US2975607A - Revaporization of liquefied gases - Google Patents

Revaporization of liquefied gases Download PDF

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Publication number
US2975607A
US2975607A US741386A US74138658A US2975607A US 2975607 A US2975607 A US 2975607A US 741386 A US741386 A US 741386A US 74138658 A US74138658 A US 74138658A US 2975607 A US2975607 A US 2975607A
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heat
transfer medium
heat transfer
line
temperature
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US741386A
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English (en)
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William W Bodle
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Conch International Methane Ltd
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Conch International Methane Ltd
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Priority to LU37293A priority Critical patent/LU37293A1/fr
Application filed by Conch International Methane Ltd filed Critical Conch International Methane Ltd
Priority to US741386A priority patent/US2975607A/en
Priority to GB17558/59A priority patent/GB861919A/en
Priority to FR797032A priority patent/FR1226947A/fr
Priority to BE579483A priority patent/BE579483A/fr
Priority to ES0250007A priority patent/ES250007A1/es
Priority to NL240071A priority patent/NL112932C/nl
Priority to SE553359A priority patent/SE220248C1/en
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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
    • 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
    • F17C2265/05—Regasification

Definitions

  • This invention relates generally to improvements in the art of preparing a liquefied natural gas for use as a fuel, and more particularly, but not by Way of limitation,
  • Natural gas is available in certain localities in amounts considerably greater than demanded in those localities, While in other localities a marked deficiency exists in the amount of natural gas available for use.
  • the source of plentiful supply is joined by land with the areas where a deficiency exists, transfer can be economically achieved by means of pipeline and the like wherein transfer is effected while the gas remains in the gaseous state.
  • the area having a deficiency is somewhat isolated, or where the source of supply and the area where a deficiency exists are separated by a large body of water, transfer by pipeline becomes impractical.
  • Transportation is effected with the liquefied natural gas housed in large insulated containers at about atmos pheric pressure or slightly above, and vw'th the natural gas at a temperature as low as -258 F.
  • the latter temperature represents the boiling point temperature for methane at atmospheric pressure.
  • natural gas has small amounts of heavier and higher boiling hydrocarbons, such as ethane, propane, butane and the like, the liquefied gas will be characterized by a some- What higher boiling temperature, usually ranging from 240 to 258 F., depending upon the amount of the heavier hydrocarbons.
  • the liquefied natural gas must, in all cases, be vaporized before being used as a fuel.
  • a natural gas containing a substantial portion of methane will, in many countries, have a heating value far above the specifications for a gas which may be used in existing equipment, and variation or adjustment might also be required in its specific gravity. In these countries it is therefore required that the liquefied gas not only be revaporised, but also reformed to a lower heating value and to adjust the specific gravity.
  • Such reforming operations may be carried out in the locality where the liquefied gas is revaporized.
  • the actual point of use of the gas may be located a substantial distance from the point where the liquefied gas becomes available, as when the point of use is inland and the liquefied gas is transported by ship.
  • a liquefied natural gas at about atmospheric pressure will have a temperature of about 240 to 258 F.
  • a liquefied gas may be revapon'zed in accordance with present vaporization practices by passing the same in heat exchange relation with a readily available heat source, such as air or sea water.
  • a readily available heat source such as air or sea water.
  • the tubes of the heat exchanger will be at a temperature far below the freezing temperature of the water.
  • the tubes will rapidly become coated with ice to reduce the heat transfer efiiciency, either resulting in complete stoppage of water flow through the heat exchanger, or requiring an over design of the heat exchanger to accommodate the inherent ice formation.
  • air instead of water hydrates will form and precipitate out of the air onto the tubes of the heat exchanger, resulting in substantially the same problem as when using water.
  • the present invention contemplates a novel method of revaporizing a liquefied gas by use of a heat transfer medium passing in heat exchange relationship with a readily available and cheap heat source, such as sea water or air, and, alternately, the liquefied gas.
  • a heat transfer medium passing in heat exchange relationship with a readily available and cheap heat source, such as sea water or air, and, alternately, the liquefied gas.
  • the primary requirement of the heat transfer medium is that its freezing temperature be below the temperature of the liquefied gas, such that no solids will form on the tubes of the heat exchanger through which the liquefied gas and the heat transfer medium are passed.
  • the heat transfer medium is used in such a quantity that the temperature thereof when passing in heat exchange relation with the heat source is higher than the freezing temperature of any component of the heat source, but [lower than the temperature of the heat source.
  • the heat transfer medium is a liquid which is vaporized by heat exchange with the heat source and condensed by heat exchange with the liquefied gas, such that the latent heat of the heat transfer medium will be the principal factor in vaporizing the liquefied gas.
  • This invention further contemplates reducing the pressure of the vaporized heat transfer medium prior to passage thereof in heat exchange relation with the liquefied gas to obtain work from the heat transfer medium. After the heat transfer medium is condensed by the liquefied gas, it is again increased in pressure before being revaporized by the heat source. The difference in the work obtained by a decrease in the pressure of the vapor, and the work required to increase the pressure of the condensed heat transfer medium, may be utilized as an auxiliary power supply in a system involving practice of the invention.
  • An important object of this invention is to facilitate the preparation of a liquefied natural gas for use as a fuel.
  • Another object of this invention is to efficiently and economically revaporize a liquefied gas either for use as a fuel or for transportation through a pipeline or the like to a reforming plant.
  • Another object of this invention is to utilize heat from a readily available and cheap heat source to revaporize a liquefied gas having a boiling temperature far below the freezing temperature of some component of the heat source, without the formation of solids on the tubes of the heat exchanger used for vaporizing the liquefied gas.
  • a further object of this invention is to utilize a readily available heat transfer medium for transferring the heat from a cheap heat source to a liquefied gas for revapon'zing the liquefied gas.
  • Another object of this invention is to provide a method evident from the following detailed description, when read in conjunction with the accompanying drawings which illustrate this invention.
  • Figure l is a flow diagram illustrating a practice of this invention.
  • FIG. 2 is a flow diagram illustrating a modified practice of this invention.
  • Figure 3 is a modification of Fig. 2 illustrating still anot-her practice of this invention.
  • Figure 4 is a flow diagram of a typical commercial installation illustrating a practice of the present invention.
  • reference character 6 designates a line for feeding liquefied natural gas to a stationary, insulated storage tank 8.
  • the line 6 extends from a container (not shown) used for transporting the liquefied natural gas which, as previously noted, will ordinarily be aboard a ship.
  • the liquefied natural gas in the tank 8 will normally be at about atmospheric pressure, or slightly above, and have a temperature of about 240 to -258 F.
  • the major portion of the liquefied natural gas in the tank 8 is fed through a line 10 to a suitable pump 12.
  • the pump 12 increases the pressure of the liquefied natural gas to the pressure at which it is desired to either immediately reform the gas, used the vaporized gas as fuel, or transport the gas through a pipe line to a distant reforming plant, as previously indicated.
  • the pressure of the liquefied natural gas discharging from the pump 12 may therefore be anywhere from slightly above atmospheric pressure to about 600 pounds per square inch, but is usually from about 50 to about 200 pounds per square inch.
  • the liquefied natural gas discharged through the line 14 from the pump 12 is directed through a vaporizer 16 where the liquefied gas is revaporized by a heat transfer medium circulated in a closed cycle, as will be described in detail below.
  • the revaporized natural gas is then directed through a line 18 to a separator 20 for removing any condensate which may exist after passage of the stream through the vaporizer 16.
  • the condensate removed in the separator 20 is returned through a line 22 to the intake of the pump 12 where it may be re-circulated to the vaporizer 16.
  • the overhead from the separator 20 consists solely of revaporized natural gas and is discharged through a line 24 to either a fuel gathering system or a reforming plant, as previously indicated.
  • the vapor boil-off or over head from the storage tank 3 is directed through a line 26, partially to a compressor 28 and partially to he used as a fuel in an engine 34 ⁇ operating the compressor 28.
  • the vapor passing through the compressor 28 is increased in pressure to the pressure of the liquefied natural gas in the line 14 and is discharged through a line 32 to be combined with the vapor in the line 24 discharging from the separator 20.
  • a by-pass line 34 may be run from the line 24 back to the engine 30 for supplying additional fuel if desired.
  • the heat transfer medium previously mentioned is circulated from-the vaporizer 16 through a line 36 to another vaporizer 38, and then through a line 44 ⁇ back to the vaporizer 16.
  • This heat transfer medium 'as will be described, provides a transfer of heat from a readily available and cheap heat source circulated through the vaporizer 38 ization progresses.
  • the heat source for the vaporizer 38 must have a temperature above the boiling temperature of the liquefied gas being vaporized and may take any desired form, but is preferably a material which is readily available and cheap, such as sea water or air. Sea water is the preferred heat source.
  • the water is directed through a line 42 from a source of supply (not shown) and is pumped by a suitable pump 44 through a line 46 to the vaporizer 38.
  • the water is passed in heat exchange relation with the heat transfer medium to supply an amount of heat to the heat transfer medium at least equal to the amount of heat dissipated from the heat transfer medium in the vaporizer 16, as previously indicated.
  • the water is discharged through a line 48 to a suitable disposal point.
  • the heat transfer medium may be any fluid having a freezing point below the boiling temperature of the liquetied natural gas, to prevent the deposition of solids in the vaporizer 16, and which, in passage through the vaporizer 38, has a temperature above the freezing temperature of the heat source but below the actual temperature of the heat source.
  • the heat transfer medium may therefore be in liquid form during its circulation through both of the vaporizers 16 and 38 to provide a transfer of sensible heat alternately to and from the heat transfer medium.
  • heat transfer medium When the heat transfer medium is in continuous liquid form, however, a large volume of heat transfer medium must be circulated through the system, since the temperature reduction thereof by passage through the vaporizer 16 is necessarily limited to such an extent as to retain the temperature of the heat transfer medium returning to the vaporizer 38 at a temperature higher than the freezing temperature of the heat source. It is therefore preferred that a heat transfer medium be used which goes through phase changes during circulation through the vaporizers 16 and 38, with a resulting transfer of latent heat.
  • the preferred heat transfer medium has a moderate vapor pressure at a temperature between the actual temperature of the heat source and the freezing temperature of the heat source to provide a vaporization of the heat transfer medium during passage thereof through the vaporizer 38.
  • the transfer medium in order to have a phase change, must be liquefiable at a temperature above boiling temperature of the liquefied natural gas, such that the heat transfer medium will be condensed during passage through vaporizer 16.
  • the freezing temperature of the heat transfer medium must still be below the boiling temperature of the liquefied natural gas.
  • the liquefied gas is a pure, or substantially pure, compound, it will boil at a constant temperature and absorb latent heat at that temperature.
  • the liquefied gas is a mixture of compounds, it will, in most cases, boil over a temperature range, the temperature increasing as Vapor- In this case, it will be desirable to make the heat transfer medium av mixture of compounds .of such composition that the heat transfer medium will condense over a range of temperatures some what above the vaporizing temperature range of the liquefied gas, thereby making it possible to recover all of the latent heat in the liquefied gas by condensing the heat transfer medium.
  • the required quantity of heat transfer medium is reduced to a minimum, since mostly (or only) latent heat changes in the heat transfer medium are utilized, rather than only sensible heat changes.
  • the heat transfer medium may be circulated through the Vaporizers 16 and 38 by gravity. By locating the vaporizer 16 physically above the vaporizer 38, the heat transfer medium condensing in the vaporizer 16 will flow by gravity into the lower vaporizer 38. On the other hand, the heat transfer medium being vaporized in the vaporizer 38 will rise through the line 40 into the vaporizer 16, thereby reducing the energy required to vaporize the liquefied natural gas.
  • a portion of the revaporized natural gas discharging through the line 24 will be diverted through a line 50'for such purposes as heat for buildings used in conjunction with the practice of the invention, and as a fuel for generators and the like, as indicated by the blocks in the lower portion of the flow diagram. Also, a block has been included to indicate that a certain portion of the natural gas is inherently lost by venting and leakage.
  • FIG. 2 A modified system is illustrated in Fig. 2, wherein reference character 52 designates a heat exchanger functioning as a boiler, and reference character 54- designates another heat exchanger functioning as a condenser for a heat transfer medium.
  • the heat source is again preferably sea water which is circulated through a line 56, the tubes of the heat exchanger 52, and then discharged through another line 58 to a suitable disposal point.
  • the liquefied gas being revaporized is directed to the tubes of the other heat exchanger 54 by a line 60 and discharged from the exchangr 54 as a vapor through line 62 leading to any desired point of use. It will be assumed that the liquefied gas passing through the line 60 has been pressurized to the desired pressure as described in connection with Fig. 1.
  • the heat transfer medium is in the form of a material which undergoes phase changes during passage through the heat exchangers 52 and 54 substantially in the same manner as previously described.
  • the vaporized heat transfer medium is discharged from the heat exchanger 52 through a line 64 to the inlet of a suitable device 66 forming a work-producing zone.
  • the device 66 is preferably a'turbine, but may be any other form of engine which may be operated by expansion of the vaporized heat transfer medium.
  • the heat transfer medium is reduced in pressure by passage through the work-producing device 66, and the resulting energy may be recovered in any desired form, such as by rotation of the shaft of a turbine.
  • the heat transfer medium discharging from the work-producing device 66 is still at least mostly in the form of a vapor, but at reduced pressure.
  • This reduced pressure heat transfer medium is directed through another line 68 to the heat exchanger 54 wherein the heat transfer medium is condensed and the liquefied gas is vaporized by a transfer of heat from the heat transfer medium to the liquefied gas.
  • the major portion of this heat is preferably derived as latent heat, such that the temperature of the heat transfer medium will not be sub stantially reduced by passage through the heat exchanger 54.
  • the condensed heat transfer medium is discharged from the heat exchanger 54 through a line 70 to a pump 72, whereby the pressure of the condensed heat transfer medium is substantially increased.
  • the pressurized and condensed heat transfer medium is returned through a line 74 back to the heat exchanger 52.
  • the maximum power recovery possible in a cycle as disclosed in Fig. 2 and described above, is related to the heat rejection by the heat transfer medium in the heat exchanger 54 and the temperatures of the heat source and the liquefied gas passing through the heat exchanger 54 in the following manner:
  • a superheater 76 may be interposed in the line 64 leading from the heat exchanger 52 to the device 66 as shown in Fig. 3.
  • the superheater 76 may be heated by any suitable means, such as steam circulated to the superheater through a line 78 and discharged through line 80.
  • a portion of the vaporized heat transfer medium may be by-passed to preheat the heat transfer medium entering the heat exchanger 52. This may be accomplished by extending a line 82 from line 64 downstream of the heat exchanger 52 and upstream of the device 66 back to the line 74 downstream from the pump 72, as also illustrated in Fig. 3. However, a pump 84 must be interposed in the line 74 downstream of the connection of the by-pass line 82' to feed the mixed heat transfer medium to the heat exchanger 52.
  • each of the three systems 86 may be easily designed to handle 50 percent of the required revaporization capacity, such that one of the systems may be out of operation at any one time for inspection and repairs. It will be understood that when only two systerns are provided, each system should have a capacity equal to the total revaporization capacity in order that either of the systems may be taken out of operation for inspection or repair while the other system continues the revaporization process.
  • the liquefied natural gas is fed to an installation such as illustrated in Fig. 4, through a line 88 from a suitable liquefied natural gas storage tank, such as the tank 8 illustrated in Fig. 1 and previously described.
  • the liquefied natural gas in the line 88 will ordinarily consist of a major portion of methane and minor portions of heavier hydrocarbons, such as butane and propane, and will be at about atmospheric pressure and at a temperature from 240 to 258 F., depending upon the composition of the stream.
  • This liquefied natural gas in the line 88 is fed to three separate pumps 90 for increasing the pressure of the liquefied natural gas and feeding the liquefied natural gas to a header 92 communicating with the outlet of each of the pumps 98.
  • any of the pumps 90 may be isolated, such that the liquefied natural gas from the line 83 will be directed through the remaining pumps 90 to the header 92. It is also desirable to provide a by-pass line 94, at the outlet of each pump 96 to selectively direct a portion of the high pressure liquefied natural gas into a header 96.
  • the high pressure liquefied natural gas in the header 96 may be used to prime any of the pumps 90 when such pumps are being placed in operation.
  • the high pressure liquefied natural gas in the header 92 is selectively directed through feed lines 98, 100 and 102 to the separate revaporization systems 86. Since the systems 86 are of the same design, it is believed necessary only to describe one in detail, such as the system shown at the left end of Fig, 4.
  • the high pressure liquefied natural gas flowing through the line 98 is directed through the tubes of a heat exchanger 104 acting as a vaporizer for the natural gas, such that the natural gas flowing through the discharge line 1% from the heat exchanger 164 will be substantially in the form of a vapor.
  • the gas discharged from the heat exchanger 104 is directed into a separator 108 for removing condensate from the stream.
  • a portion of the condensate from the separator 8 is directed back to the heat exchanger 104- through a line 1111 for reheating thereof.
  • This portion of the condensate in the separator 1118 may be directed through the heat exchanger 104 by a gravity process, such that when the condensate level in the separator 108 tends to exceed the liquid level in the exchanger 104, an additional amount of condensate will be directed back through the exchanger 1% for reheating.
  • a liquefied natural gas will ordinarily contain at least a minor percentage of heavy ends, such as butane and propane, which will ordinarily collect in the lower portion of the separator 108 as a condensate. Therefore, a portion of the condensate from the separator 108 may be directed into a header 1121eading to a suitable storage vessel 114 where the heavy ends may be collected and selectively discharged through a line 116. It will also be observed that condensate from the separators 1118 of the remaining systems is also directed into the header 112i for storing additional heavy ends in the vessel 11.4.
  • the fiow of condensate into the header 112 from each separator 108 is regulated by a valve 118 in turn controlled by a liquid level controller 120 mounted on the respective separator.
  • the overhead from the separator 108' will be in the form of a vapor and is discharged through a line 122.
  • a flow controller 123 is connected to the line 122 and a valve 124' in the liquefied gas feed line 98 to correlate the feed of liquefied gas with the amount of vapor produced by the heat exchanger 104. For example, if the composition of the liquefied gas feed changes, the amount of vapor produced will vary, and the quantity of liquefied gas fed to the respective system must be varied accordingly to prevent an over or under supply of liquefied gas to the exchanger 104- and separator 1118.
  • the natural gas revaporized by each of the systems 86 is directed into a header 126 leading to another separator 12% for removal of any condensate which may have formed in the lines 122 or the header 126.
  • the condensate in the separator 128 is discharged through a line 130 into the heavy ends storage vessel 114. It will also be noted that the flow through the discharge line 130 is controlled by a liquid level controller 132 mounted on a side of the separator 128.
  • the vapor overhead from the separator 123 is directed through a discharge line 134 for use either as a fuel or for use in a subsequent reforming operation in the manner previously described.
  • the natural gas in the line 134 will be in gaseous form and at an elevated pressure for ease of transporation or subsequent use as a fuel.
  • the heat exchanger 104 is preferably heated by a closed propane cycle, wherein propane is condensed in the exchanger 104 and then falls by gravity through a line. 136 to a lower'heat exchanger 13?.
  • propane is condensed in the exchanger 104 and then falls by gravity through a line. 136 to a lower'heat exchanger 13?.
  • the condensed propane is revaporized in the heat exchanger 138, such that the propane vapors will rise through a line 140 from the heat exchanger 138 back into the heat exchanger 104;
  • the usual heat source for vaporizing the propane in the heat exchanger 138 is in the form of sea Water constantly available at an inlet line 142. Sea water from the inlet line 142 is pumped through line 144 to the tubes ofthe heat exchanger 138, as well as to the heat-exchangers 138 of the remaining systems 86.
  • the sea water discharging from the heat exchanger 138 is directed back through a line 146 to a header 148 for convenient disposal of the used water.
  • the amount of sea water directed throughthe heat exchanger 138 is regulated by a valve 149 which in turn is controlled by the temperature of the condensed propane through use of a temperature controller 150 con-. nected to line 136, such that the amount of heat available. to the heat exchanger 138 may be controlled as desired.
  • a furnace 151 may be used.
  • a furnace 151 is preferably installed for each of the systems 86 and is heated by a suitable fuel from a fuel line 152. This fuel may be easily obtained by bleeding off a portion of. the natural gas in the natural gas discharge line 134 as illustrated at the right hand end of the flow diagram.
  • the condensed propane may be directed from the line 136 through a by-pass line 154 for passage through the respective furnace 151 where the propane will be revaporized;
  • the propane vapors will in turn rise through a line 156 which is joined with the previously describedpropane vapor line 140 for flow into the upper heat ex changer 1194.
  • make-up line 160 is extended 138 to :a propane supply and in turn communicates with a from the heat exchanger discharge line 162, which requires additional propane, the additional be directed through the respective line 160 with the propane in the respective system.
  • the present invention provides for a power recovery in a revaporization of liqueued natural gas, such that the net power required for a system will be reduced to a minimum.
  • a method of vaporizing a liquefied gas having a boiling temperature range below the temperature of a heat source comprising the steps of:
  • a method as defined in claim 1 characterized further in combining a portion of the vaporized heat transfer medium with the pressurized and condensed heat transfer medium to preheat the heat transfer medium prior to revaporization thereof, and pressurizing the combined vaporized and condensed heat transfer medium prior to revaporiz-ation thereof.
  • a method as defined in claim 1 characterized further in that heat source is 6.
  • a method as defined in claim 4 characterized further in that the heat transfer medium is propane.
  • a method of utilizing heat from a readily available heat source for vaporizing a liquefied gas having a boiling temperature below the freezing temperature of at least one component of the heat source comprising passing the liquefied gas in heat exchange relationship with a vaporized heat transfer medium having a condensation temperature above the boiling point temperature of the liquefied gas and a freezing point temperature below the boiling point temperature of the liquefied gas and at a rate to vaporize the liquefied gas and condense the heat transfer medium, passing the condensed heat transfer medium in heat exchange relationship with the heat source '5. having a temperature above the boiling point temperature of the heat transfer medium and in which no component of the heat source has a freezing point temperature above the temperature of the heat transfer medium and at a flow rate to vaporize the heat transfer medium, and repeating the cycle.
  • a method of utilizing heat from a readily available heat source for vaporizing a liquefied gas having a boiling temperature below the freezing temperature of at least one component of the heat source comprising passing the heat transfer medium in heat exchange relationship with the liquefied gas and alternately the heat source, said heat transfer medium having a frezmg temperature below the boiling temperature of the liquefied gas and having a temperature between the temperature of the heat source and the freezing temperature of any component of the heat source while passing in heat exchange relationship with the heat source, passing the vaporized heat transfer medium through a Work producing zone with a reduction in pressure before passage thereof in heat exchange relationship with the liquefied gas, pressurizing the condensed heat transfer medium before passage thereof in heat exchange relationship with the heat source and lay-passing a portion of the heat transfer medium from upstream of the work producing zone to the pressurized and condensed heat transfer medium to preheat to heat transfer medium before passage thereof in heat exchange relationship with the heat source.
  • a method of utilizing heat from a readily available heat source for vaporizing a liquefied gas having a boiling temperature below the freezing temperature of at least one component of the heat source comprising passing a heat transfer medium in heat exchange relation with the liquefied gas, and, alternately, the heat source, said heat transfer medium having a freezing temperature below the boiling temperature of the liquefied gas and having a temperature between the temperature of the heat source and the freezing temperature of any component of the heat source while passing in heat exchange relation with the heat source, and characterized further in that the heat transfer medium is a liquid having a moderate vapor pressure at a temperature between the temperature of the heat source and the freezing temperature of any component of the heat source for vaporization of the heat transfer medium upon passage in heat exchange relation with the heat source.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
US741386A 1958-06-11 1958-06-11 Revaporization of liquefied gases Expired - Lifetime US2975607A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
LU37293A LU37293A1 (fr) 1958-06-11 1958-06-10 Revaporisation de gaz liquéfiés
US741386A US2975607A (en) 1958-06-11 1958-06-11 Revaporization of liquefied gases
GB17558/59A GB861919A (en) 1958-06-11 1959-05-22 Revaporization of liquefied gases
BE579483A BE579483A (fr) 1958-06-11 1959-06-09 Revaporisation de gaz liquéfiés
FR797032A FR1226947A (fr) 1958-06-11 1959-06-09 Procédé de revaporisation de gaz liquéfiés
ES0250007A ES250007A1 (es) 1958-06-11 1959-06-09 Procedimiento perfeccionado para revaporizar un gas licuado
NL240071A NL112932C (nl) 1958-06-11 1959-06-10 Inrichting voor het verdampen van een vloeibaar gemaakt gas zoals aardgas of methaan met behulp van een warmteoverdragend medium dat een kringloop doorloopt
SE553359A SE220248C1 (en) 1958-06-11 1959-06-10 Method of evaporation of condensed gases

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US741386A US2975607A (en) 1958-06-11 1958-06-11 Revaporization of liquefied gases

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US2975607A true US2975607A (en) 1961-03-21

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US741386A Expired - Lifetime US2975607A (en) 1958-06-11 1958-06-11 Revaporization of liquefied gases

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US (1) US2975607A (fr)
BE (1) BE579483A (fr)
ES (1) ES250007A1 (fr)
FR (1) FR1226947A (fr)
GB (1) GB861919A (fr)
LU (1) LU37293A1 (fr)
NL (1) NL112932C (fr)
SE (1) SE220248C1 (fr)

Cited By (40)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3266261A (en) * 1964-11-27 1966-08-16 James H Anderson Method and apparatus for evaporating liquefied gases
DE1247751B (de) * 1963-02-07 1967-08-17 Siemens Ag Gasturbinen-Speicherkraftanlage
US3421574A (en) * 1966-03-11 1969-01-14 Niagara Blower Co Method and apparatus for vaporizing and superheating cold liquefied gas
US3675436A (en) * 1970-02-25 1972-07-11 Struthers Scient And Intern Co Desalination process
DE2402043A1 (de) * 1974-01-11 1975-07-24 Sulzer Ag Verfahren und anlage zur verdampfung und erwaermung von verfluessigtem erdgas
US3986340A (en) * 1975-03-10 1976-10-19 Bivins Jr Henry W Method and apparatus for providing superheated gaseous fluid from a low temperature liquid supply
DE2751642A1 (de) * 1977-11-17 1979-08-09 Borsig Gmbh Verfahren zur umwandlung einer tiefsiedenden fluessigkeit, insbesondere unter atmosphaerendruck stehendem erdgas oder methan, in den gasfoermigen zustand mit anschliessender erwaermung
EP0048316A1 (fr) * 1980-09-19 1982-03-31 Uhde GmbH Procédé et dispositif pour la révaporisation de gaz naturel liquéfié
US4372124A (en) * 1981-03-06 1983-02-08 Air Products And Chemicals, Inc. Recovery of power from the vaporization of natural gas
US4437312A (en) 1981-03-06 1984-03-20 Air Products And Chemicals, Inc. Recovery of power from vaporization of liquefied natural gas
US4438729A (en) * 1980-03-31 1984-03-27 Halliburton Company Flameless nitrogen skid unit
US4458633A (en) * 1981-05-18 1984-07-10 Halliburton Company Flameless nitrogen skid unit
US4479350A (en) * 1981-03-06 1984-10-30 Air Products And Chemicals, Inc. Recovery of power from vaporization of liquefied natural gas
US4995234A (en) * 1989-10-02 1991-02-26 Chicago Bridge & Iron Technical Services Company Power generation from LNG
US5036678A (en) * 1990-03-30 1991-08-06 General Electric Company Auxiliary refrigerated air system employing mixture of air bled from turbine engine compressor and air recirculated within auxiliary system
US5056335A (en) * 1990-04-02 1991-10-15 General Electric Company Auxiliary refrigerated air system employing input air from turbine engine compressor after bypassing and conditioning within auxiliary system
US6089028A (en) * 1998-03-27 2000-07-18 Exxonmobil Upstream Research Company Producing power from pressurized liquefied natural gas
US6116031A (en) * 1998-03-27 2000-09-12 Exxonmobil Upstream Research Company Producing power from liquefied natural gas
EP1064506A4 (fr) * 1998-03-18 2002-11-13 Exxonmobil Oil Corp Regazeification de gnl a bord d'un navire de transport
US6598408B1 (en) * 2002-03-29 2003-07-29 El Paso Corporation Method and apparatus for transporting LNG
US20030159800A1 (en) * 2002-02-27 2003-08-28 Nierenberg Alan B. Method and apparatus for the regasification of LNG onboard a carrier
WO2004031644A1 (fr) * 2002-10-04 2004-04-15 Hamworthy Kse A.S. Systeme et procede de regazification
US20050061002A1 (en) * 2003-08-12 2005-03-24 Alan Nierenberg Shipboard regasification for LNG carriers with alternate propulsion plants
WO2005043034A1 (fr) * 2003-10-29 2005-05-12 Shell Internationale Research Maatschappij B.V. Systemes de vaporisation destines a des structures de reception et de stockage de gaz naturel liquefie
US20050115248A1 (en) * 2003-10-29 2005-06-02 Koehler Gregory J. Liquefied natural gas structure
WO2005041396A3 (fr) * 2003-10-22 2007-02-08 Paul L Scherzer Procede et systeme destines a generer de l'electricite au moyen de gaz d'origine naturelle
WO2007105957A1 (fr) * 2006-03-15 2007-09-20 Torp Technology As Appareil pour un navire équipé d'un évaporateur de gaz naturel liquéfié
US20070214805A1 (en) * 2006-03-15 2007-09-20 Macmillan Adrian Armstrong Onboard Regasification of LNG Using Ambient Air
US20070271932A1 (en) * 2006-05-26 2007-11-29 Chevron U.S.A. Inc. Method for vaporizing and heating a cryogenic fluid
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas
US20080127673A1 (en) * 2004-11-05 2008-06-05 Bowen Ronald R Lng Transportation Vessel and Method For Transporting Hydrocarbons
US20090193780A1 (en) * 2006-09-11 2009-08-06 Woodside Energy Limited Power Generation System for a Marine Vessel
US20090249799A1 (en) * 2008-04-07 2009-10-08 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Apparatus and method for increasing efficiency of a gas turbine and a marine structure having the same
US20090249798A1 (en) * 2008-04-07 2009-10-08 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Apparatus and method for increasing efficiency of a gas turbine and a marine structure having the same
US20100263389A1 (en) * 2009-04-17 2010-10-21 Excelerate Energy Limited Partnership Dockside Ship-To-Ship Transfer of LNG
US20110030391A1 (en) * 2009-08-06 2011-02-10 Woodside Energy Limited Mechanical Defrosting During Continuous Regasification of a Cryogenic Fluid Using Ambient Air
US8069677B2 (en) 2006-03-15 2011-12-06 Woodside Energy Ltd. Regasification of LNG using ambient air and supplemental heat
JP2016102554A (ja) * 2014-11-28 2016-06-02 大阪瓦斯株式会社 液化ガス用気化装置
US9919774B2 (en) 2010-05-20 2018-03-20 Excelerate Energy Limited Partnership Systems and methods for treatment of LNG cargo tanks
US10539361B2 (en) 2012-08-22 2020-01-21 Woodside Energy Technologies Pty Ltd. Modular LNG production facility

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US2111618A (en) * 1935-06-26 1938-03-22 Gen Refrigeration Corp Air conditioning apparatus
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DE1247751B (de) * 1963-02-07 1967-08-17 Siemens Ag Gasturbinen-Speicherkraftanlage
US3266261A (en) * 1964-11-27 1966-08-16 James H Anderson Method and apparatus for evaporating liquefied gases
US3421574A (en) * 1966-03-11 1969-01-14 Niagara Blower Co Method and apparatus for vaporizing and superheating cold liquefied gas
US3675436A (en) * 1970-02-25 1972-07-11 Struthers Scient And Intern Co Desalination process
DE2402043A1 (de) * 1974-01-11 1975-07-24 Sulzer Ag Verfahren und anlage zur verdampfung und erwaermung von verfluessigtem erdgas
US3986340A (en) * 1975-03-10 1976-10-19 Bivins Jr Henry W Method and apparatus for providing superheated gaseous fluid from a low temperature liquid supply
DE2751642A1 (de) * 1977-11-17 1979-08-09 Borsig Gmbh Verfahren zur umwandlung einer tiefsiedenden fluessigkeit, insbesondere unter atmosphaerendruck stehendem erdgas oder methan, in den gasfoermigen zustand mit anschliessender erwaermung
US4438729A (en) * 1980-03-31 1984-03-27 Halliburton Company Flameless nitrogen skid unit
US5551242A (en) * 1980-03-31 1996-09-03 Halliburton Company Flameless nitrogen skid unit
EP0048316A1 (fr) * 1980-09-19 1982-03-31 Uhde GmbH Procédé et dispositif pour la révaporisation de gaz naturel liquéfié
DE3035349A1 (de) * 1980-09-19 1982-04-08 Uhde Gmbh, 4600 Dortmund Verfahren und anlage zur rueckverdampfung von fluessigem erdgas
US4372124A (en) * 1981-03-06 1983-02-08 Air Products And Chemicals, Inc. Recovery of power from the vaporization of natural gas
US4437312A (en) 1981-03-06 1984-03-20 Air Products And Chemicals, Inc. Recovery of power from vaporization of liquefied natural gas
US4479350A (en) * 1981-03-06 1984-10-30 Air Products And Chemicals, Inc. Recovery of power from vaporization of liquefied natural gas
US4458633A (en) * 1981-05-18 1984-07-10 Halliburton Company Flameless nitrogen skid unit
US4995234A (en) * 1989-10-02 1991-02-26 Chicago Bridge & Iron Technical Services Company Power generation from LNG
US5036678A (en) * 1990-03-30 1991-08-06 General Electric Company Auxiliary refrigerated air system employing mixture of air bled from turbine engine compressor and air recirculated within auxiliary system
US5056335A (en) * 1990-04-02 1991-10-15 General Electric Company Auxiliary refrigerated air system employing input air from turbine engine compressor after bypassing and conditioning within auxiliary system
EP1064506A4 (fr) * 1998-03-18 2002-11-13 Exxonmobil Oil Corp Regazeification de gnl a bord d'un navire de transport
KR100569621B1 (ko) * 1998-03-18 2006-04-11 엑손모빌 오일 코포레이션 수송선 상에서 액화천연가스를 가스화하는 방법 및 시스템
US6089028A (en) * 1998-03-27 2000-07-18 Exxonmobil Upstream Research Company Producing power from pressurized liquefied natural gas
US6116031A (en) * 1998-03-27 2000-09-12 Exxonmobil Upstream Research Company Producing power from liquefied natural gas
EP1075588A4 (fr) * 1998-03-27 2003-06-18 Exxonmobil Upstream Res Co Production d'energie a partir de gaz naturel liquefie sous pression
US20100192597A1 (en) * 2002-02-27 2010-08-05 Excelerate Energy Limited Partnership Method and Apparatus for the Regasification of LNG Onboard a Carrier
US20030159800A1 (en) * 2002-02-27 2003-08-28 Nierenberg Alan B. Method and apparatus for the regasification of LNG onboard a carrier
US7293600B2 (en) 2002-02-27 2007-11-13 Excelerate Energy Limited Parnership Apparatus for the regasification of LNG onboard a carrier
US20080148742A1 (en) * 2002-02-27 2008-06-26 Nierenberg Alan B Method and apparatus for the regasification of lng onboard a carrier
US6598408B1 (en) * 2002-03-29 2003-07-29 El Paso Corporation Method and apparatus for transporting LNG
WO2004031644A1 (fr) * 2002-10-04 2004-04-15 Hamworthy Kse A.S. Systeme et procede de regazification
US7484371B2 (en) 2003-08-12 2009-02-03 Excelerate Energy Limited Partnership Shipboard regasification for LNG carriers with alternate propulsion plants
US7219502B2 (en) 2003-08-12 2007-05-22 Excelerate Energy Limited Partnership Shipboard regasification for LNG carriers with alternate propulsion plants
US20050061002A1 (en) * 2003-08-12 2005-03-24 Alan Nierenberg Shipboard regasification for LNG carriers with alternate propulsion plants
US7608935B2 (en) 2003-10-22 2009-10-27 Scherzer Paul L Method and system for generating electricity utilizing naturally occurring gas
US20070120367A1 (en) * 2003-10-22 2007-05-31 Scherzer Paul L Method and system for generating electricity utilizing naturally occurring gas
WO2005041396A3 (fr) * 2003-10-22 2007-02-08 Paul L Scherzer Procede et systeme destines a generer de l'electricite au moyen de gaz d'origine naturelle
US20050115248A1 (en) * 2003-10-29 2005-06-02 Koehler Gregory J. Liquefied natural gas structure
WO2005043034A1 (fr) * 2003-10-29 2005-05-12 Shell Internationale Research Maatschappij B.V. Systemes de vaporisation destines a des structures de reception et de stockage de gaz naturel liquefie
US8156758B2 (en) 2004-09-14 2012-04-17 Exxonmobil Upstream Research Company Method of extracting ethane from liquefied natural gas
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas
US20080127673A1 (en) * 2004-11-05 2008-06-05 Bowen Ronald R Lng Transportation Vessel and Method For Transporting Hydrocarbons
US8069677B2 (en) 2006-03-15 2011-12-06 Woodside Energy Ltd. Regasification of LNG using ambient air and supplemental heat
US8607580B2 (en) 2006-03-15 2013-12-17 Woodside Energy Ltd. Regasification of LNG using dehumidified air
WO2007105957A1 (fr) * 2006-03-15 2007-09-20 Torp Technology As Appareil pour un navire équipé d'un évaporateur de gaz naturel liquéfié
US20070214805A1 (en) * 2006-03-15 2007-09-20 Macmillan Adrian Armstrong Onboard Regasification of LNG Using Ambient Air
US20070271932A1 (en) * 2006-05-26 2007-11-29 Chevron U.S.A. Inc. Method for vaporizing and heating a cryogenic fluid
US20090193780A1 (en) * 2006-09-11 2009-08-06 Woodside Energy Limited Power Generation System for a Marine Vessel
US20090199575A1 (en) * 2006-09-11 2009-08-13 Woodside Energy Limited Boil off gas management during ship-to-ship transfer of lng
US20090249798A1 (en) * 2008-04-07 2009-10-08 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Apparatus and method for increasing efficiency of a gas turbine and a marine structure having the same
US20090249799A1 (en) * 2008-04-07 2009-10-08 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Apparatus and method for increasing efficiency of a gas turbine and a marine structure having the same
US20100263389A1 (en) * 2009-04-17 2010-10-21 Excelerate Energy Limited Partnership Dockside Ship-To-Ship Transfer of LNG
US20110030391A1 (en) * 2009-08-06 2011-02-10 Woodside Energy Limited Mechanical Defrosting During Continuous Regasification of a Cryogenic Fluid Using Ambient Air
US9919774B2 (en) 2010-05-20 2018-03-20 Excelerate Energy Limited Partnership Systems and methods for treatment of LNG cargo tanks
US10539361B2 (en) 2012-08-22 2020-01-21 Woodside Energy Technologies Pty Ltd. Modular LNG production facility
JP2016102554A (ja) * 2014-11-28 2016-06-02 大阪瓦斯株式会社 液化ガス用気化装置
WO2016084765A1 (fr) * 2014-11-28 2016-06-02 大阪瓦斯株式会社 Dispositif de vaporisation de gaz liquéfié

Also Published As

Publication number Publication date
LU37293A1 (fr) 1959-08-10
FR1226947A (fr) 1960-08-18
BE579483A (fr) 1959-10-01
SE220248C1 (en) 1968-04-30
GB861919A (en) 1961-03-01
ES250007A1 (es) 1959-12-16
NL112932C (nl) 1966-06-15

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