Nothing Special   »   [go: up one dir, main page]

US2799997A - Method and apparatus for reducing power needed for compression - Google Patents

Method and apparatus for reducing power needed for compression Download PDF

Info

Publication number
US2799997A
US2799997A US455052A US45505254A US2799997A US 2799997 A US2799997 A US 2799997A US 455052 A US455052 A US 455052A US 45505254 A US45505254 A US 45505254A US 2799997 A US2799997 A US 2799997A
Authority
US
United States
Prior art keywords
gas
heat exchange
compression
chamber
gaseous materials
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US455052A
Inventor
Willard L Morrison
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Constock Liquid Methane Corp
Original Assignee
Constock Liquid Methane Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Constock Liquid Methane Corp filed Critical Constock Liquid Methane Corp
Priority to US455052A priority Critical patent/US2799997A/en
Priority claimed from GB1454157A external-priority patent/GB799765A/en
Application granted granted Critical
Publication of US2799997A publication Critical patent/US2799997A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/06—Fluid distribution
    • F17C2265/066—Fluid distribution for feeding engines for propulsion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/011—Barges

Definitions

  • This invention relates to processes involving the compression of various gaseous materials and has for one object to provide a method for reducing the power necessary to compress said gaseous materials.
  • Another object is to provide an apparatus-eifective to reduce the power necessary to compress gaseous materials.
  • Another object is to provide a method of cooling gaseous materials which are to be compressed prior to such compressin in order to reduce the power necessary to compress said gaseous materials to a desired pressure.
  • Another object is to provide a method of cooling gaseous materials prior to their compression in order to reduce the power necessary for such compression wherein the cooling medium may be utilized, also to produce the power required for such compression.
  • the carrier 1 is a barge or similar carrier which may be tied up at a dock or similarly located alongside a plant wherein gaseous materials are processed, the process involving at one or more stages the compression of such gaseous materials.
  • the carrier 1 may have one or more containers or tanks such as that illustrated at 2. Any suitable pumping means such as the pump generally shown at 3 may be employed to transfer a supply of liquefied natural gas from the containers 2, for example, through the piping or conduit 4 to a reservoir 5. Similarly a pumping means 6 may be employed to transfer the liquefied natural gas from the reservoir through pipe 7.
  • a coil 8 may be connected to the pipe 7 as indicated at 9 and may be enclosed within a heat exchange chamber 10.
  • a conduit 11 may be employed to convey the gaseous materials which are to be compressed, to the chamber 10, for heat exchange contact with coil 8.
  • a conduit 12 is connected to the heat exchange chamber to convey the gaseous material which have been cooled therein from the chamber 10 to a compressor mechanism 13.
  • the coil 8 has an outlet pipe 14 leading from the chamber it
  • a branch conduit 15 is connected at one end to the pipe 14 and at its opposite end to an internal combustion engine which is powered by gas vaporized and warmed by heat exchange in coil 8, illustrated diagrammatically at 16.
  • the pipe 11 is connected to a source of supply of gaseous materials and that the pipe 14 may be connected to a variety of mechanisms and may in fact be so connected as to direct the natural gas which has been vaporized by heat exchange in the chamber 10 to a point of use in the process of the plant in which the gaseous materials are treated. Since the elements to which the pipes 11 and 14 may be connected do not form any ice part of the present invention they are not illustrated or further discussed herein.
  • An outlet conduit 20 leads from the compressor 13 and conducts the gaseous materials compressed therein to a second heat exchange chamber 21.
  • a water pump 22 is effective to direct water under pressure through a water pipe 23.
  • a coil 24 is positioned within the heat exchange chamber 21 and is connected, at one end to the branch conduit 25 leading from pipe 23 and at its opposite end to a water discharge pipe 26 extending from the chamber 21.
  • An outlet pipe 27 is connected to the chamber 21 to conduct the gaseous materials which have been cooled within the chamber 21 by the water passing through the coil 24, to a third heat exchange chamber 28 which contains the coil 29.
  • the coil 29 is connected at one end to the liquid natural gas supply pipe 7 and at its opposite end to an outlet conduit 30.
  • An outlet pipe 31 is connected to the chamber 28 to convey the gas cooled therein by the liquid natural gas flowing through the coil 29 to a second compressor 35.
  • a branch conduit 36 is connected to the pipe 30 to convey the natural gas vaporized and warmed by heat exchange, to an internal combustion engine illustrated at 37.
  • the pipe 30 may be connected to a suitable mechanism as described above with relation to pipe 14.
  • the outlet pipe 45 is a discharge conduit leading from compressor 35 to conduct the gaseous materials compressed therein to a fourth heat exchange chamber 41 through which extends the coil 42 which is connected at one end to the water supply pipe 23 and at its opposite end to the water discharge pipe 43.
  • 45 is an outlet conduit connected to the chamber 41 to convey the gaseous materials cooled therein by heat exchange with the water passing through the coil 42.
  • the outlet pipe 45 may be connected to a variety of mechanisms employed in the processing plant or, if desired, it may be connected to a fifth heat exchange chamber similar to the chamber 28. It will be realized that the mechanism illustrated diagrammatically at 8-20 may be repeated at any desired number of points without departing from the nature and scope of the invention.
  • a method for reducing the power necessary to compress gaseous materials which involves the concept of cooling the gases prior to such compression by the use of liquefied natural gas as a refrigerant passed in heat exchange relationship with such gaseous materials immediately prior to compression thereof.
  • the liquefied methane which is supplied in tonnage quantities at a temperature of -258 F. within the containers 2 and reservoir 5 is pumped through the heat exchange coil 8.
  • the gaseous materials entering the heat exchange chamber 10 are thus cooled as they pass about the coil 8 and the liquefied natural gas is vaporized.
  • the cooled gaseous materials are conveyed from the chamber 10 to a compressor 13 by the conduit 12.
  • a portion of the vaporized natural gas flowing from the coil 8 through the pipe 14 is bled off and directed into the internal combustion engine 16 where it serves as a fuel to provide the power necessary to operate the compressor 13.
  • the refrigerant eifect is utilized to cool gaseous materials about to be compressed and to use also at least a portion of the natural gas in gaseous phase resulting from such cooling as a fuel to provide the necessary compression power.
  • compressor outlet 20 could be, under certain circumstances, connected directlyto the heat exchange chamber 28 wherein the gases which were heated to some extent by the [compressor 13 would be again cooled beforeentering a. second compressor 35.
  • Such gasification will take place if the pressure in those coils issubstantially at atmospheric because liquefied methane or natural gas boils at approximately -258 P.
  • the pressure in the coils '8 and 29 is maintained above atmospheric, then the boiling point of the liquefied methane. will be above --258 F.
  • steps which comprise: (a) in a first step passing the cold methane in heat exchange with the second gasto substantially reduce its temperature and. increase its density, (b) in a second stage compressing the said second gas efiiuent from said first stage, (0) in a third stage water cooling the second gas efiluent from said second stage, (d)' in a fourth stage passing a further stream of cold methane in heat exchange relation with said second gas efiluent' from said third stage, (e) in a fifth stage compressing the second. gas effluent from said fourth stage, and (f) in a sixth stage water.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

July 2 1957' w. L. MORRISON 2,799,997
METHOD AND APPARATUS FOR REDUCING POWER NEEDED FOR COMPRESSION Filed Sept. 9, 1954 INVENTOR, Willard L. Morrison y Parker 8: Carter ATTORNEYS United States atent METHOD AND APPARATUS FOR REDUCING PQWER NEEDED FOR CGMPRESSION Willard L. Morrison, Lake Forest, Ill., assignor, by direct and mesne assignments, to Constock Liquid Methane Corporation, a corporation of Delaware Application September 9, 1954, Serial No. 455,652
4 Claims. (Cl. 62-1) This invention relates to processes involving the compression of various gaseous materials and has for one object to provide a method for reducing the power necessary to compress said gaseous materials.
Another object is to provide an apparatus-eifective to reduce the power necessary to compress gaseous materials.
Another object is to provide a method of cooling gaseous materials which are to be compressed prior to such compressin in order to reduce the power necessary to compress said gaseous materials to a desired pressure.
Another object is to provide a method of cooling gaseous materials prior to their compression in order to reduce the power necessary for such compression wherein the cooling medium may be utilized, also to produce the power required for such compression.
Other objects will appear from time to time in the course of the specification and claims.
The invention is illustrated more or less diagrammatically in the accompanying drawing wherein the single figure comprising the drawing is a top plan view in cross section.
Like parts are indicated by like characters throughout the specification and drawings.
Referring to the drawing, 1 is a barge or similar carrier which may be tied up at a dock or similarly located alongside a plant wherein gaseous materials are processed, the process involving at one or more stages the compression of such gaseous materials. The carrier 1 may have one or more containers or tanks such as that illustrated at 2. Any suitable pumping means such as the pump generally shown at 3 may be employed to transfer a supply of liquefied natural gas from the containers 2, for example, through the piping or conduit 4 to a reservoir 5. Similarly a pumping means 6 may be employed to transfer the liquefied natural gas from the reservoir through pipe 7. A coil 8 may be connected to the pipe 7 as indicated at 9 and may be enclosed within a heat exchange chamber 10. A conduit 11 may be employed to convey the gaseous materials which are to be compressed, to the chamber 10, for heat exchange contact with coil 8. A conduit 12 is connected to the heat exchange chamber to convey the gaseous material which have been cooled therein from the chamber 10 to a compressor mechanism 13. The coil 8 has an outlet pipe 14 leading from the chamber it A branch conduit 15 is connected at one end to the pipe 14 and at its opposite end to an internal combustion engine which is powered by gas vaporized and warmed by heat exchange in coil 8, illustrated diagrammatically at 16.
It will be realized that the pipe 11 is connected to a source of supply of gaseous materials and that the pipe 14 may be connected to a variety of mechanisms and may in fact be so connected as to direct the natural gas which has been vaporized by heat exchange in the chamber 10 to a point of use in the process of the plant in which the gaseous materials are treated. Since the elements to which the pipes 11 and 14 may be connected do not form any ice part of the present invention they are not illustrated or further discussed herein.
An outlet conduit 20 leads from the compressor 13 and conducts the gaseous materials compressed therein to a second heat exchange chamber 21. A water pump 22 is effective to direct water under pressure through a water pipe 23. A coil 24 is positioned within the heat exchange chamber 21 and is connected, at one end to the branch conduit 25 leading from pipe 23 and at its opposite end to a water discharge pipe 26 extending from the chamber 21. An outlet pipe 27 is connected to the chamber 21 to conduct the gaseous materials which have been cooled within the chamber 21 by the water passing through the coil 24, to a third heat exchange chamber 28 which contains the coil 29. The coil 29 is connected at one end to the liquid natural gas supply pipe 7 and at its opposite end to an outlet conduit 30. An outlet pipe 31 is connected to the chamber 28 to convey the gas cooled therein by the liquid natural gas flowing through the coil 29 to a second compressor 35. A branch conduit 36 is connected to the pipe 30 to convey the natural gas vaporized and warmed by heat exchange, to an internal combustion engine illustrated at 37. The pipe 30 may be connected to a suitable mechanism as described above with relation to pipe 14.
40 is a discharge conduit leading from compressor 35 to conduct the gaseous materials compressed therein to a fourth heat exchange chamber 41 through which extends the coil 42 which is connected at one end to the water supply pipe 23 and at its opposite end to the water discharge pipe 43. 45 is an outlet conduit connected to the chamber 41 to convey the gaseous materials cooled therein by heat exchange with the water passing through the coil 42. The outlet pipe 45 may be connected to a variety of mechanisms employed in the processing plant or, if desired, it may be connected to a fifth heat exchange chamber similar to the chamber 28. It will be realized that the mechanism illustrated diagrammatically at 8-20 may be repeated at any desired number of points without departing from the nature and scope of the invention.
59 illustrates fiy-wheels employed with the compressors 13, 35.
The use and operation of this invention are as follows:
A method is provided for reducing the power necessary to compress gaseous materials which involves the concept of cooling the gases prior to such compression by the use of liquefied natural gas as a refrigerant passed in heat exchange relationship with such gaseous materials immediately prior to compression thereof.
The liquefied methane which is supplied in tonnage quantities at a temperature of -258 F. within the containers 2 and reservoir 5 is pumped through the heat exchange coil 8. The gaseous materials entering the heat exchange chamber 10 are thus cooled as they pass about the coil 8 and the liquefied natural gas is vaporized. The cooled gaseous materials are conveyed from the chamber 10 to a compressor 13 by the conduit 12. A portion of the vaporized natural gas flowing from the coil 8 through the pipe 14 is bled off and directed into the internal combustion engine 16 where it serves as a fuel to provide the power necessary to operate the compressor 13. Thus, by liquefying natural gas and supplying it in quantity, the refrigerant eifect is utilized to cool gaseous materials about to be compressed and to use also at least a portion of the natural gas in gaseous phase resulting from such cooling as a fuel to provide the necessary compression power.
As natural gas is often used as one of the raw materials in certain processing plants and since only a portion of the natural gas vaporized in the chamber 11 is necessary to provide the amount of power needed for compressing the gaseousmateria1s which. have been cooled within the chamber 10,. the. remaining vaporized natural gas. may
be used as raw material in the process within the plant,
or may be diverted to other use in or out of the plant.
1 The gaseous materials: compressed by the compressor 13 flow outward therefrom through the outlet 'c'onduitiZti,"
havingbeenraisedin tmperaturebycompression. Under certain Circumstances it may b e'foundadvisableto produce water cooled heat exchanger through the conduit 27 maybe "directed into the compressing plant or may be again cooled by means corresponding to those already described. I 7
It will beunderstood that the compressor outlet 20 could be, under certain circumstances, connected directlyto the heat exchange chamber 28 wherein the gases which were heated to some extent by the [compressor 13 would be again cooled beforeentering a. second compressor 35.
It isknown that the horsepower required to compress gases per unit mass varies directly as the inlet absolute temperature from the same initial pressure to the same final pressure. While various means have been employed to cool. said gases prior to compression, I have found that natural gas liquefied at about -258 F. may be utilized efiectively to cool said gases prior to compression and this use of natural gas is productive of particularly advantageous results in that the natural gas, when supplied .in large quantities in liquefied form at or about --258 F..may be utilized first, as an effective coolant for gaseous materials in a processing plant, then as a fuel to power the compression mechanism, and thirdly, as a raw material usable in the process within the plant. Also any surplus of natural gas in gaseous phase resulting from the use of liquefied natural gas as a coolant may be utilized as a fuel toeconomically and effectively power other mechanisms within the plant.
While .I have illustrated my invention as using the gas as fuel in internal combustion engines, it will be obvious that the gas might be used just as well as fuel for any other means of generating the necessary power.
I have referred to the vaporization of the liquefied gas by heat exchange as it passes through the coils 8 and 29. Such gasification will take place if the pressure in those coils issubstantially at atmospheric because liquefied methane or natural gas boils at approximately -258 P. On the other hand, if by control of the exhaust pressure through the pipes 14 and 3t) and by operation of the pump 6, the pressure in the coils '8 and 29 is maintained above atmospheric, then the boiling point of the liquefied methane. will be above --258 F.
I claim:
1. In the method of raising the temperature of a stream.
of methane from about minus 258 F. to substantially atmospheric temperature while simultaneously substantially compressing a stream of a second gas, the steps which comprise: (a) in a first step passing the cold methane in heat exchange with the second gasto substantially reduce its temperature and. increase its density, (b) in a second stage compressing the said second gas efiiuent from said first stage, (0) in a third stage water cooling the second gas efiluent from said second stage, (d)' in a fourth stage passing a further stream of cold methane in heat exchange relation with said second gas efiluent' from said third stage, (e) in a fifth stage compressing the second. gas effluent from said fourth stage, and (f) in a sixth stage water.
cooling to substantially atmospheric temperature the second gas effluent from said fifth stage.
2. The method of substantially raising the temperature of a stream of a first gas from a temperature substantially below atmospheric t'o'substantially atmospheric temperature while simultaneously compressing a second gas to a substantially elevated pressure which comprises in progressive stages compressing said second gas stream, passing the stream of said second gas entering each com-s pressor in heat exchange relation with separate portions of said first gas, and water cooling the stream of said second gas as 'it leaves, each of said compressors, and subsequently utilizing said heated-up first gas as a fuel. 7
3. The method of claim 1 characterized further in that a portion of the methane stream after heat exchange with 7 the combination of a plurality of heat exchangers,rmeans to convey said second gas stream sequentially through said' heat exchangers means of conveying difierent portions respectively of the stream of said first gas through said heat exchangers, means for compressing said second gas stream after it has passed through one of saidheat exchangers and means for conveying water in heat exchange relation with said stream of said second gas as it leaves at least one of said compressors.
References'Cited in the file of this patent UNITED STATES PATENTS Cooper Oct., 18,
US455052A 1954-09-09 1954-09-09 Method and apparatus for reducing power needed for compression Expired - Lifetime US2799997A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US455052A US2799997A (en) 1954-09-09 1954-09-09 Method and apparatus for reducing power needed for compression

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US455052A US2799997A (en) 1954-09-09 1954-09-09 Method and apparatus for reducing power needed for compression
GB1454157A GB799765A (en) 1957-05-07 1957-05-07 Means for heating a gas and for the compression of another gas

Publications (1)

Publication Number Publication Date
US2799997A true US2799997A (en) 1957-07-23

Family

ID=26250635

Family Applications (1)

Application Number Title Priority Date Filing Date
US455052A Expired - Lifetime US2799997A (en) 1954-09-09 1954-09-09 Method and apparatus for reducing power needed for compression

Country Status (1)

Country Link
US (1) US2799997A (en)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2965688A (en) * 1957-03-05 1960-12-20 British Oxygen Co Ltd Cooling selective acetylene solvent by heat exchange with vaporizing liquid methane
US2975608A (en) * 1957-07-01 1961-03-21 Conch Int Methane Ltd Transportation and use of liquefied natural gas
US2975607A (en) * 1958-06-11 1961-03-21 Conch Int Methane Ltd Revaporization of liquefied gases
US2983585A (en) * 1957-12-11 1961-05-09 British Oxygen Co Ltd Preparation of liquid hydrogen
US3034309A (en) * 1955-01-19 1962-05-15 Otto H Muck Method for transporting gas
US3054269A (en) * 1956-06-29 1962-09-18 Cooper Bessemer Corp Liquification of gas
US3058314A (en) * 1957-08-12 1962-10-16 British Oxygen Co Ltd Process and apparatus for the low temperature separation of air
US3183677A (en) * 1960-06-16 1965-05-18 Conch Int Methane Ltd Liquefaction of nitrogen in regasification of liquid methane
US3256705A (en) * 1963-12-26 1966-06-21 Dimentberg Moses Apparatus for and method of gas transportation
US3324670A (en) * 1964-11-09 1967-06-13 Shell Oil Co Method of transporting methane or natural gas
US3365898A (en) * 1965-06-03 1968-01-30 Shell Oil Co Method for transporting gas
US5678411A (en) * 1995-04-26 1997-10-21 Ebara Corporation Liquefied gas supply system

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1266621A (en) * 1918-01-26 1918-05-21 Cons Liquid Gas Company Gas process.
US1808494A (en) * 1926-02-15 1931-06-02 Shell Petroleum Corp Refrigerating process
US1935749A (en) * 1927-01-25 1933-11-21 Schlumbohm Peter Vacuum refrigerating machine
US2456386A (en) * 1946-05-07 1948-12-14 Howell C Cooper Cascade refrigeration unit with controls therefor
US2484875A (en) * 1945-12-22 1949-10-18 Howell C Cooper Heat transfer and precipitation means

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1266621A (en) * 1918-01-26 1918-05-21 Cons Liquid Gas Company Gas process.
US1808494A (en) * 1926-02-15 1931-06-02 Shell Petroleum Corp Refrigerating process
US1935749A (en) * 1927-01-25 1933-11-21 Schlumbohm Peter Vacuum refrigerating machine
US2484875A (en) * 1945-12-22 1949-10-18 Howell C Cooper Heat transfer and precipitation means
US2456386A (en) * 1946-05-07 1948-12-14 Howell C Cooper Cascade refrigeration unit with controls therefor

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3034309A (en) * 1955-01-19 1962-05-15 Otto H Muck Method for transporting gas
US3054269A (en) * 1956-06-29 1962-09-18 Cooper Bessemer Corp Liquification of gas
US2965688A (en) * 1957-03-05 1960-12-20 British Oxygen Co Ltd Cooling selective acetylene solvent by heat exchange with vaporizing liquid methane
US2975608A (en) * 1957-07-01 1961-03-21 Conch Int Methane Ltd Transportation and use of liquefied natural gas
US3058314A (en) * 1957-08-12 1962-10-16 British Oxygen Co Ltd Process and apparatus for the low temperature separation of air
US2983585A (en) * 1957-12-11 1961-05-09 British Oxygen Co Ltd Preparation of liquid hydrogen
US2975607A (en) * 1958-06-11 1961-03-21 Conch Int Methane Ltd Revaporization of liquefied gases
US3183677A (en) * 1960-06-16 1965-05-18 Conch Int Methane Ltd Liquefaction of nitrogen in regasification of liquid methane
US3256705A (en) * 1963-12-26 1966-06-21 Dimentberg Moses Apparatus for and method of gas transportation
US3324670A (en) * 1964-11-09 1967-06-13 Shell Oil Co Method of transporting methane or natural gas
US3365898A (en) * 1965-06-03 1968-01-30 Shell Oil Co Method for transporting gas
US5678411A (en) * 1995-04-26 1997-10-21 Ebara Corporation Liquefied gas supply system

Similar Documents

Publication Publication Date Title
US3885394A (en) Process and apparatus for treating and utilizing vaporized gas in a ship for transporting liquified gas
US3511058A (en) Liquefaction of natural gas for peak demands using split-stream refrigeration
US3347055A (en) Method for recuperating refrigeration
US2799997A (en) Method and apparatus for reducing power needed for compression
US8555672B2 (en) Complete liquefaction methods and apparatus
US3002362A (en) Natural gas expansion refrigeration system
US5473900A (en) Method and apparatus for liquefaction of natural gas
RU2304746C2 (en) Method and device for liquefying natural gas
RU2541360C1 (en) Liquefied natural gas production method and complex for its implementation
US3183666A (en) Method of gasifying a liquid gas while producing mechanical energy
US2535148A (en) Method of storing natural gas
EP0113539A2 (en) Method and apparatus for producing liquid natural gas
CN211924353U (en) Marine liquid ammonia fuel feed system
EP1724514A1 (en) Vaporizor
IL28868A (en) Process for liquefaction of natural gas and transportation by marine vessel
GB1334977A (en) Method of continuously vapourising and superheating liquefied cryogenic fluid
US2632302A (en) Volatile liquid pumping
CN110325807A (en) Utilize the liquified natural gas liquefier of mechanical refrigeration and liquid nitrogen refrigerating
US20110094261A1 (en) Natural gas liquefaction core modules, plants including same and related methods
US6085545A (en) Liquid natural gas system with an integrated engine, compressor and expander assembly
JPS62278399A (en) Device and method of vaporizing liquefied hydrocarbon
RU2696145C1 (en) Method and device for treating evaporated gas for feeding at least to an engine
US3630042A (en) Method and system for desalinization of water
RU2673972C1 (en) Complex for reduction, liquidation and compression of natural gas (options)
US3319434A (en) Low temperature refrigeration and gas storage