US2783624A - Method of liquefying gas - Google Patents
Method of liquefying gas Download PDFInfo
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- US2783624A US2783624A US248973A US24897351A US2783624A US 2783624 A US2783624 A US 2783624A US 248973 A US248973 A US 248973A US 24897351 A US24897351 A US 24897351A US 2783624 A US2783624 A US 2783624A
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- temperature
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- 238000000034 method Methods 0.000 title claims description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 42
- 239000007788 liquid Substances 0.000 claims description 27
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 238000009835 boiling Methods 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000000740 bleeding effect Effects 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 55
- 239000011261 inert gas Substances 0.000 description 6
- 239000003507 refrigerant Substances 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000004868 gas analysis Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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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
- F25J1/003—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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- 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
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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
- F25J1/0022—Hydrocarbons, e.g. natural gas
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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
- F25J1/0203—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
- F25J1/0228—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
- F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
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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
- F25J1/0243—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2201/00—Vessel construction, in particular geometry, arrangement or size
- F17C2201/05—Size
- F17C2201/052—Size large (>1000 m3)
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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
- 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
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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
- 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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- 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
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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
- F17C2260/00—Purposes of gas storage and gas handling
- F17C2260/04—Reducing risks and environmental impact
- F17C2260/042—Reducing risk of explosion
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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
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/03—Treating the boil-off
- F17C2265/032—Treating the boil-off by recovery
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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
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/06—Fluid distribution
- F17C2265/066—Fluid distribution for feeding engines for propulsion
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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
- 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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- 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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
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- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T137/00—Fluid handling
- Y10T137/2496—Self-proportioning or correlating systems
- Y10T137/2514—Self-proportioning flow systems
- Y10T137/2516—Interconnected flow displacement elements
Definitions
- Methane must be lowered in temperature to approximately l15.8 degrees F. before it can be liquefied. Above that temperature no matter how great pressures are applied, it will not liquefy.
- the gases .of higher boiling point can be compressed or liquefied and stored and shipped in the usual type of commercial gas bottles or gas tanks though they require under ordinary circumstances bottles or tanks of great weight and strength.
- the refrigerant is recirculated or recycled through the system.
- the compressor and condenser will produce the liquefied methane at ap-.
- the liquid methane will then be discharged into an insulated portable receiver, will be allowed there to expand to atmospheric pressure with resultant sharp temperature drop of the liquid. This reduction in pressure will allow some of the gas to evaporate and will cool the remainder. The liquid will remain in the receiver.
- the evaporated gas will be returned to the system for further compression and liquefaction, the liquid left in the receiver being replaced by methane from the outside mixed with that which returns from the insulated receiver and this process will continue until a receiver of substantial size is substantially filled with liquefied methane at a temperature of approximately 258 degrees F. and .at a pressure of approximately atmospheric.
- the portable receiver When the portable receiver is filled with the liquefied 2 methane, if it were possible to so insulate it that no heat would be added to it, the methane would remain liquid without boiling or evaporation at the temperature of the receiver. Actually, of course, no matter how well insulated the receiver is, some heat is added. Thatheat causes the liquid to boil orevaporate and so gas is given off from the surface of the. liquid. This gas, unless released,would soon raise the pressure in thereceiver far above the safety point so it must be allowed to escape.
- the pressure in the receiver remains at a substantially constant level and evaporation continues at a rate dependent upon the rate at which heat is added.
- the liquid remains at the same temperature just as water re mains at the same temperature while it boils.
- This gas may be 'used to assist in maintaining the temperature of the remaining liquefied gas constant so as to control the rate at which heat is allowed to reach the mass of liquefied gas, and may then be used as fuel or for any other purpose desired.
- A is the first stage of refrigeration. It'includes compressor 1-, condenser 2, receiver 3, evaporator 4.
- B is the second stage of refrigeration. It includes a compressor 5, condenser 6, cooled by the evaporator 4 of stage A, a receiver 7 and an evaporator 8.
- a C is the final stage of refrigeration wherein 9 is a supply pipe bringing methane to the compressor 10, which discharges into the condenser 11, cooled by the evaporator8 of the B stage, discharging liquefied gas through a pipe 12 to a receiver tank 13 on the ship 14 insulated at 15. 16 is a return pipe for evaporated gas from the receiver tank 13 to the low pressure side of the compressor 10.
- pipe 19 is con nected to a pipe 21 on the shore and the methane under the residual pressure in the receiver 13 or the cold evaporated gas passes through the evaporator or heat exchanger 22 of a refrigerating system. Thereafter, the warm gas -is discharged through the pipe 23 to the burner 24 under the boiler 25.
- the particular details of the evaporator and the burner 3 'I l a form no part of my invention and are not illustrated.
- the gas may be used under a boiler.v It might be stored in a receiver on shore. It might be used as fuel for internal combustion engines or it might be burned in other heat processes, as desired. The point'is that after the cold methane from the receiver on the boat has been used to extract heat from something else, the warmed gas may then be used to generate power or heat as the case may be.
- the evaporated gas must be permitted to escape from the receiver tank at such a rate that the pressure in the tank does not rise above a predetermined maximum so any excess of evaporated gas must be permitted to escape freely to the'atmosphere, at a pressure, but slightly above atmospheric, set by the relief valve 18 in the discharge pipe 26. So long as the engine uses gas at a rate not greater than the-evaporation rate, all the gas passes through the engine and is there burned.
- the relief valve 18 permits gas to discharge through the pipe 26- from the engine supply pipe 19 to a mixing nozzle 27 where the methane is mixed with an inert: gaswhich reaches the nozzle through a pipe 28 from the inert gas reservoir 29.
- a control mechanism 30 automatically opens the supply pipe for the inert gas whenthe pressure in the line between the receiver and'th'e engine exceeds the safety point so that the inert gas is automatically mixed with hydrocarbon vapor when that is discharged to the atmosphere.
- an inertor at least a non-explosive, non-poisonous mixture will be'dischargedto the atmosphere.
- 31 indicates a gas analysis mechanism.
- This gas analysis mechanism is so adjusted that wheneverthe oxygen content in the receiver 13 exceeds the safety point, it opens the valve 32 in the pipe 33 leading from inert gas reservoir 29 so as to force inert gas into the receiver at a rate sufiicient to maintain the oxygen content percentage below the danger point.
- inert gas passes out with the gas returned to the compressor, being separated out by any suitable means 34 in the supply line to the compressor.
- valve 35 is a valve in the pipe 19 whereby the supply of gas to the engine may be shut off when the valve 35 is opened to permit gas to pass to the heat exchanger 22 through the flexible removable connecting pipe 21, the valve 35, of course, being closed when the boat is on the way to the point of use.
- the use and operation of this invention is in a very real sense the same as the use of any cascading low temperature refrigerating system.
- the first two stages would be, for instance, in Louisiana, near the mouth of the Mississippi River. Part of the third stage would be there, namely, the compressor and the condenser.
- the receiver is Wandering or peripatetic. That is, it is the tank in the boat that moves back and forth between New La and Chicago.
- the evaporator is in Chicago.
- the third stage differs from the usual. in that the refrigerant, the gas which is compressed and liquefied never returns again to the system but it is replaced by other similar gas at the southern end of. the line.
- a part of the third stage can be said to be located entirely in Louisiana, that is to say, as the liquid methane is supplied to the receiver vessel on the ship, while most of the liquid stays there, some of it evaporates and is returned to the compressor for recirculation with additional gas added :to the system to replace that which remains as liquid in the receiver vessel.
- the rate at which the liquid evaporates, depending as it does upon the amount of heat supplied to the liquid mass, varies with the outside temperature.
- The'rate at which the propelling mechanism uses thisgas varies from zero when. the power mechanism on the boatis; at rest to a maximum.
- the evaporator rate may well be such as to supply more than enough fuel toop'erate the propelling engine and in any event, under circumstances when the engine is at rest or developing low power, the rate of evaporation-will be greater than the rate of use, therefore the importance of the control which permits wasting to atmosphere of excess gas to avoid building up dangerous pressures in the peripatetic receiver.
- the method of storing hydrocarbons of low boiling point consisting essentially of methane, which consists in providing a supply of hydrocarbon in gaseous condition, compressing it to a pressure above its critical pressure, cooling the compressed ga to a temperature above liquefaction temperature under the pressure condition'existing, then discharging it to a storage receiver with expansion to about atmospheric pressure to lower the temperature to liquefaction temperature to produce a mixture of liquid and gas, withdrawing the gaseous phase as a gas and adding gas from the supply and recompressing and recooling it and then sending it back to the receiver, continuing such circulation until the receiver is filled with a suitable quantity of. liquid at Substantially atmospheric pressure, bleeding the vapors released from the liquid in the receiver when the pressure in the receiver exceeds a predetermined level thereby to maintain a pressure therein at substantially atmospheric pressure.
- the method of storing hydrocarbons of low boiling point, consisting essentially of methane which consists in providing a supply of the hydrocarbon in gaseous condition at a pressure above its critical pressure, cooling the compressed gas to a temperature above liquefaction temperature under the pressure conditions existing, then discharging it to astorage receiver with expansion to about atmospheric pressure to lower the temperature to liquefaction temperature to produce a mixture of liquid and gas, withdrawing the gaseous phase as a gas and recompressing the gas for addition to the supply followed by recoolingand then sending it back to the receiver, continuing such. circulation until the receiver is filled with a suitable quantity of liquid at substantially atmospheric pressure, bleeding the'vapors released from the liquid in the receiver when the pressure in the receiver exceeds a predetermined level thereby to maintain a pressure therein at substantially atmospheric pressure.
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Ocean & Marine Engineering (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Description
March 5, 1957 w. MORRISON 2,783,624
METHOD OF LIQUEFYING GAS Filed Sept. 29, 1951 '17? 0622 for Q fly/(mil Jfvrrzlsow United States Patent METHOD OF LIQUEFYING GAS Willard L. Morrison, Lake Forest, 111., assignor, by mesue assignments, to Constock Liquid Methane Corporation, a corporation of Delaware Application September 29, 1951, Serial No. 248,973 2 Claims. c1. 62-175) "a residual refractory gas that remains after the refinery has removed the liquids such as gasoline, kerosene, fuel oil lubes and the like and after the so-called liquid petroleum gases such as propane and the like have been extracted.
Methane must be lowered in temperature to approximately l15.8 degrees F. before it can be liquefied. Above that temperature no matter how great pressures are applied, it will not liquefy. The gases .of higher boiling point can be compressed or liquefied and stored and shipped in the usual type of commercial gas bottles or gas tanks though they require under ordinary circumstances bottles or tanks of great weight and strength.
The problem which I propose to solve while in the main similar to problems that have been solved in the past with less satisfaction, is a diiferent one in that I propose the storage and shipment of very much larger quantities of this refractory methane gas.
In general, I propose to liquefy this gas by reducing its temperature and raising its pressure to a point below the critical temperature and above the critical pressure, then this liquid gas will be reduced'in pressure to somewhere in the neighborhood of atomspheric. Its temperature as a result of such pressure reduction is also greatly reduced, at which time and under which circumstances it will be stored and shipped. f
I propose to use refrigerating machinery including compressor, condenser, receiver and evaporator elements, by cascading where the evaporator of one refrigerant cools the condenser of the second refrigerant in a similar refrigerating circuit and the second refrigerant cools the methane in the evaporator of the methane circuit. In the first two circuits the refrigerant is recirculated or recycled through the system. In the third circuit the compressor and condenser will produce the liquefied methane at ap-.
proximately -1l5.8 degrees F. and at approximately 675 pounds absolute.
The liquid methane will then be discharged into an insulated portable receiver, will be allowed there to expand to atmospheric pressure with resultant sharp temperature drop of the liquid. This reduction in pressure will allow some of the gas to evaporate and will cool the remainder. The liquid will remain in the receiver. The evaporated gas will be returned to the system for further compression and liquefaction, the liquid left in the receiver being replaced by methane from the outside mixed with that which returns from the insulated receiver and this process will continue until a receiver of substantial size is substantially filled with liquefied methane at a temperature of approximately 258 degrees F. and .at a pressure of approximately atmospheric.
When the portable receiver is filled with the liquefied 2 methane, if it were possible to so insulate it that no heat would be added to it, the methane would remain liquid without boiling or evaporation at the temperature of the receiver. Actually, of course, no matter how well insulated the receiver is, some heat is added. Thatheat causes the liquid to boil orevaporate and so gas is given off from the surface of the. liquid. This gas, unless released,would soon raise the pressure in thereceiver far above the safety point so it must be allowed to escape.
Thus the pressure in the receiver remains at a substantially constant level and evaporation continues at a rate dependent upon the rate at which heat is added. The liquid remains at the same temperature just as water re mains at the same temperature while it boils. This gas may be 'used to assist in maintaining the temperature of the remaining liquefied gas constant so as to control the rate at which heat is allowed to reach the mass of liquefied gas, and may then be used as fuel or for any other purpose desired. w
, Inone instance, I-propose that the receiver be installed in 1a-boat or barge and the escaping gas will be used to furnish-the fuel to operate the engine to propel the ship to its destination, at which point the remaining liquefied gas will be disposed-of.
The transportation of such a gas as methane by pip line is an exceedingly expensive proposition because of the necessity of a continuous pipe from point of origin to point of use and the expense of building and operating a pipe line can only be justified when a continuous maximum volume of gas is to be transported. The method and apparatus which I propose which involves a com pressing and refrigerating system at pointof origin a peripatetic or wandering insulated receiver and a place to put the gas at the end of the line is therefore much less' expensive and much more flexible because the receiver may move to any desired point where the gas is needed. The cost of propelling the liquefied gas from point of origin to point of use in-terms of gas loss furnishing the power to operate the engine is so small that it is negligible and furnishes n0 bar to the operating of the flexible system I propose.
My invention is illustrated more or less diagrammatically in the accompanyingdrawing wherein is shown a diagrammatic ,flow sheet.
Like parts are indicated by like characters throughout the specification and drawing. 7 a
A is the first stage of refrigeration. It'includes compressor 1-, condenser 2, receiver 3, evaporator 4. B is the second stage of refrigeration. It includes a compressor 5, condenser 6, cooled by the evaporator 4 of stage A, a receiver 7 and an evaporator 8.
a C is the final stage of refrigeration wherein 9 is a supply pipe bringing methane to the compressor 10, which discharges into the condenser 11, cooled by the evaporator8 of the B stage, discharging liquefied gas through a pipe 12 to a receiver tank 13 on the ship 14 insulated at 15. 16 is a return pipe for evaporated gas from the receiver tank 13 to the low pressure side of the compressor 10.
When the receiver tank on the ship is filled, the pipes 12 and 16 to the tank are disconnected, the valves 17 being closed.- Then as the liquid methane in the receiver tank 13 evaporates, gas passes through the relief valve 18 to the pipe 19 to the engine 20 to drive the ship.
When the ship reaches its destination, pipe 19 is con nected to a pipe 21 on the shore and the methane under the residual pressure in the receiver 13 or the cold evaporated gas passes through the evaporator or heat exchanger 22 of a refrigerating system. Thereafter, the warm gas -is discharged through the pipe 23 to the burner 24 under the boiler 25.
The particular details of the evaporator and the burner 3 'I l a form no part of my invention and are not illustrated. The gas may be used under a boiler.v It might be stored in a receiver on shore. It might be used as fuel for internal combustion engines or it might be burned in other heat processes, as desired. The point'is that after the cold methane from the receiver on the boat has been used to extract heat from something else, the warmed gas may then be used to generate power or heat as the case may be.
Whether the engine uses all the evaporated gas or not to propel the boat, the evaporated gas must be permitted to escape from the receiver tank at such a rate that the pressure in the tank does not rise above a predetermined maximum so any excess of evaporated gas must be permitted to escape freely to the'atmosphere, at a pressure, but slightly above atmospheric, set by the relief valve 18 in the discharge pipe 26. So long as the engine uses gas at a rate not greater than the-evaporation rate, all the gas passes through the engine and is there burned. When the evaporation rate is higher than the engine use rate, the relief valve 18 permits gas to discharge through the pipe 26- from the engine supply pipe 19 to a mixing nozzle 27 where the methane is mixed with an inert: gaswhich reaches the nozzle through a pipe 28 from the inert gas reservoir 29. A control mechanism 30 automatically opens the supply pipe for the inert gas whenthe pressure in the line between the receiver and'th'e engine exceeds the safety point so that the inert gas is automatically mixed with hydrocarbon vapor when that is discharged to the atmosphere. Thus an inertor at least a non-explosive, non-poisonous mixture will be'dischargedto the atmosphere.
To avoid explosion the receiver in the boat must never be allowed to contain oxygen above a certain predetermined safety point. To guard against this, 31 indicates a gas analysis mechanism. This gas analysis mechanism is so adjusted that wheneverthe oxygen content in the receiver 13 exceeds the safety point, it opens the valve 32 in the pipe 33 leading from inert gas reservoir 29 so as to force inert gas into the receiver at a rate sufiicient to maintain the oxygen content percentage below the danger point. As the tank is being filled from the shore, such inert gas passes out with the gas returned to the compressor, being separated out by any suitable means 34 in the supply line to the compressor.
36 is a valve in the pipe 19 whereby the supply of gas to the engine may be shut off when the valve 35 is opened to permit gas to pass to the heat exchanger 22 through the flexible removable connecting pipe 21, the valve 35, of course, being closed when the boat is on the way to the point of use. i
I have illustrated at A, B and C a suitable arrangement for the compression and cooling of the gas which 1 propose to store and ship. Under some circumstances the natural pressure of the gas as it isdischarged fromthe well may obviate the necessity of using at least the compressor in the final stage. It is Well-known that under some circumstances the gas pressures are exceedingly high as the well discharges and therefore under such circumstances this pressure may be taken advantage of in the liquefaction of the gas.
The use and operation of my invention are as follows:
The use and operation of this invention is in a very real sense the same as the use of any cascading low temperature refrigerating system. The first two stages would be, for instance, in Louisiana, near the mouth of the Mississippi River. Part of the third stage would be there, namely, the compressor and the condenser. The receiver is Wandering or peripatetic. That is, it is the tank in the boat that moves back and forth between New Orleans and Chicago. The evaporator is in Chicago. The third stage differs from the usual. in that the refrigerant, the gas which is compressed and liquefied never returns again to the system but it is replaced by other similar gas at the southern end of. the line.
In a sense, a part of the third stage can be said to be located entirely in Louisiana, that is to say, as the liquid methane is supplied to the receiver vessel on the ship, while most of the liquid stays there, some of it evaporates and is returned to the compressor for recirculation with additional gas added :to the system to replace that which remains as liquid in the receiver vessel.
The rate at which the liquid evaporates, depending as it does upon the amount of heat supplied to the liquid mass, varies with the outside temperature. The'rate at which the propelling mechanism uses thisgas varies from zero when. the power mechanism on the boatis; at rest to a maximum. The evaporator rate may well be such as to supply more than enough fuel toop'erate the propelling engine and in any event, under circumstances when the engine is at rest or developing low power, the rate of evaporation-will be greater than the rate of use, therefore the importance of the control which permits wasting to atmosphere of excess gas to avoid building up dangerous pressures in the peripatetic receiver.
1 claim:
1. The method of storing hydrocarbons of low boiling point, consisting essentially of methane, which consists in providing a supply of hydrocarbon in gaseous condition, compressing it to a pressure above its critical pressure, cooling the compressed ga to a temperature above liquefaction temperature under the pressure condition'existing, then discharging it to a storage receiver with expansion to about atmospheric pressure to lower the temperature to liquefaction temperature to produce a mixture of liquid and gas, withdrawing the gaseous phase as a gas and adding gas from the supply and recompressing and recooling it and then sending it back to the receiver, continuing such circulation until the receiver is filled with a suitable quantity of. liquid at Substantially atmospheric pressure, bleeding the vapors released from the liquid in the receiver when the pressure in the receiver exceeds a predetermined level thereby to maintain a pressure therein at substantially atmospheric pressure.
2. The method of storing hydrocarbons of low boiling point, consisting essentially of methane, which consists in providing a supply of the hydrocarbon in gaseous condition at a pressure above its critical pressure, cooling the compressed gas to a temperature above liquefaction temperature under the pressure conditions existing, then discharging it to astorage receiver with expansion to about atmospheric pressure to lower the temperature to liquefaction temperature to produce a mixture of liquid and gas, withdrawing the gaseous phase as a gas and recompressing the gas for addition to the supply followed by recoolingand then sending it back to the receiver, continuing such. circulation until the receiver is filled with a suitable quantity of liquid at substantially atmospheric pressure, bleeding the'vapors released from the liquid in the receiver when the pressure in the receiver exceeds a predetermined level thereby to maintain a pressure therein at substantially atmospheric pressure.
References Cited in the file of this patent UNITED STATES PATENTS Thompson May 1, 1951
Claims (1)
1. THE METHOD OF STROING HYDROCARBONS OF LOW BOILING POINT, CONSISTING ESSENTIALLY OF METHANE, WHICH CONSISTS IN PROVIDING A SUPPLY OF HYDROCARBON IN GASEOUS CONDITION, COMPRESSING IT TO A PRESSURE ABOVE ITS CRITICAL PRESSURE, COOLING THE COMPRESSED GAS TO A TEMPERATURE ABOVE LIQUEFACTION TEMPERATURE UNDER THE PRESSURE CONDITION EXISTING, THEN DISCHARGING IT TO A STORAGE RECEIVER WITH EXPANSION TO ABOUT ATMOSPHERIC PRESSURE TO LOWER THE TEMPERATURE TO LIQUEFACTION TEMPERATURE TO PRODUCE A MIXTURE OF LIQUID AND GAS, WITHDRAWING THE GASEOUS PHASE AS A GAS AND ADDING GAS FROM THE SUPPLY AND RECOMPRESSING AND RECOOLING IT AND THEN SENDING IT BACK TO THE RECEIVER, CONTINUING SUCH CIRCULATION UNTIL THE RECEIVER IS FILLED WITH A SUITABLE QUANTITY OF LIQUID AT SUBSTANTIALLY ATMOSPHERIC PRESSURE, BLEEDING THE VAPORS RELEASED FROM THE LIQUID IN THE RECEIVER WHEN THE PRESSURE IN THE RECEIVER EXCEEDS A PREDETERMINED LEVEL THEREBY TO MAINTAIN A PRESSURE THEREIN AT SUBSTANTIALLY ATMOSPHERIC PRESSURE.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US248973A US2783624A (en) | 1951-09-29 | 1951-09-29 | Method of liquefying gas |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US248973A US2783624A (en) | 1951-09-29 | 1951-09-29 | Method of liquefying gas |
GB11685/54A GB766128A (en) | 1954-04-22 | 1954-04-22 | Apparatus and method of storing, shipping and using volatile hydrocarbons |
Publications (1)
Publication Number | Publication Date |
---|---|
US2783624A true US2783624A (en) | 1957-03-05 |
Family
ID=9990807
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US248973A Expired - Lifetime US2783624A (en) | 1951-09-29 | 1951-09-29 | Method of liquefying gas |
Country Status (5)
Country | Link |
---|---|
US (1) | US2783624A (en) |
BE (1) | BE528204A (en) |
FR (1) | FR1099270A (en) |
GB (1) | GB766128A (en) |
NL (1) | NL96502C (en) |
Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2959020A (en) * | 1958-01-29 | 1960-11-08 | Conch Internat Mcthane Ltd | Process for the liquefaction and reliquefaction of natural gas |
US2975608A (en) * | 1957-07-01 | 1961-03-21 | Conch Int Methane Ltd | Transportation and use of liquefied natural gas |
US2975604A (en) * | 1956-05-07 | 1961-03-21 | Little Inc A | Method of distribution of condensable gases |
US2978876A (en) * | 1958-01-16 | 1961-04-11 | Conch Int Methane Ltd | Reliquefaction system for liquefied gases |
US2984080A (en) * | 1958-06-25 | 1961-05-16 | Conch Int Methane Ltd | Method and means for the transportation of liquefied natural gas |
US3005317A (en) * | 1959-10-26 | 1961-10-24 | Phillips Petroleum Co | Combination dry or liquid cargo vessel and process |
US3098362A (en) * | 1959-11-04 | 1963-07-23 | Sohda Yoshitoshi | Container vessel for storage and transportation of liquefied natural gases |
US3108446A (en) * | 1959-12-21 | 1963-10-29 | Sohda Yoshitoshi | Container vessel arrangement for storage and transportation of liquefied natural gases |
US3132489A (en) * | 1961-01-03 | 1964-05-12 | Chicago Bridge & Iron Co | Apparatus for the refrigerated storage of liquefied gas |
US3387462A (en) * | 1965-07-29 | 1968-06-11 | Snecma | Dual fuel injection device for propulsion motors, more especially for methane-carrying ships |
US4282187A (en) * | 1979-09-21 | 1981-08-04 | Grumman Aerospace Corporation | Production of synthetic hydrocarbons from air, water and low cost electrical power |
WO1998043029A1 (en) * | 1997-03-21 | 1998-10-01 | Kværner Maritime A.S. | Method and device for storage and transport of liquefied natural gas |
US20090060725A1 (en) * | 2007-09-05 | 2009-03-05 | Solar Turbines Incorporated | Engine with intake air temperature control system |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CH561620A5 (en) * | 1972-12-11 | 1975-05-15 | Sulzer Ag | |
FR2570478A1 (en) * | 1984-09-19 | 1986-03-21 | Nord Mediterranee Chantiers | Processes and devices for condensing and recycling the gases which evaporate from the hold of a ship for transporting liquefied gas and ships comprising these devices |
HU193122B (en) * | 1985-07-30 | 1987-08-28 | Olajipari Foevallal Tervezoe | Method and arrangement for decreasing the evaporation losses of storage spaces containing evaporating material and recovering the vapours from gas-vapour mixture |
FI121745B (en) * | 2005-12-28 | 2011-03-31 | Waertsilae Finland Oy | Arrangement and method for producing cooling energy for the refrigerant circulation system in a watercraft |
DE102010007328A1 (en) * | 2010-02-08 | 2011-08-11 | Meyer Werft GmbH, 26871 | Seagoing vessel, in particular gas-powered seagoing vessel |
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US2464026A (en) * | 1945-06-01 | 1949-03-08 | Gen Electric | Gas eliminator for electric apparatus |
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-
1951
- 1951-09-29 US US248973A patent/US2783624A/en not_active Expired - Lifetime
-
1954
- 1954-04-09 NL NL186660A patent/NL96502C/xx active
- 1954-04-14 FR FR1099270D patent/FR1099270A/en not_active Expired
- 1954-04-17 BE BE528204D patent/BE528204A/xx unknown
- 1954-04-22 GB GB11685/54A patent/GB766128A/en not_active Expired
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US1140250A (en) * | 1914-10-12 | 1915-05-18 | Godfrey L Cabot | Means for handling and transporting liquid gas. |
US1225574A (en) * | 1914-10-26 | 1917-05-08 | Godfrey L Cabot | Apparatus for condensing gas under high pressure. |
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US1984250A (en) * | 1932-03-14 | 1934-12-11 | York Ice Machinery Corp | Production of solid carbon dioxide |
US2090163A (en) * | 1934-05-09 | 1937-08-17 | Lee S Twomey | Method of liquefying and storing fuel gases |
US2145678A (en) * | 1935-05-16 | 1939-01-31 | Servel Inc | Vehicle cooler using engine fuel as refrigerant |
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US2309813A (en) * | 1940-07-22 | 1943-02-02 | Edmund W Whiting | Fuel tank |
US2317836A (en) * | 1941-05-07 | 1943-04-27 | Western Electric Co | Safety apparatus |
US2464026A (en) * | 1945-06-01 | 1949-03-08 | Gen Electric | Gas eliminator for electric apparatus |
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Cited By (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2975604A (en) * | 1956-05-07 | 1961-03-21 | Little Inc A | Method of distribution of condensable gases |
US2975608A (en) * | 1957-07-01 | 1961-03-21 | Conch Int Methane Ltd | Transportation and use of liquefied natural gas |
US2978876A (en) * | 1958-01-16 | 1961-04-11 | Conch Int Methane Ltd | Reliquefaction system for liquefied gases |
US2959020A (en) * | 1958-01-29 | 1960-11-08 | Conch Internat Mcthane Ltd | Process for the liquefaction and reliquefaction of natural gas |
US2984080A (en) * | 1958-06-25 | 1961-05-16 | Conch Int Methane Ltd | Method and means for the transportation of liquefied natural gas |
US3005317A (en) * | 1959-10-26 | 1961-10-24 | Phillips Petroleum Co | Combination dry or liquid cargo vessel and process |
US3098362A (en) * | 1959-11-04 | 1963-07-23 | Sohda Yoshitoshi | Container vessel for storage and transportation of liquefied natural gases |
US3108446A (en) * | 1959-12-21 | 1963-10-29 | Sohda Yoshitoshi | Container vessel arrangement for storage and transportation of liquefied natural gases |
US3132489A (en) * | 1961-01-03 | 1964-05-12 | Chicago Bridge & Iron Co | Apparatus for the refrigerated storage of liquefied gas |
US3387462A (en) * | 1965-07-29 | 1968-06-11 | Snecma | Dual fuel injection device for propulsion motors, more especially for methane-carrying ships |
US4282187A (en) * | 1979-09-21 | 1981-08-04 | Grumman Aerospace Corporation | Production of synthetic hydrocarbons from air, water and low cost electrical power |
WO1998043029A1 (en) * | 1997-03-21 | 1998-10-01 | Kværner Maritime A.S. | Method and device for storage and transport of liquefied natural gas |
US20090060725A1 (en) * | 2007-09-05 | 2009-03-05 | Solar Turbines Incorporated | Engine with intake air temperature control system |
US8474241B2 (en) | 2007-09-05 | 2013-07-02 | Solar Turbines Inc. | Engine with intake air temperature control system |
Also Published As
Publication number | Publication date |
---|---|
NL96502C (en) | 1961-01-16 |
FR1099270A (en) | 1955-09-01 |
GB766128A (en) | 1957-01-16 |
BE528204A (en) | 1957-02-15 |
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