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
• • 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
• • 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
  • F25J1/003—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

Definitions

• the present invention relates to the field of vessels for storing and/or transporting gas in the liquid state and more particularly relates to a gas supply system for consumer appliances included within such vessels.
• a ship comprising a tank of gas in the liquid state intended to be consumed and/or to be delivered to a point of destination
• said ship may be able to use at least part of said gas to the liquid state in order to supply at least one of its motors, via a gas supply system.
• a gas supply system This is the case for ships equipped with an ME-GI type propulsion engine.
• the gas In order to supply this type of engine, the gas must be compressed at very high pressure by special compressors capable of compressing the gas up to 300 bars, but such compressors are expensive, generate substantial maintenance costs and induce vibrations. within the ship.
• the present invention makes it possible to meet such an objective by proposing a gas supply system for at least one high-pressure gas-consuming device and at least one low-pressure gas-consuming device of a floating structure comprising at least one tank configured to contain the gas, the supply system comprising: at least one first gas supply circuit of the high-pressure gas-consuming device, comprising at least one pump configured to pump the gas taken from the liquid state in the tank, at least one high-pressure evaporator configured to evaporate the gas circulating in the first gas supply circuit, at least one second gas supply circuit of the low-pressure gas-consuming device , comprising at least one compressor configured to compress gas withdrawn in the vapor state from the tank up to a pressure compatible with the needs 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 as far as the tank, at least a first heat exchanger and a second heat exchanger each configured to operate a heat exchange between the gas flowing in the return line and the gas flowing in the first supply circuit, characterized in that the first
• the presence of the bypass channel thus makes it possible to circulate the gas through the second heat exchanger only when necessary, for example in the event of excess gas in the vapor state present in the vessel.
• the gas can also flow through within the main track in its entirety, including the portion of the main track running parallel to the bypass track, and is treated directly by the high pressure evaporator after passing through the first heat exchanger.
• the gas taken from within the tank and intended to supply the high-pressure gas-consuming device thus has several circulation modes, which ensures that the circulation of superfluous gas is avoided and also limits the quantity of energy linked to the use of the high pressure evaporator and/or the second heat exchanger.
• the vapor-era gas present in the tank and not used for the consumption of the low-pressure gas-consuming device can be recondensed and is thus returned to the tank at the liquid era, instead of being eliminated.
• the loss of gas to the vapor era present in excess in the tank is then at least reduced.
• the first gas supply circuit therefore makes it possible to meet the fuel needs of the device consuming high-pressure gas.
• the latter may, for example, be the means of propulsion of the floating structure, for example a MEGI engine.
• the first supply circuit extends from the tank to the high pressure gas consuming device.
• the pump is installed at the bottom of the tank and pumps the gas to the liquid state so that it can circulate in the first supply circuit.
• the high-pressure evaporator guarantees the evaporation of the gas before it is supplied to the high-pressure gas-consuming device.
• the high pressure evaporator is the seat of a heat exchange between the gas circulating in the first supply circuit and a heat transfer fluid, for example glycol water, sea water or steam. water. The latter must be at a temperature high enough to create a change in the gas era so that the latter passes to the vapor or supercrystal era and feeds the high-pressure gas-consuming device.
• the gas circulating in the first supply circuit passes through the first heat exchanger, then optionally the second heat exchanger depending on the configuration chosen.
• the gas can then be vaporized through the evaporator high pressure.
• the temperature of the gas thus makes it possible to increase more or less before the latter passes through the high pressure evaporator if the configuration of the first supply circuit allows it.
• the gas circulating in the first feed circuit can be in a two-phase, vapor, liquid or supercritical phase at the outlet of the second heat exchanger if the bypass route is taken by the gas.
• the gas contained in the tank can pass naturally, or forced by the floating structure, into the vapor phase.
• the gas within the tank passing to the vapor stage must be evacuated so as not to create an overpressure within the tank.
• the second gas supply circuit of the appliance consuming low pressure gas extends from the tank to the low pressure gas consuming device.
• the latter may, for example, be an auxiliary motor such as an electric generator.
• the compressor arranged on the second supply circuit is responsible for sucking in the gas present in the top of the tank in order to be able to supply the device consuming low-pressure gas, but also to regulate the pressure within tank.
• the second supply circuit is structurally separate from the first supply circuit, except that both supply circuits are connected to the tank.
• the vapor-era gas can supply the low-pressure gas-consuming device, or circulate through the return line if the low-pressure gas-consuming device does not require a fuel supply .
• the return line is connected downstream of the compressor, the vapor-era gas sucked in by the compressor can therefore flow through it.
• the vapor-era gas circulating in the return line first passes through the second heat exchanger, then the first heat exchanger, before returning to the tank.
• the heat exchange can be carried out within the two heat exchangers or only within the first heat exchanger. Thanks to the heat exchange taking place between the gas circulating in the first supply circuit and the gas circulating in the return line, the temperature of the gas at the vapor stage decreases by passing through the heat exchangers, up to so that said gas condenses and returns to the liquid erar substantially at the outlet of the first heat exchanger. The recondensed gas then circulates to the vessel.
• the main path comprises an additional pump interposed between the first heat exchanger and the high pressure evaporator. It is the additional pump which makes it possible to increase the pressure of the gas circulating in the first supply circuit, so that it has a compatible pressure for the supply of the device consuming high pressure gas.
• the position of the additional pump is parricularly advantageous. Indeed, setting up the additional pump upstream of the first heat exchanger leads to a rise in the pressure and the temperature of the gas in the liquid era as soon as it passes through the first heat exchanger, which is detrimental to the condensation of the gas. at the same time steam circulating in the return line also crosses the first heat exchanger.
• the optimum arrangement therefore consists of placing the additional pump downstream of the first heat exchanger.
• the bypass path begins at a point of divergence arranged on the main path between the additional pump and the high pressure evaporator. It is from the point of divergence that the first supply circuit is divided between the portion of the main track and the bypass track.
• the gas circulating therein after having passed through the first heat exchanger, can circulate in the portion of the main channel to subsequently be directly treated by the high pressure evaporator er /or within the bypass path to cross the second heat exchanger.
• the point of divergence is downstream of the additional pump so that the second heat exchanger is also downstream of the additional pump.
• the gas circulating in the bypass channel which can be in a vapor, liquid, diphasic state or supercritical at the outlet of the second heat exchanger, arranging the additional pump downstream of the second heat exchanger can be detrimental to the correct operation of the latter given that the additional pump only allows the pumping of a fluid in the liquid state.
• the first supply circuit comprises a distribution device configured to control a distribution of the flow of gas towards the portion of the main track and/or towards the branch track.
• the distribution device can be controlled remotely, so that the circulation of the gas within the first supply circuit is optimal for the consumption of the gas by the consuming device and for the condensation of the gas circulating in the return line .
• the bypass path ends at a convergence point arranged on the main path between the divergence point and the high pressure evaporator.
• a convergence point arranged on the main path between the divergence point and the high pressure evaporator.
• the point of convergence of the portion of the main channel and the bypass channel is arranged downstream of the point of divergence and upstream of the high pressure evaporator.
• the gas circulating in the bypass path passes through the second heat exchanger, then rejoins the main path before being treated by the high pressure evaporator. All of the gas circulating in the first supply circuit is therefore treated by the high pressure evaporator according to the first embodiment. The latter therefore allows the gas to pass through the second heat exchanger and/or to bypass the latter.
• the distribution device comprises a first valve configured to manage the flow of gas within the bypass channel and a second valve arranged on the portion of the main channel.
• the valves can be controlled remotely in order to switch to the open or closed position and thus to determine the circulation of the gas circulating within the first supply circuit.
• the first valve can be arranged on the branch path upstream or downstream of the second heat exchanger.
• the second valve is for its part arranged on the portion of the main track arranged in parallel with the bypass track.
• the first valve makes it possible to control the flow of gas in the bypass channel
• the second valve makes it possible to control the flow of gas in the portion of the main channel arranged in parallel with the bypass channel. If the first valve is closed and the second valve open, then the gas flows within the main path in its entirety. If the first valve is open and the second valve closed, then the gas flows entirely through the bypass channel then joins the main channel upstream of the high pressure evaporator.
• the two valves can also be opened so that the gas separates into two fractions, one directly joining the high pressure evaporator via the portion of the main channel, the other circulating within the bypass channel crossing the second heat exchanger.
• the bypass path and the first valve are configured so that the gas which circulates between the point of divergence and the second heat exchanger is maintained at liquid level.
• the first valve has the sole function of authorizing or not the circulation of gas within the bypass channel without causing any change in erar, for example by releasing the gas flowing in the bypass channel.
• the gas circulating in the bypass channel is kept at the liquid state until it crosses the second heat exchanger.
• the gas circulating in the bypass path can leave the second heat exchanger in a liquid phase. , steam, two-phase or supercriric.
• the branch line ends at a convergence point arranged on the main line downstream of the high pressure evaporator.
• a connected configuration corresponds to a second embodiment of the power supply system according to the invention.
• the branch path bypasses the high pressure evaporator. The latter is therefore located within the portion of the main track arranged in parallel with the bypass track.
• the gas circulating in the first supply circuit is therefore either treated by the high pressure evaporator if the gas circulates within the portion of the main channel, or is treated by the second heat exchanger whether the gas is flowing within the bypass path.
• the gas At the outlet of the high pressure evaporator or the second heat exchanger, the gas has compatible characteristics for its consumption by the device consuming high pressure gas, for example by being in a vapor or supercritical state.
• the second embodiment therefore makes it possible to distribute the load of the change of state of the gas circulating within the first supply circuit, and this while cooling the gas circulating in the return line thanks to the heat exchange operated at the within the second heat exchanger.
• the distribution device comprises a distribution valve.
• the distribution valve makes it possible to control the flow of gas circulating in the portion of the main channel and/or in the bypass channel.
• the valve may have a degree of opening, a distribution of the gas flowing between the portion of the main channel and/or the bypass channel being dependent on the degree of opening of the distribution valve.
• the distribution valve is arranged on the portion of the main track.
• the greater the degree of opening of the distribution valve the greater the proportion of gas circulating within the portion of the main channel.
• the lower the degree of opening of the distribution valve the greater the proportion of gas circulating within the bypass channel. If the distribution valve is completely open, the gas flows exclusively in the portion of the main channel. If the distribution valve is closed, the gas flows exclusively in the bypass path.
• the distribution valve can be positioned either between the point of divergence and the high pressure evaporator, or between the high pressure evaporator and the point of convergence.
• the distribution valve is arranged on the branch line.
• the higher the degree of opening of the distribution valve the greater the proportion of gas circulating within the bypass channel. Conversely, the lower the degree of opening of the distribution valve, the greater the proportion of gas circulating within the portion of the main channel. If the distribution valve is completely open, the gas flows exclusively in the bypass channel. If the distribution valve is closed, the gas flows exclusively in the portion of the main track.
• the distribution valve can be positioned either between the point of divergence and the second heat exchanger, or between the second heat exchanger and the point of convergence.
• the return line comprises an expansion member arranged between the first heat exchanger and the tank and configured to regulate a gas flow rate circulating in the return line, said expansion member and the reparririon being configured so that the gas which circulates within the diversion channel passes from the liquid erar to the vapor or supercrystal erar.
• the gas circulating in the first supply circuit is treated by the high pressure evaporator or by the second heat exchanger.
• the gas flowing in the bypass path must be, at the outlet of the second heat exchanger, in a state compatible to be consumed by the high-pressure gas-consuming device, for example in a vapor or supercriric state. It is therefore important that the gas circulating in the bypass channel is entirely at the vapor or supercritical stage at the outlet of the second heat exchanger.
• the flow of gas circulating in the bypass channel can be proportional to the flow of gas circulating in the return line so that, during the heat exchange, the majority of the gas circulating in the bypass channel will end up in a vapor phase. or supercritical at the outlet of the second heat exchanger.
• the expansion device arranged on the return line therefore makes it possible to control the flow of gas circulating in the return line, while the distribution valve makes it possible to control the flow of gas circulating in the path of derivation.
• the gas circulating in the bypass channel leaves the second heat exchanger in a state compatible with its consumption by the gas-consuming device at high pressure, without having been treated by the high pressure evaporator.
• the first heat exchanger is configured to condense the gas circulating within the return line.
• the first heat exchanger is the exchanger through which the gas in the liquid state of the first supply circuit passes when said gas in the liquid state is at its lowest temperature. It is therefore the heat exchange taking place within the first heat exchanger that will change the state of the gas circulating in the return line to change it from the vapor state to the liquid state.
• the second heat exchanger is configured to pre-cool the gas circulating within the return line.
• the gas circulating in the first supply circuit is less cold than at the inlet of the first heat exchanger, a heat exchange having served to condense the gas circulating in the return line.
• the gas in liquid state is compressed by the additional pump and then reaches the point of divergence.
• the gas may subsequently pass through the second heat exchanger. If this is the case, a heat exchange also takes place within the second heat exchanger, allowing the precooling of the gas in the vapor state within the return line.
• the return line can comprise a zone of divergence dividing the return line into a first section and into a second section both extending from the zone of divergence to the tank, the first heat exchanger being configured to operate a heat exchange between the gas circulating in the vapor state in the first section of the return line and the gas in the liquid state circulating in the first supply circuit, the second section bypassing the first heat exchanger.
• the gas in the vapor state present in the tank and not used for the consumption of the device consuming gas at low pressure can be condenses by circulating via the first section of the return line and is thus returned to the tank in the liquid state, instead of being eliminated.
• the quantity of gas in the liquid state circulating in the first supply circuit is less than six times the quantity of gas in the vapor state circulating in the return line, then it is advantageous to circulate the gas at the vapor state at least partially within the second section of the return line, part of the gas in the vapor state then circulating in the first section in a quantity such that the condensation is complete.
• the gas in the vapor state flowing in the return line can flow into the first section or into the second section from the zone of divergence. If the gas in the vapor state circulates in the first section, the latter initially passes through the second heat exchanger, then the first heat exchanger, before returning to the tank, as described previously. If the gas in the vapor state circulates in the second section, it passes through the second heat exchanger and then returns directly to the tank. According to this configuration, the temperature of the gas at the vapor state decreases due to the exchange of calories operated within the second heat exchanger, but is however not condensed. The gas thus returns to the tank in the vapor state, but nevertheless being cooled.
• the second section of the return line thus comprises an end immersed in the liquid contained in the tank.
• the second section may include an ejection member arranged at the submerged end.
• the ejection device allows in particular to expand the gas in the vapor state circulating in the second section of the return line before the latter is dispersed in the tank.
• the expansion of the gas in the vapor state associated with the fact that the submerged end is preferably arranged at the bottom of the tank, makes it possible to liquefy at least part of the gas in the vapor state when the latter returns to the tank, also causing a rise in temperature of the gas in liquid form present in the tank.
• the ejection member can for example be an ejector or a bubbling device.
• the supply system comprises an auxiliary supply line connected to the first supply circuit, upstream of the first heat exchanger, and extending as far as the second supply circuit, in downstream of the compressor, the supply system comprising a low pressure evaporator configured to evaporate the gas circulating in the auxiliary supply line.
• auxiliary supply line is used when the low-pressure gas-consuming device needs to be supplied with gas in the vapor state, but the latter is not in sufficient quantity within the top of the vessel.
• the auxiliary supply line thus makes it possible to divert part of the gas in the liquid state circulating in the first supply circuit.
• This part is then evaporated by the low pressure evaporator, according to an operation similar to that of the high pressure evaporator, that is to say by heat exchange with a heat transfer fluid such as glycol water, sea water or water vapour, for example.
• the low-pressure evaporator thus induces an exchange of calories between the gas in the liquid state circulating in the auxiliary supply line and this heat transfer fluid. Once in the vapor state, the gas continues to circulate within the auxiliary supply line and joins the second supply circuit in order to supply the low-pressure gas-consuming device.
• the auxiliary supply line is not used and can for example be closed by a valve.
• the invention also covers a floating structure for storing and/or transporting gas in the liquid state, comprising at least one tank containing gas in the liquid state, at least one device consuming high-pressure gas, at least a low-pressure gas-consuming appliance and at least one gas supply system for these appliances.
• the invention also covers a system for loading or unloading a liquid gas which combines at least one onshore and/or port installation and at least one floating structure for storing and/or transporting liquid gas.
• the invention finally covers a method for loading or unloading a liquid gas from a floating structure for storing and/or transporting gas in which pipes for loading and/or unloading gas in the liquid state arranged on an upper deck of the floating structure can be connected, by means of appropriate connectors, to a maritime or port terminal in order to transfer the gas in the liquid state from or to the tank.
• FIG. 1 represents a first embodiment of a supply system according to the invention
• FIG. 1 represents the first embodiment of the supply system comprising a return line divided into two sections
• FIG. 3 represents a second embodiment of the power supply system
• FIG. 4 is a cutaway schematic representation of a tank of a floating structure and a loading and/or unloading terminal for this tank.
• Figures 1 to 3 show a gas supply system 1 arranged on a floating structure.
• the supply system 1 makes it possible to circulate gas which may be in the liquid state, in the vapor state, in the two-phase state or in the supercritical state, from a storage tank 8 and/or transport, and to a high-pressure gas-consuming device 4 and/or a low-pressure gas-consuming device 5, in order to supply the latter with fuel.
• Said floating structure can for example be a ship capable of storing and/or transporting gas in the liquid state.
• the supply system 1 is in this case capable of using the gas in the liquid state that the floating structure stores and/or transports to supply the high-pressure gas-consuming device 4, which can for example be a motor propulsion, and the low-pressure gas consuming device 5, which can for example be an electric generator supplying the floating structure with electricity.
• the supply system 1 is provided with a first gas supply circuit 2.
• the first supply circuit 2 comprises a pump 9 disposed within the tank 8.
• the pump 9 makes it possible to pump the gas in the liquid state and to cause it to circulate in particular within the first supply circuit 2. By sucking and by compressing the gas in the liquid state, the pump 9 makes it possible to raise the pressure of the latter to a value comprised between 6 and 17 bars.
• the first supply circuit 2 comprises a main channel 40 and a bypass channel 41.
• the main channel 40 extends from the pump 9 to the high pressure gas consuming device 4.
• the bypass channel 41 is as for it arranged in parallel with a portion 50 of the main channel 40.
• the gas circulating in the first supply circuit 2 can therefore circulate via the portion 50 of the main channel 40 or via the bypass channel 41.
• the control of the circulation of the gas within the portion 50 of the main channel 40 and/or of the bypass channel 41 is managed by a distribution device 60 which ensures the distribution of the gas according to factors and/or needs which will be detailed subsequently. If the gas flows within the bypass path 41, the gas passes through a second heat exchanger 7. The details concerning the two heat exchangers 6, 7 will be described later.
• the branch path 41 comprises a first part 41a extending between the point of divergence 42 and the second heat exchanger 7, and a second part 41b extending between the second heat exchanger 7 and the point of convergence 43.
• the portion 50 of the main channel 40 and the branch channel 41 both extend from the point of divergence 42 to a point of convergence 43. From the latter, the gas circulates again within the main channel 40 until to a high pressure evaporator 11.
• the high pressure evaporator 11 makes it possible to modify the state of the gas circulating in the first supply circuit 2 in order to make it pass to the vapor state.
• Such a state allows the gas to be compatible for supplying the high-pressure gas-consuming device 4, for example by being in a vapor or supercritical state.
• the evaporation of the gas in the liquid state can for example be done by heat exchange with a heat transfer fluid at a temperature high enough to evaporate the gas in the liquid state, here glycol water, sea water or water vapour.
• the increase in gas pressure is ensured by the additional pump 10 when the latter pumps the gas in the liquid state.
• the additional pump 10 makes it possible to raise the pressure of the gas in the liquid state to a value between 30 and 400 bars, in particular for use with ammonia and/or hydrogen, between 30 and 70 bars for a use with liquefied petroleum gas, and preferably between 150 and 400 bars for use with ethane, ethylene or with liquefied natural gas consisting mainly of methane.
• the gas is at a pressure and in a state compatible for the supply of the high pressure consuming device 4.
• Such a configuration makes it possible to avoid the installation of high pressure compressors on the first supply circuit 2 which present cost constraints and generate strong vibrations.
• the distribution device 60 comprises a first valve 44 arranged at the level of the bypass path 41 and a second valve 45 arranged at the level of the portion 50 of the main channel 40.
• a first valve 44 arranged at the level of the bypass path 41
• a second valve 45 arranged at the level of the portion 50 of the main channel 40.
• the first valve 44 is arranged at the level of the first part 41a of the bypass channel 41.
• the first valve 44 can also be arranged on the second part 41b of the bypass channel 41.
• the gas at the vapor state contained in the top of tank 12 must be evacuated.
• the first supply circuit 2 is configured to use the gas in the liquid state to supply the high-pressure gas-consuming device 4.
• the supply system 1 therefore comprises a second gas supply circuit 3, which uses the gas in the vapor state to supply the low-pressure gas-consuming device 5.
• the second supply circuit 3 extends therefore between the top of the tank 12 and the low-pressure gas consuming device 5.
• the first supply circuit 2 and the second supply circuit 3 are structurally distinct. each other.
• the second supply circuit 3 comprises a compressor 13.
• the compressor 13 In addition to sucking in the gas in the vapor state, the compressor 13 also makes it possible to compress the gas in the vapor state circulating in the second supply circuit 3 at a pressure of between 6 and 20 bar absolute, so that the gas in the vapor state is at a pressure compatible for supplying the low-pressure gas-consuming device 5.
• the second supply circuit 3 thus makes it possible to supply the appliance consuming low-pressure gas 5, and this while regulating the pressure within the tank 8 by drawing in the gas in the vapor state present in the top of the tank 12 .
• the supply system 1 comprises a return line 14 which extends from the second supply circuit 3 to tank 8.
• the return line 14 is connected to the second supply circuit 3 downstream of the compressor 13 with respect to a direction of circulation of the gas in the vapor state circulating in the second supply circuit 3.
• said gas first passes through the second heat exchanger 7, then passes through the first heat exchanger 6.
• the heat exchange taking place within the first exchanger of heat 6 and of the second heat exchanger 7 is therefore between the gas circulating in the first supply circuit 2 and the gas circulating in the return line 14. More particularly, the heat exchange taking place within the second heat exchanger 7 takes place between the gas flowing in the branch path 41 and the gas flowing in the return line 14.
• the first heat exchanger 6 is of co ndenser the gas in the vapor state of the return line 14, so that it changes to the liquid state and returns to the tank 8 in this state, instead of being eliminated by the burner 18. It is at the inlet of the first heat exchanger 6 that the gas in the liquid state of the first supply circuit 2 has the lowest temperature. Therefore, it is therefore after having passed through the first heat exchanger 6 that the gas circulating in the return line 14 is condensed. The gas in the return line 14 is therefore in the vapor state at the inlet of the first heat exchanger 6 and exits in the liquid state following the heat exchange taking place within the first heat exchanger 6.
• the return line 14 can comprise an expansion device 15 which lowers the pressure of the gas to a pressure comprised between 1 and 3 bar absolute.
• the expansion member 15 is also able to regulate a flow of gas circulating within the return line 14. Once the gas is condensed, it continues its course to the tank 8.
• the first heat exchanger Heat 6 therefore acts as a condenser.
• the second heat exchanger 7 is located downstream of the first heat exchanger 6 according to the direction of circulation of the gas in the first supply circuit 2, and upstream of the first heat exchanger 6 according to the direction of circulation of the gas in the return line 14. Provided that the gas circulating within the first supply circuit 2 passes through the bypass path 41, the second heat exchanger 7 therefore provides pre-cooling of the gas in the vapor state circulating in the return line 14 before the latter is condensed within the first heat exchanger 6. At the branch line 41, the gas at the inlet of the second heat exchanger 7 has previously passed through the first heat exchanger 6 and was pumped by the additional pump 10, which therefore increased its temperature and pressure.
• the gas circulating within the first supply circuit 2 leaves the second heat exchanger 7 in a liquid, vapor, diphasic state. or supercritical.
• the temperature of the gas circulating in the return line 14 is therefore lowered after passing through the second heat exchanger 7, implementing the pre-cooling indicated above.
• the gas does not flow in the bypass channel 41, and the gas flowing in the return line 14 passes through the second heat exchanger 7 without being pre-cooled therein.
• the circulation of the gas via the portion 50 of the main channel 40 can also be preferred when there is no gas to be recondensed circulating in the return line 14.
• the heat exchange operated within the second heat exchanger 7 makes it possible to increase the temperature of the gas circulating in the bypass channel 41 and thus makes it possible to limit the energy necessary to be supplied to the heat-transfer fluid circulating in the high-pressure evaporator 11 to evaporate the gas having passed through the second heat exchanger 7 beforehand.
• the additional pump 10 is advantageously arranged downstream of the first heat exchanger 6 and upstream of the second heat exchanger 7 if the gas circulates via the bypass channel 41. Thanks to the expansion device 15, the regulation of the gas flow circulating within the return line 14 ensure that the gas circulating in the first circuit alimenrarion 2 st through the first heat exchanger 6 evening maintained at the liquid erar at the outlet of the latter. The additional pump 10 then draws in the gas maintained in the liquid state without risking being damaged by the presence of at least a fraction of gas in the vapor state.
• the presence of the additional pump 10 downstream of the first heat exchanger 6 ensures the increase in pressure of the gas to the liquid era, without disturbing the heat exchange occurring within the first heat exchanger 6
• the condensation of the vapor-era gas flowing in the return line 14 is thus carried out in an optimal manner.
• the power supply system 1 also comprises an auxiliary power supply line 16, extending from the first power supply circuit 2, via a connection between the pump 9 and the first heat exchanger 6, as far as the second power supply circuit. 3, by being connected thereto between the compressor 13 and the low-pressure gas-consuming device 5.
• the auxiliary supply line 16 makes it possible to supply the low-pressure gas-consuming device 5 in the event of flow insufficient gas in the vapor era formed within the head of vessel 12.
• auxiliary supply line 16 in order to supply the low pressure gas consuming device 5.
• the auxiliary supply line 16 passes through a low pressure evaporator 17 so that the gas in the liquid state circulating in the line auxiliary supply 16 goes into the vapor state.
• the operation of the low pressure evaporator 17 can for example be identical to that of the high pressure evaporator 11, that is to say that the gas is evaporated by heat exchange with a heat transfer fluid at a sufficiently high temperature to evaporate gas in liquid state.
• the gas in the vapor state circulates within the auxiliary supply line 16, then joins the second supply circuit 3 in order to supply the appliance consuming gas at low pressure 5.
• auxiliary supply line 16 is used only in the absence of gas in the vapor state in sufficient quantity within the head of the vessel 12.
• the line of auxiliary supply 16 comprises a valve 19 controlling the flow of gas within the auxiliary supply line 16 when the use of the latter is not necessary.
• FIG. 2 shows the first embodiment of the supply system 1 with a return line 14 divided into two separate sections.
• the return line 14 thus comprises a main section 56 which begins at the level of the connection with the second supply circuit 3 and which extends as far as a zone of divergence 53.
• the line return 14 is divided into a first section 51 and a second section 52 both extending from the divergence zone 53 to the tank 8.
• the divergence zone 53 is arranged downstream of the second heat exchanger 7. It is therefore the main section 56 of the return line 14 which crosses the second heat exchanger 7.
• the gas in the vapor state circulates as far as the divergence zone 53 and can subsequently circulate within the first section 51 or the second section 52.
• the first section 51 crosses the first heat exchanger 6 while the second section 52 extends to the tank 8 bypassing the first heat exchanger 6.
• the gas at the vapor level can circulate within the first section 51 and be condensed thanks to the exchange of calories occurring at the level of the first heat exchanger 6, or can circulate within the second section 52 st return to the tank 8 to the gaseous era.
• the choice of the section within which the gas circulates in the vapor state is in particular dependent on a flow rate of gas in the liquid state circulating in the first supply circuit 2, said flow rate having to be sufficient to completely condense the vapor-era gas circulating in the return line 14.
• the quantity of liquid-era gas circulating in the first supply circuit is greater than or equal to six times the quantity of vapor-era gas circulating in the return line, the gas in the vapor era can be directed towards the first section 51 so that the condensation of the latter can be implemented.
• a first fraction of the vapor-era gas circulates within the first section 51 in quantity connects that the first fraction is fully condensed within the first exchanger 6, while a second fraction of the gas in the vapor era, corresponding to the quantity of gas in the vapor era not circulating in the first section 51, circulates within the second section 52 in order to return directly within the tank 8.
• the expansion member 15 is arranged at the level of the first section 51, downstream of the first heat exchanger 6, while the second section 52 comprises a regulating member flow rate 54.
• the expansion member 15 and the flow control member 54 can also perform a function of expanding the gas flowing in one or the other of the sections.
• the gas which circulates there returns to the bottom of the tank 8 or at least to a zone where the gas is in liquid form. More particularly, the gas circulating in the vapor state in the second section 52 returns to the bottom of the vessel in the vapor state.
• the temperature and the density of the gas in the liquid state present in the tank 8 thus makes it possible to condense the gas in the vapor state leaving the second section 52.
• the second section 52 may comprise an ejection member 55 arranged at one end of the second section 52 immersed in the liquid contents of the tank 8.
• the ejection member 55 makes it possible to expand the gas in the vapor state circulating in the second section 52 in order to facilitate the condensation thereof within the tank 8.
• the ejection member 55 can for example be an ejector or a bubbling device.
• the return of the gas in the vapor state in the tank 8 via the second section 52 causes a rise in the temperature of the gas in the liquid state present in the tank 8.
• FIG. 3 represents a second embodiment of the supply system 1 according to the invention.
• the second embodiment differs from the first embodiment by the configuration of the main channel 40 and of the bypass channel 41. Reference will therefore be made to the description of FIGS. 1 and 2 for the notions common to the two embodiments.
• the point of convergence 43 is here arranged downstream of the high pressure evaporator 11.
• the branch path still comprising the second heat exchanger 7, is configured to bypass the high pressure evaporator 11.
• the latter is therefore arranged within the portion 50 of the main channel 40.
• the first supply circuit 2 is configured so that the gas circulates entirely within the main channel 40, the latter, after having passed through the first heat exchanger 6 and the additional pump 10, is directly treated by the high pressure evaporator 11 by circulating within the portion 50.
• the distribution device 60 comprises a distribution valve 47 arranged on the first part 41a of the bypass channel 41.
• the distribution valve 47 can be arranged on the second part 41b of the branch line 41, or on the portion 50 of the main line 40, between the point of divergence 42 and the high pressure evaporator 11 or between the high pressure evaporator 11 and the point of convergence 43.
• the distribution of the gas flowing in the portion 50 of the main channel 40 and/or in the bypass channel 41 is done according to a degree of opening of the distribution valve 47.
• the distribution valve 47 is arranged on the bypass channel 41.
• the more the distribution valve 47 is open the higher the proportion of gas flowing in the bypass channel 41 is high.
• the degree of opening of the distribution valve 47 it is therefore possible to manage the distribution of the gas in the portion 50 of the main channel 40 and/or in the bypass channel 41.
• the gas flowing in the bypass channel 41 is not treated by the high pressure evaporator 11, it is essential that the characteristics of the gas, after passing through the second heat exchanger 7, conform to its use as fuel for the high-pressure gas-consuming device 4, for example by corresponding to a vapor or supercritical state.
• the distribution valve 47 is thus controlled in order to allow the circulation in the bypass channel 41 of a quantity of gas such that the heat exchange occurring in the second heat exchanger 7 is sufficient for the totality of said quantity of gas goes into the vapor or supercritical state in order to be compatible with the gas-consuming device at high pressure 4.
• the expansion device 15 of the return line 14 can also influence a connected condition by controlling the flow of gas circulating in the return line 14.
• the gas circulating in the return line 14 is pre-cooled within the second heat exchanger 7, provided that at least a fraction of gas circulating within the first supply circuit 2 passes through bypass 41.
• the second embodiment allows the distribution of the evaporation of the gas circulating in the first supply circuit 2 between the portion 50 via the high pressure evaporator 11 and the bypass channel 41 via the second exchanger heat 7.
• An evaporation connection carried out in parallel makes it possible to limit the activity of the high pressure evaporator 11 and therefore to partly save the energy necessary for its operation when all of the gas circulating in the first circuit of feed 2 is treated by the high pressure evaporator 11.
• the distribution valve 47 When there is no gas to be recondensed circulating in the return line 14, and the heat exchange is not taking place within the second heat exchanger 7, the distribution valve 47 is closed, er this in order to circulate the gas entirely within the portion 50 so that this last evening treated by the high pressure evaporator 11.
• the return line 14 can include the main section 56, then split into the first section 51 and into the second section 52 from the divergence zone 53. Cerre last is always positioned downstream of the second heat exchanger 7.
• the operation of the return line 14 as illustrated in Figure 3 is identical to what has been described in Figure 2.
• FIG. 4 is a cutaway view of a floating structure 20 which shows the tank 8 which contains the gas in the liquid state and in the vapor state, the tank 8 being of generally prismatic shape mounted in a double hull 22 of the floating structure 20.
• the wall of the tank 8 comprises a primary eranchéiré membrane intended to be in contact with the gas at the liquid érar contained in the tank 8, a secondary eranchéiré membrane arranged between the eranchéiré membrane primary and the double hull 22 of the structure floating 20, and two thermally insulating barriers arranged respectively between the primary sealing membrane and the secondary sealing membrane and between the secondary sealing membrane and the double shell 22.
• Lines 23 for loading and/or unloading gas in the liquid state arranged on the upper deck of the floating structure 20 can be connected, by means of appropriate connectors, to a maritime or port terminal to transfer the cargo of gas in the liquid state from or to the tank 8.
• FIG. 4 also represents an example of a maritime or port terminal comprising loading and/or unloading equipment 25, an underwater pipeline 26 and an onshore and/or port installation 27.
• the onshore and/or port installation 27 can for example be arranged on the quay of a port, or according to another example be arranged on a concrete gravity platform.
• the onshore and/or port installation 27 comprises liquid state gas storage tanks 30 and connecting pipes 31 connected by the underwater pipe 26 to the loading and/or unloading equipment 25.
• pumps fitted to the onshore and/or port installation 27 and/or pumps fitted to the floating structure 20 are used.
• the invention achieves the object it had set itself, and makes it possible to propose a gas supply system for appliances consuming gas at high or low pressure whose the high pressure is made using pumps and an evaporator, comprising a means of condensing a gas in the vapor state before its return to the tank as well as a supply of high pressure gas making it possible to optimize the energy used for the high pressure of said gas.
• Variants not described here could be implemented without departing from the context of the invention, since, in accordance with the invention, they comprise a supply system in accordance with the invention.

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• 2021
  • 2021-01-19 FR FR2100468A patent/FR3119013B1/fr active Active
• 2022
  • 2022-01-14 JP JP2023543228A patent/JP2024503496A/ja active Pending
  • 2022-01-14 KR KR1020237027756A patent/KR20230134137A/ko unknown
  • 2022-01-14 CN CN202280009865.7A patent/CN116710725A/zh active Pending
  • 2022-01-14 EP EP22712602.6A patent/EP4281718A1/fr active Pending
  • 2022-01-14 WO PCT/FR2022/050089 patent/WO2022157446A1/fr active Application Filing

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