US3768271A - Method and plant for storing and transporting a liquefied combustible gas - Google Patents
Method and plant for storing and transporting a liquefied combustible gas Download PDFInfo
- Publication number
- US3768271A US3768271A US3768271DA US3768271A US 3768271 A US3768271 A US 3768271A US 3768271D A US3768271D A US 3768271DA US 3768271 A US3768271 A US 3768271A
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- United States
- Prior art keywords
- gas
- inert gas
- container
- liquefied
- expanded
- Prior art date
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- 238000000034 method Methods 0.000 title claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000007789 gas Substances 0.000 claims abstract description 75
- 239000011261 inert gas Substances 0.000 claims abstract description 48
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 230000006835 compression Effects 0.000 claims description 14
- 238000007906 compression Methods 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 5
- 238000005057 refrigeration Methods 0.000 claims description 5
- 239000000567 combustion gas Substances 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 241000269627 Amphiuma means Species 0.000 claims description 2
- 239000003546 flue gas Substances 0.000 claims description 2
- 150000002829 nitrogen Chemical class 0.000 claims description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 48
- 238000001704 evaporation Methods 0.000 abstract description 8
- 230000008020 evaporation Effects 0.000 abstract description 7
- 239000003345 natural gas Substances 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000008030 elimination Effects 0.000 description 2
- 238000003379 elimination reaction Methods 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003949 liquefied natural gas Substances 0.000 description 1
- 238000004172 nitrogen cycle Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0015—Nitrogen
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—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"
- F25J1/0035—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 gas expansion with extraction of work
- F25J1/0037—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 gas expansion with extraction of work of a return stream
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—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
- F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
- F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—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
- F25J1/0251—Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2221/00—Handled fluid, in particular type of fluid
- F17C2221/01—Pure fluids
- F17C2221/014—Nitrogen
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- F17C2221/00—Handled fluid, in particular type of fluid
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- F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
- 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
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- 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
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- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
Definitions
- cryogenic plants it is occasionally required to alternately liquefy one of two gases, depending on the phases of operation of the plant.
- an inert gas usually nitrogen
- an inert gas usually nitrogen
- such vessels are equipped with liquid nitrogen tanks or with inert-gas generators.
- the ship consumes in its propulsion machinery the natural gas that evaporates from the tanks, or approximately 0.1 to 0.3 percent of the transported quantity daily. More often'than not a good state of equilibrium exists between evaporation on the one hand and consumption by the ships boilers or engines on the other, but if the engines must be slowed or stopped there is a surplus of evaporated gas and the problems of eliminating it then arise and have heretofore been unsatisfactorily resolved.
- the fourth mode corresponds to the phase. of ap-. proach to the terminal port and the time during which the ship is laid up with its engines stopped. In this case it is impossible to burn the gas in the engines. since ship propulsion requirements are minimal or nil, so that elimination of the evaporated gas poses problems heretofore unresolved.
- a fifth mode corresponds to the unloading phase. In this case it is usually possible to discharge the evaporated gas to land through pipes provided for the purpose.
- a sixth mode corresponds to the degassing phase, namely the discharging into the atmosphere of the gas contained in the empty tanks, in conjunction with the process of filling with nitrogen and the subsequent entry of atmospheric air.
- This operation requires a certain amount of nitrogen which is produced by an inertgas generator or a store of liquid nitrogen, and in order to accomplish all the above-mentioned operations a very large stock of liquid nitrogen may be carried on board, namely approximately one ton of liquid nitrogen for every thousand cubic metres of natural gas tankag e.
- methane tankers involves two requirements which it has heretofore been the custom to meet separately.
- One is the production and/or storage of liquid nitrogen, the other is the elimination of evaporated natural gas when consumption of the latter is slowed or arrested by design or not when the vessels propulsion system is slowed or stopped on reaching port.
- the present invention rests on the discovery that it is possible to meet both these requirements together under satisfactory conditions. i
- the inert gas is liquefied by making use of additional energy derived from the evaporation of the combustible gas, or else the evaporated combustible gas is reliquefied by making use of the evaporation of the liquid inert gas, as the case may be.
- the associated plant or equipment most notably for a methane tanker, includes a machine capable of receiving surplus energy for assuring the two hereinspecified operating modes in alternation, some at least of the component parts of said machine being used for both operating modes.
- FIG. 1 is a schematic diagram of the overall arrangement of a plant according to this invention, as used aboard a methane tanker
- FIG. 2 shows the same plant adapted for producing liquid nitrogen
- FIG. 3 shows the same plant adapted for reliquefying natural gas.
- FIGS. 2 and 3 the piping circuits which are in service are shown in bold lines, while the others, which are inoperative through closure of appropriate cocks and valves, are shown in fine lines.
- the plant includes a turbo-compressor set consisting of an alternating or rotary compressor 1 coupled either directly or through gearing to a reciprocating or rotary expansion engine 2 and to an extra-power motor 3, which motor may be an electric motor or a heat or steam engine, or be formed of a plurality of motors.
- a turbo-compressor set consisting of an alternating or rotary compressor 1 coupled either directly or through gearing to a reciprocating or rotary expansion engine 2 and to an extra-power motor 3, which motor may be an electric motor or a heat or steam engine, or be formed of a plurality of motors.
- it is powered with natural gas taken from the natural gas transported in the ship.
- the plant includes a plurality of heat-exchangers, the drawings most clearly showing the cooling exchanger 4 which utilizes water supplied by the ships cooling network 5, and the cooling exchanger 6 which in this case involves four separate fluid flow-paths 6a, 6b, 6c, 6d.
- the plant further comprises a liquid nitrogen separator 7 and a natural gas liquefier 8 liquid methane tanks as represented by the tank 9,
- tank 10 Y a natural-gas-fired boiler 11, the combustion smokes from which are discharged through the stack 12 and associated pipes, valves (see below) and other gear.
- the gaseous nitrogen generator 13 When it is required to produce nitrogen, the gaseous nitrogen generator 13 is activated and extracts the carbon dioxide from the stack tains the nitrogen.
- the cycle generated by the turbine engine 1-2 can be designed to work at atmospheric pressure during suction of compressor 1.
- a two-pressure cycle could be used, in which the lower pressure would be higher than atmospheric pressure.
- the gaseous nitrogen produced by generator 13 is compressed by a booster 14 driven by an appropriate motor 15.
- valves allow of establishing different circuits for performance of the plants different functions, these valves being designated from left to right by reference numerals 16, 17 33, 34 (only the valves relevant to the present description being shown on the drawing).
- valve 26 When valve 26 is open it allows boiler 11 to be fed directly with evaporated gas without passing through the heat exchanger 6 when the production of nitrogen is stopped.
- valve 27 When valve 27 is open, the ships ancillary systems and services are supplied with nitrogen in the gaseous state.
- the plant is capable of operating in at least two different ways in a first operating mode liquid nitrogen is produced
- the shaft lines 1, 2, 3 and l4, are set in rotation, and the evaporated gas is caused to pass through open valve 24 and heat exchanger circuit 6d, where the evaporated gas at around 161.4 C relinquishes its frigories and issues at around 40 C in order to feed the boiler 11 through open valve 25.
- the plant achieves steady-state operating conditions when it liquefies a quantity of nitrogen equal to the nitrogen produced by the generator. Production of liquid nitrogen is facilitated by the extra cold which is produced by the methane evaporated in tanks 9 and which is given up in heat exchanger 6.
- the plant may be designed to produce liquid nitrogen without extra cold from methane evaporation in the tanks 9 (e.g., when the latter are waiting to be filled with, or else no longer contain any, liquefied methane), in which case the extra power supplied by motors 3 and 15 will attain its highest level, these motors being accordingly designed to be capable of continuous operation under these conditions without being overloaded.
- the plant In a second operating mode, the plant is devised in such manner as to reliquefy the evaporated natural gas from the tanks 9.
- Liquid nitrogen is conveyed from tank 10 (assumed to already contain liquid nitrogen from a previous operation or an external source) to cooling heat-exchanger 6b and issues therefrom under gravity, pressure or pumping. This additional cooling effect enables the nitrogen refrigeration cycle to be initiated in a closed circuit.
- the plant will achieve steady operating conditions when the extra frigories provided by the liquid nitrogen and the extra energy provided by the motor 3 allow all the evaporated gas from the tanks to be liquefied in the condenser 8, the liquid procuded in this way returning to tank 9 through open valve 17.
- the liquid nitrogen is evaporated and heats up in the circuit 6b of heat-exchanger 6 and is discharged to the stack at a temperature of approvimately 20 C to 30 C.
- a plant devised according to this invention allows of accomplishing two entirely different functions, to wit, producing liquid nitrogen and reliquefying the natural gas evaporating from the methane tankers tanks, These functions are moreover performed by utilizing the same basic elements, namely the liquefaction line formed by compressor 1, turbine 2, motor 3, heatexchanger 4 and heat-exchanger 6, an important feature of the invention being this dual function of the elements 1, 2, 3, 4 6.
- a system for handling a liquefiable combustible gas for storage and transportion including a container for liquefiable inert gas in liquid form, a container for a liquefiable combustible gas in liquid form, a source of said inert gas in gaseous form, and a source of said combustible gas in gaseous form, an improved arrangement for optionally liquefying a selected one of said gases in gaseous form for delivery to the corresponding container comprising:
- a. means for circulating said inert gas through a refrigeration cycle including an expansion stage, a compression stage, and power means for supplying to said compression stage at least a portion of the energy required thereby;
- said combusting means is a boiler and including further means for treating the resulting smoke, which further means include means for eliminating the carbon dioxide from the smoke whereby to extract nitrogen inert gas therefrom, and a booster connected to said circulating means for compressing this nitrogen and injecting it into said circulating means whereby to liquefy it.
- a liquefiable combustible gas for storage and transportion including a container for liquefiable inert gas in liquid form, a container for a liquefiable combustible gas in liquid form, a source of said inert gas in gaseous form, and a source of said combustible gas in gaseous form, an improved arrangement for optionally liquefying a :selected one of said gases in gaseous form for delivery 'to the corresponding container comprising:
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Abstract
For the purpose of storing and transporting a liquefied combustible gas, in a methane tanker for example, together with a virtually inert gas such as nitrogen in contact with said combustible gas, use is made of additional energy either, as the case may be, in order to liquefy the inert gas - utilizing the evaporation of the combustible gas to that end - or in order to reliquefy the evaporated combustible gas - utilizing the evaporation of the liquid inert gas to that end.
Description
United States Patent Denis Oct. 30, 1973 [54] METHOD AND PLANT FOR STORING AND 3,313,116 4/1967 Nonnecke et al 62/45 A 2223222 2/:222 w-..- as:
, 1 rams et a COMBUSTIBLE GAS 3,000,707 9/196] Barstow 23/281 [76] Inventor: Louis Henri Daniel Denis, 43, rue
Raffet Paris France Primary Examiner-Meyer Perlin [22] Filed: J n. 18, 1972 Assistant Examiner-Ronald C. Capossela Attorney-William J. Daniel [21] Appl. No; 218,738
[30] Foreign Application Priority Data [57] ABSTRACT Jan. 19, 1971 France 7101682 For the P p Of Storing and transporting a liquefied combustible gas, in a methane tanker for example, to- 52 0.8. Ci. 62/55, 23/281 220/88 B with a virtually gas Such as 51 Int. Cl. Fl7c 7/02 intact with Said ciimbustibie gas, use is made addi- 58 Field 0! Search 62/45 55- 114/74 A- iimai ewgy eithe" as the case may g 23/281 liquefy the inert gas utilizing the evaporation of the combustible gas to that end or in order to reliquefy [56] References Cited the evaporated combustible gas utilizing the evapo- UNITED STATES PATENTS ration of the liquid inert gas to that end.
3,365,898 1/1968 VanKleff 62/55 9 Claims, 3 Drawing Figures 1 l 30 32 j 78 I] i 22 5 4 3 v 29 MW vv WWW g 34 M16 2 8 M W 5 15 2 7 pi; i 2/ E 21 f l zs METHOD AND PLANT FOR STORING AND TRANSPORTING A LIQUEFIED COMBUSTI BLE GAS This invention covers a method and a plant for storing and transporting a liquefied combustible gas, such asthe plant aboard a methane tanker, in which use is made of a virtually inert gas such as nitrogen which may be in contact with the combustible gas and exist likewise in liquid form in the plant.
In certain cryogenic plants it is occasionally required to alternately liquefy one of two gases, depending on the phases of operation of the plant.
A case in point arises with ships used to transport liquid hydrocarbon gases, usually methane tankers. In such vessels several possible operating modes or phases exist, with variants in each case.
In one mode of operation, when the tanker is travelling empty towards its loading port, an inert gas, usually nitrogen, is required in order to place and maintain the liquefied natural gas tanks in a neutral atmosphere until the port is reached. For this reason such vessels are equipped with liquid nitrogen tanks or with inert-gas generators.
In a second mode, corresponding to the tanker loading phase, a similar requirement for liquid nitrogen exists during these operations in order to maintain the atmosphere neutral before the methane gas fills all the spaces not occupied by the fuel.
In a third mode, when the loaded tanker leaves the port on its way to the terminal port, the ship consumes in its propulsion machinery the natural gas that evaporates from the tanks, or approximately 0.1 to 0.3 percent of the transported quantity daily. More often'than not a good state of equilibrium exists between evaporation on the one hand and consumption by the ships boilers or engines on the other, but if the engines must be slowed or stopped there is a surplus of evaporated gas and the problems of eliminating it then arise and have heretofore been unsatisfactorily resolved.
The fourth mode corresponds to the phase. of ap-. proach to the terminal port and the time during which the ship is laid up with its engines stopped. In this case it is impossible to burn the gas in the engines. since ship propulsion requirements are minimal or nil, so that elimination of the evaporated gas poses problems heretofore unresolved.
A fifth mode corresponds to the unloading phase. In this case it is usually possible to discharge the evaporated gas to land through pipes provided for the purpose.
A sixth mode corresponds to the degassing phase, namely the discharging into the atmosphere of the gas contained in the empty tanks, in conjunction with the process of filling with nitrogen and the subsequent entry of atmospheric air. This operation requires a certain amount of nitrogen which is produced by an inertgas generator or a store of liquid nitrogen, and in order to accomplish all the above-mentioned operations a very large stock of liquid nitrogen may be carried on board, namely approximately one ton of liquid nitrogen for every thousand cubic metres of natural gas tankag e.
Thus the operation of methane tankers involves two requirements which it has heretofore been the custom to meet separately. One is the production and/or storage of liquid nitrogen, the other is the elimination of evaporated natural gas when consumption of the latter is slowed or arrested by design or not when the vessels propulsion system is slowed or stopped on reaching port.
As stated precedingly, this second requirement has been met unsatisfactorily or not at all heretofore.
The present invention rests on the discovery that it is possible to meet both these requirements together under satisfactory conditions. i
To that end and in accordance with the subject method of this invention, which may be used for storing and transporting a liquefied combustible gas with a virtually inert gas in contact therewith, the inert gas is liquefied by making use of additional energy derived from the evaporation of the combustible gas, or else the evaporated combustible gas is reliquefied by making use of the evaporation of the liquid inert gas, as the case may be.
The associated plant or equipment, most notably for a methane tanker, includes a machine capable of receiving surplus energy for assuring the two hereinspecified operating modes in alternation, some at least of the component parts of said machine being used for both operating modes.
The description which follows of a possible embodiment of the invention, given with reference to the accompanying non-limitative exemplary drawings, will provide a clear understanding of how the invention can be carried into practice.
In the drawings FIG. 1 is a schematic diagram of the overall arrangement of a plant according to this invention, as used aboard a methane tanker FIG. 2 shows the same plant adapted for producing liquid nitrogen and i FIG. 3 shows the same plant adapted for reliquefying natural gas.
In FIGS. 2 and 3, the piping circuits which are in service are shown in bold lines, while the others, which are inoperative through closure of appropriate cocks and valves, are shown in fine lines.
In the embodiment shown in the: drawings, the plant includes a turbo-compressor set consisting of an alternating or rotary compressor 1 coupled either directly or through gearing to a reciprocating or rotary expansion engine 2 and to an extra-power motor 3, which motor may be an electric motor or a heat or steam engine, or be formed of a plurality of motors. Preferably, it is powered with natural gas taken from the natural gas transported in the ship.
The plant includes a plurality of heat-exchangers, the drawings most clearly showing the cooling exchanger 4 which utilizes water supplied by the ships cooling network 5, and the cooling exchanger 6 which in this case involves four separate fluid flow-paths 6a, 6b, 6c, 6d.
The plant further comprises a liquid nitrogen separator 7 and a natural gas liquefier 8 liquid methane tanks as represented by the tank 9,
and liquid nitrogen tanks as represented by the tank 10 Y a natural-gas-fired boiler 11, the combustion smokes from which are discharged through the stack 12 and associated pipes, valves (see below) and other gear.
When it is required to produce nitrogen, the gaseous nitrogen generator 13 is activated and extracts the carbon dioxide from the stack tains the nitrogen.
The cycle generated by the turbine engine 1-2 can be designed to work at atmospheric pressure during suction of compressor 1. Alternatively, a two-pressure cycle could be used, in which the lower pressure would be higher than atmospheric pressure. In this latter event, as well as in certain operating modes, the gaseous nitrogen produced by generator 13 is compressed by a booster 14 driven by an appropriate motor 15.
Manually-operated or automatic isolating valves allow of establishing different circuits for performance of the plants different functions, these valves being designated from left to right by reference numerals 16, 17 33, 34 (only the valves relevant to the present description being shown on the drawing).
When valve 26 is open it allows boiler 11 to be fed directly with evaporated gas without passing through the heat exchanger 6 when the production of nitrogen is stopped.
When valve 27 is open, the ships ancillary systems and services are supplied with nitrogen in the gaseous state.
As indicated precedingly, the plant is capable of operating in at least two different ways in a first operating mode liquid nitrogen is produced,
and for exemplary purposes the case will be taken of a refrigerating system the lower pressure of which'is higher than atmospheric pressure.
As shown in FIG. 2, this is accomplished by opening the valves 19, 20, 22, 24, 25, 28, 29, 31, 32, 33 and closing the valves 16, 17, 18, 21, 23, 26, 30, 34.
The shaft lines 1, 2, 3 and l4, are set in rotation, and the evaporated gas is caused to pass through open valve 24 and heat exchanger circuit 6d, where the evaporated gas at around 161.4 C relinquishes its frigories and issues at around 40 C in order to feed the boiler 11 through open valve 25.
The operating conditions of a nitrogen-cycle refrigerating machine are accordingly established this way, the nitrogen being delivered under pressure and cooled in separator 7, whence the liquid nitrogen is discharged into tank 10, while the cold gaseous nitrogen under pressure is directed to the inlet side of expansion turbine 2.
The plant achieves steady-state operating conditions when it liquefies a quantity of nitrogen equal to the nitrogen produced by the generator. Production of liquid nitrogen is facilitated by the extra cold which is produced by the methane evaporated in tanks 9 and which is given up in heat exchanger 6.
Alternatively, the plant may be designed to produce liquid nitrogen without extra cold from methane evaporation in the tanks 9 (e.g., when the latter are waiting to be filled with, or else no longer contain any, liquefied methane), in which case the extra power supplied by motors 3 and 15 will attain its highest level, these motors being accordingly designed to be capable of continuous operation under these conditions without being overloaded.
In a second operating mode, the plant is devised in such manner as to reliquefy the evaporated natural gas from the tanks 9.
As shown in FIG. 3, this is accimplished by opening the valves 16, 17, 18, 21, 23, 34 and closing the valves 19, 20, 22, 24, 25, 26, 28, 30, 32, 33.
gases (C0, N and re- Boiler 11 and generator 13 are shut off and the shaft lines 1, 2, 3 and 14, 15 are set rotating. Liquid nitrogen is conveyed from tank 10 (assumed to already contain liquid nitrogen from a previous operation or an external source) to cooling heat-exchanger 6b and issues therefrom under gravity, pressure or pumping. This additional cooling effect enables the nitrogen refrigeration cycle to be initiated in a closed circuit.
The plant will achieve steady operating conditions when the extra frigories provided by the liquid nitrogen and the extra energy provided by the motor 3 allow all the evaporated gas from the tanks to be liquefied in the condenser 8, the liquid procuded in this way returning to tank 9 through open valve 17.
The liquid nitrogen is evaporated and heats up in the circuit 6b of heat-exchanger 6 and is discharged to the stack at a temperature of approvimately 20 C to 30 C.
Thus a plant devised according to this invention allows of accomplishing two entirely different functions, to wit, producing liquid nitrogen and reliquefying the natural gas evaporating from the methane tankers tanks, These functions are moreover performed by utilizing the same basic elements, namely the liquefaction line formed by compressor 1, turbine 2, motor 3, heatexchanger 4 and heat-exchanger 6, an important feature of the invention being this dual function of the elements 1, 2, 3, 4 6.
The efficiency and economics of the plant are thus considerably increased, making the plant economically viable aboard a methane tanker. This contrasts with liquid nitrogen producing plants or methane reliquefying plants devised in conventional fashion or as individual systems, which are of debatable profitability.
It goes without saying that the invention has been described in schematic form only, but with sufficient clarity for the specialist in the art to be able to carry it into practice without I difficulty. Obviously, alternatives could be introduced in the exemplary schematic form described herein, and for instance the heat-exchanger 6 could be devised as a plurality of separate elements grouped in series or in parallel. It will therefore be manifest that many changes and substitutions of parts could be made without departing from the scope of the invention as defined by the claims.
I claim:
1. In a system for handling a liquefiable combustible gas for storage and transportion, including a container for liquefiable inert gas in liquid form, a container for a liquefiable combustible gas in liquid form, a source of said inert gas in gaseous form, and a source of said combustible gas in gaseous form, an improved arrangement for optionally liquefying a selected one of said gases in gaseous form for delivery to the corresponding container comprising:
a. means for circulating said inert gas through a refrigeration cycle including an expansion stage, a compression stage, and power means for supplying to said compression stage at least a portion of the energy required thereby;
b. heat exchange means through which said circulating inert gas passes while in expanded cooled condition;
c. means for expanding one of said gases from its liquefied form in the corresponding container and passing the expanded cooled gas through said heat exchanger;
d. means for applying the cooling effect of said two expanded gases to the selected gas from its source to liquefy said gas; and
e. means for delivering the thus liquefied gas to the container therefor.
2. The system according to claim 1 including f. means for passing surplus expanded combustion gas from said liquefied combustion gas container in heat exchange relation with said cooled inert gas to re-liquefy the same for return to said container, liquefied inert gas from the container thereof being expanded to cool the same and passed in cooled condition through said heat exchange means (b).
3. The system according to claim 2 wherein compressed inert gas from said compression stage is cooled by passage through said heat exchange means (b) and then passed in heat exchange relation with said expanded combustible gas in means (f).
4. The system according to claim 1 wherein said inert gas after compression in said compression stage is cooled to liquefy the same and a fraction of said liquefied inert gas is delivered to said inert gas container, and make-up fresh inert gas from said sourcethereof is added to said circulating means.
5. The system according to claim 4 wherein said compressed inert gas is cooled by passage through said heat exchange (b) 6. The system according to claim 4 including means for combusting said combustible gas and wherein said inert gas is extracted from the flue gases of said combusting means.
7. The system according to claim 6 wherein said combusting means is a boiler and including further means for treating the resulting smoke, which further means include means for eliminating the carbon dioxide from the smoke whereby to extract nitrogen inert gas therefrom, and a booster connected to said circulating means for compressing this nitrogen and injecting it into said circulating means whereby to liquefy it.
8. The system according to claim 6 wherein liquefied combustible gas from said container thereof is expanded and passed through said heat exchange means before being combusted in said combusting means.
9. In a method of handling a liquefiable combustible gas for storage and transportion, including a container for liquefiable inert gas in liquid form, a container for a liquefiable combustible gas in liquid form, a source of said inert gas in gaseous form, and a source of said combustible gas in gaseous form, an improved arrangement for optionally liquefying a :selected one of said gases in gaseous form for delivery 'to the corresponding container comprising:
a. circulating said inert gas through a refrigeration cycle including an expansion stage, a compression stage, while supplying to said compression stage at least a portion of the power required thereby;
b. passing said circulating inert gas while in expanded cooled condition through a heat exchanging zone;
c. expanding one of said gases from its liquefied form in the corresponding container and passing the expanded cooled gas through said heat exchanging zone;
d. applying the cooling effect of said two expanded gases to the selected gas from its source to liquefy said gas; and
e. delivering the thus liquefied gas to the container therefor.
Claims (9)
1. In a system for handling a liquefiable combustible gas for storage and transportion, including a container for liquefiable inert gas in liquid form, a container for a liquefiable combustible gas in liquid form, a source of said inert gas in gaseous form, and a source of said combustible gas in gaseous form, an improved arrangement for optionally liquefying a selected one of said gases in gaseous form for delivery to the corresponding container comprising: a. means for circulating said inert gas through a refrigeration cycle including an expansion stage, a compression stage, and power means for supplying to said compression stage at least a portion of the energy required thereby; b. heat exchange means through which said circulating inert gas passes while in expanded cooled condition; c. means for expanding one of said gases from its liquefied form in the corresponding container and passing the expanded cooled gas through said heat exchanger; d. means for applying the cooling effect of said two expanded gases to the selected gas from its source to liquefy said gas; and e. means for delivering the thus liquefied gas to the container therefor.
2. The system according to claim 1 including f. means for passing surplus expanded combustion gas from said liquefied combustion gas container in heat exchange relation with said cooled inert gas to re-liquefy the same for return to said container, liquefied inert gas from the container thereof being expanded to cool the same and passed in cooled condition through said heat exchange means (b).
3. The system according to claim 2 wherein compressed inert gas from said compression stage is cooled by passage through said heat exchange means (b) and then passed in heat exchange relation with said expanded combustible gas in means (f).
4. The system according to claim 1 wherein said inert gas after compression in said compression stage is cooled to liquefy the same and a fraction of said liquefied inert gas is delivered to said inert gas container, and make-up fresh inert gas from said source thereof is added to said circulating means.
5. The system according to claim 4 wherein said compressed inert gas is cooled by passage through said heat exchange (b).
6. The system according to claim 4 including means for combusting said combustible gas and wherein said inert gas is extracted from the flue gases of said combusting means.
7. The system according to claim 6 wherein said combusting means is a boiler and including further means for treating the resulting smoke, which further means include means for eliminating the carbon dioxide from the smoke whereby to extract nitrogen inert gas therefrom, and a booster connected to said circulating means for compressing this nitrogen and injecting it into said circulating means whereby to liquefy it.
8. The system according to claim 6 wherein liquefied combustible gas from said container thereof is expanded and passed through said heat exchange means before being combusted in said combusting means.
9. In a method of handling a liquefiable combustible gas for storage and transportion, including a container for liquefiable inert gas in liquid form, a container for a liquefiable combustible gas in liquid form, a source of said inert gas in gaseous form, and a source of said combustible gas in gaseous form, an improved arrangement for optionally liquefying a selected one of said gases in gaseous form for delivery to the corresponding container comprising: a. circulating said inert gas through a refrigeration cycle including an expansion stage, a compression stage, while supplying to said compression stage at least a portion of the power required thereby; b. passing said circulating inert gas while in expanded cooled condition through a heat exchanging zone; c. expanding one of said gases from its liquefied form in the corresponding container and passing the expanded cooled gas through said heat exchanging zone; d. applying the cooling effect of said two expanded gases to the selected gas from its source to liquefy said gas; and e. delivering the thus liquefied gas to the container therefor.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
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FR7101682A FR2122307B1 (en) | 1971-01-19 | 1971-01-19 |
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US3768271D Expired - Lifetime US3768271A (en) | 1971-01-19 | 1972-01-18 | Method and plant for storing and transporting a liquefied combustible gas |
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US3365898A (en) * | 1965-06-03 | 1968-01-30 | Shell Oil Co | Method for transporting gas |
US3400547A (en) * | 1966-11-02 | 1968-09-10 | Williams | Process for liquefaction of natural gas and transportation by marine vessel |
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US3885394A (en) * | 1972-12-11 | 1975-05-27 | Sulzer Ag | Process and apparatus for treating and utilizing vaporized gas in a ship for transporting liquified gas |
WO1980001103A1 (en) * | 1978-11-15 | 1980-05-29 | Minnesota Mining & Mfg | Heat and liquid recovery using open cycle heat pump system |
EP0020645A1 (en) * | 1978-11-15 | 1981-01-07 | Minnesota Mining & Mfg | Heat and liquid recovery using open cycle heat pump system. |
EP0020645A4 (en) * | 1978-11-15 | 1981-10-13 | Minnesota Mining & Mfg | Heat and liquid recovery using open cycle heat pump system. |
US4295282A (en) * | 1978-11-15 | 1981-10-20 | Minnesota Mining And Manufacturing Company | Heat and liquid recovery using open cycle heat pump system |
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US5176002A (en) * | 1991-04-10 | 1993-01-05 | Process Systems International, Inc. | Method of controlling vapor loss from containers of volatile chemicals |
US5678411A (en) * | 1995-04-26 | 1997-10-21 | Ebara Corporation | Liquefied gas supply system |
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WO2001057430A1 (en) * | 2000-02-03 | 2001-08-09 | Cabot Lng Llc | Vapor recovery system using turboexpander-driven compressor |
US6460350B2 (en) | 2000-02-03 | 2002-10-08 | Tractebel Lng North America Llc | Vapor recovery system using turboexpander-driven compressor |
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US20040083756A1 (en) * | 2002-11-01 | 2004-05-06 | Jean-Pierre Tranier | Combined air separation natural gas liquefaction plant |
US7143606B2 (en) | 2002-11-01 | 2006-12-05 | L'air Liquide-Societe Anonyme A'directoire Et Conseil De Surveillance Pour L'etide Et L'exploitation Des Procedes Georges Claude | Combined air separation natural gas liquefaction plant |
US20080016879A1 (en) * | 2002-12-09 | 2008-01-24 | Dresser, Inc. | System and method of use of expansion engine to increase overall fuel efficiency |
US7287389B2 (en) * | 2003-03-20 | 2007-10-30 | Snecma Moteurs | Feeding energy to a gas terminal from a ship for transporting liquefied gas |
US20040182090A1 (en) * | 2003-03-20 | 2004-09-23 | Snecma Moteurs | Feeding energy to a gas terminal from a ship for transporting liquefied gas |
US8069677B2 (en) | 2006-03-15 | 2011-12-06 | Woodside Energy Ltd. | Regasification of LNG using ambient air and supplemental heat |
US20070214804A1 (en) * | 2006-03-15 | 2007-09-20 | Robert John Hannan | Onboard Regasification of LNG |
US20070214805A1 (en) * | 2006-03-15 | 2007-09-20 | Macmillan Adrian Armstrong | Onboard Regasification of LNG Using Ambient Air |
US8607580B2 (en) | 2006-03-15 | 2013-12-17 | Woodside Energy Ltd. | Regasification of LNG using dehumidified air |
US20070214806A1 (en) * | 2006-03-15 | 2007-09-20 | Solomon Aladja Faka | Continuous Regasification of LNG Using Ambient Air |
US20090199575A1 (en) * | 2006-09-11 | 2009-08-13 | Woodside Energy Limited | Boil off gas management during ship-to-ship transfer of lng |
US20090193780A1 (en) * | 2006-09-11 | 2009-08-06 | Woodside Energy Limited | Power Generation System for a Marine Vessel |
US20090314005A1 (en) * | 2007-12-21 | 2009-12-24 | Green Partners Technology Gmbh | Piston engine systems and methods |
US8739569B2 (en) * | 2008-02-27 | 2014-06-03 | Mitsubishi Heavy Industries, Ltd. | Liquefied gas reliquefier, liquefied-gas storage facility and liquefied-gas transport ship including the same, and liquefied-gas reliquefaction method |
US20100170297A1 (en) * | 2008-02-27 | 2010-07-08 | Masaru Oka | Liquefied gas reliquefier, liquefied-gas storage facility and liquefied-gas transport ship including the same, and liquefied-gas reliquefaction method |
WO2010128466A2 (en) * | 2009-05-08 | 2010-11-11 | Corac Group Plc | Production and distribution of natural gas |
WO2010128466A3 (en) * | 2009-05-08 | 2011-12-29 | Corac Group Plc | Production and distribution of natural gas |
US20110030391A1 (en) * | 2009-08-06 | 2011-02-10 | Woodside Energy Limited | Mechanical Defrosting During Continuous Regasification of a Cryogenic Fluid Using Ambient Air |
US8499567B2 (en) * | 2011-06-27 | 2013-08-06 | Honeywell International, Inc. | Hybrid fuel tank inerting system |
US20120325811A1 (en) * | 2011-06-27 | 2012-12-27 | Honeywell International Inc. | Hybrid fuel tank inerting system |
US10539361B2 (en) | 2012-08-22 | 2020-01-21 | Woodside Energy Technologies Pty Ltd. | Modular LNG production facility |
WO2015063453A3 (en) * | 2013-10-28 | 2015-08-27 | Highview Enterprises Limited | Method and system for the re-liquefaction of boil-off gas |
CN105683690A (en) * | 2013-10-28 | 2016-06-15 | 高维有限公司 | Method and system for the re-liquefaction of boil-off gas |
JP2016535211A (en) * | 2013-10-28 | 2016-11-10 | ハイヴュー・エンタープライゼズ・リミテッド | Method and system for reliquefaction of boil-off gas |
CN105683690B (en) * | 2013-10-28 | 2020-03-13 | 高维有限公司 | Method and system for reliquefying boil-off gas |
US11402152B2 (en) * | 2017-07-07 | 2022-08-02 | Tor Christensen | Large scale coastal liquefaction |
Also Published As
Publication number | Publication date |
---|---|
FR2122307A1 (en) | 1972-09-01 |
FR2122307B1 (en) | 1975-01-17 |
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