15) being arranged between the first heat exchanger (6) and the tank (8) and being configured to regulate the flow of gas circulating in the return line (14), the expansion member (15) and the distribution valve (47) being configured to cause the gas circulating within the bypass path (41) to transition from a liquid state to a gaseous or supercritical state.
12. The supply system (1) according to any one of the preceding claims, wherein the first heat exchanger (6) is configured to condense gas circulating within the return line (14).
13. The supply system (1) according to any one of the preceding claims, wherein the second heat exchanger (7) is configured to pre-cool the gas circulating in the return line (14).
14. Supply system (1) according to any one of the preceding claims, wherein the return line (14) comprises a splitting zone (53) dividing the return line (14) into a first section (51) and a second section (52), both extending from the splitting zone (53) to the tank (8), the first heat exchanger (6) being configured to exchange heat between gas circulating in gaseous state in the first section (51) of the return line (14) and liquid gas circulating in the first supply circuit (2), the second section (52) bypassing the first heat exchanger (6).
15. The supply system (1) according to any one of the preceding claims, comprising an auxiliary supply line (16) connected to the first supply circuit (2) upstream of the first heat exchanger (6) and extending downstream of the compressor (13) to the second supply circuit (3), the supply system (1) comprising a low pressure evaporator (17) configured to evaporate the gas circulating in the auxiliary supply line (16).
16. Floating structure (20) for storing and/or transporting liquid gas, comprising at least one tank (8) containing liquid gas, at least one high pressure gas consuming device (4), at least one low pressure gas consuming device (5) and at least one supply system (1) for supplying gas to these devices according to any of the preceding claims.
17. A system for loading or unloading liquefied gas, incorporating at least one onshore and/or harbour facility (27) and at least one floating structure (20) for storing and/or transporting liquefied gas according to claim 16.
18. Method for loading or unloading liquid gas from a floating structure (20) for storing and/or transporting gas according to claim 16, wherein a pipe (23) for loading and/or unloading liquid gas arranged on the upper deck of the floating structure (20) can be connected to a sea or port terminal by means of a suitable connector for transporting liquid gas to or from the tank (8).
CN202280009865.7A 2021-01-19 2022-01-14 Gas supply system for high-pressure and low-pressure gas consumers Pending CN116710725A (en)

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FRFR2100468 2021-01-19
FR2100468A FR3119013B1 (en) 2021-01-19 2021-01-19 Gas supply system for appliances using high and low pressure gas
PCT/FR2022/050089 WO2022157446A1 (en) 2021-01-19 2022-01-14 Gas supply system for high- and low-pressure gas consuming appliances

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FR3049341B1 (en) * 2016-03-23 2019-06-14 Cryostar Sas SYSTEM FOR TREATING A GAS FROM THE EVAPORATION OF A CRYOGENIC LIQUID AND THE PRESSURIZED GAS SUPPLY OF A GAS ENGINE
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EP4281718A1 (en) 2023-11-29
FR3119013B1 (en) 2023-03-17

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