US2909906A - Low temperature refrigeration - Google Patents

Low temperature refrigeration Download PDF

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US2909906A
US2909906A US531125A US53112555A US2909906A US 2909906 A US2909906 A US 2909906A US 531125 A US531125 A US 531125A US 53112555 A US53112555 A US 53112555A US 2909906 A US2909906 A US 2909906A
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gas
stream
methane
nitrogen
temperature
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Philip E Bocquet
Shao E Tung
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Constock Liquid Methane Corp
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Constock Liquid Methane Corp
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Priority to LU37632D priority Critical patent/LU37632A1/xx
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Priority to US531125A priority patent/US2909906A/en
Priority to GB29696/59A priority patent/GB860723A/en
Priority to DEC19759A priority patent/DE1126435B/de
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0017—Oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—Nitrogen
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • 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
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/66—Butane or mixed butanes
    • 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
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being nitrogen
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

Definitions

  • This invention relates to improvements in the art of refrigeration, and more particularly, but not by way of limitation, to an improved refrigeration process of liquefying methane by use of initially liquid nitrogen.
  • the present invention has conveniently definable utility when applied to the liquefaction of methane by nitrogen. Therefore, the invention will be described with detailed reference to these particular fluids. It is to be understood, however, that the present process is not limited to the use of these fluids, but may be practiced with various other uids having similar relations, as will be more fully hereinafter set forth.
  • Liquid nitrogen may be conveniently used to obtain at least a portion of this refrigeration. The liquid nitrogen may be obtained at approximately atmospheric pressure and at 320 F., and will absorb approximately 168 B.t.u./lb. in being heated to 80 F. Following present teachings, the liquefaction would be accomplished by simply heat interchanging the nitrogen and methane at atmospheric pressure.
  • the methane would be liquefied by such a process, but either approximately 2.1 pounds of nitrogen must be used for liquefactionof each pound of methane, or a substantial amount of external refrigeration must be used, since the methane will require 398 B.t.u./lb. refrigeration and the nitrogen supplies only 186 B.t.u./ lb.
  • the present invention contemplates a process of liquefying methane by nitrogen, wherein one pound of methane may be liquefied by each pound of nitrogen with only a minor use of external refrigeration; and wherein the process produces mechanical power which may be used in the production of the external refrigeration. It is proposed to pressurize the liquid nitrogen, and then provide two heat exchanges of the nitrogen with a stream of methane. It is proposed to feed the methane at a pressure as near to well head pressure as possible. lf the pressure is too low, the methane may be compressed prior to the refrigeration thereof, to obtain a better balance inv the demand and supply of refrigeration during the process.
  • An important object of this invention is to increase the refrigeration which may be obtained by an initially liquid refrigerant.
  • Another object of this invention is to provide a process a gas stream by refrigeration, wherein the mass rates of the stream and the refrigerant are substantially equal.
  • Another object of this invention is to provide a process of liquefying a gas stream by refrigeration, wherein the refrigerant produces mechanical power during the process.
  • a further object of this invention is to provide an economical process of liquefying a gas stream which may b simply performed by standard equipment.
  • Another object of this invention is to provide a process of liquefying a gas stream by an initially liquid refrigerant, wherein the refrigerant is interchanged with the stream in two passes of the refrigerant 'through substantially equal temperature zones.
  • a still further object of this invention is to provide a process of liquefying a gas stream by interchange with a refrigerant and a supplemental refrigerant, wherein the mass rates of the stream and refrigerant are equal, yet the refrigerant supplies the major portion of the required refrigeration.
  • Still another object of this invention is to provide a process of liquefying a gas 'stream by interchange with an initially liquid refrigerant, wherein the refrigerant is cooled at an intermediate point in the process for a second interchange with the stream.
  • the present invention may be defined as the method of refrigerating a rst fluid which comprises:
  • reference characters 2, 4, and 6 designate three heat exchangers arranged in side-by-side relation.
  • the smaller heat exchanger 2 has two flow passageways 8 and 10 therethrough for the passageof the refrigerant and the stream being liquefied, respectively, as will be more fully hereinafter set forth.
  • the central heat exchanger 4 has three llow passageways 12, 14, and 16 therethrough, and the larger heat exchanger 6 has four ilow passageways 18, 2i), 22, and 24 therethrough. lt will be understood that the heat exchangers 2, 4, and 6 are shown diagrammatically and that the various liow passageways may be arranged in any suitable manner to obtain the desired refrigeration, as will be subsequently described.
  • the apparatus required for practicing the present invention also includes a source of outside refrigeration 26, which communicates with the flow passageway 24 of the heat exchanger 6 to provide supplemental refrigeration of the methane stream during the initial stages of the vre ⁇ frigeration.
  • a compressor 2S communicates with the llow passageway 8 of the smaller heat exchanger 2 and may be of any suitable type which can pressurize an initially liquid stream to a substantial pressure.
  • the gas stream to be liqueed (which will be described as methane) is conducted sequentially through the refrigeration flow passageways 22, 16, and 10 by suitable piping 30.
  • the refrigerant (which will be described as nitrogen) is conducted through the compressor 28 and llow passageways S, 14, and 20 by suitable piping 32.
  • the outlet of the flow passageway 20 of the largest heat exchanger 6 communicates with the inlet -of the flow passageway 12 of the central heat exchanger 4 through suitable piping 34.
  • a mechanical expansion device 36 is interposed in they conduit 34 to expand the refrigerant, as will be more fully hereinafter setforth.
  • the mechanical expansion device 36 is preferably a turboexpander in orderrthat useful power may be generated by the expansion of the refrigerant.
  • V(a) For methane-Transactions of The American Institute of Chemical Engineers, 42, 55 (1946).
  • I V(b) For nitrogen-US. Bureau of Mines Technical Paper 424.
  • methane frequently exists in a gaseous state at approximately atmospheric pressure and A90 F. prior to liquefaction thereof. Also, liquid nitrogen may be obtained at atmospheric pressure and approximately 320 F. Prior to the conduction of the methane into the larger heat exchanger 6, the methane is preferably compressed to a pressure above its critical pressure, such as 1,000 p.s.i.a., as indicated in the drawing. The methane will then exist in a uid state at approximately 90 F. and will have a heat content of approximately 388 B.t.u./lb.
  • the methane is conducted sequentially through the heat exchangers 6, 4, and 2 (in that order) to lower the temperature of the methane and reduce the heat content thereof, whereby the methane will be discharged from the flow passageway 10 of the heat exchanger 2 in a liquid state.
  • the pressure of the methane may be retained at 1,000 p.s.i.a. throughout its ow through the various heat exchangers and then expanded through a suitable throttling valve (not shown) for reduction to approximately atmospheric pressure. In that event, it will beunderstood that the methane discharging from the smaller heat exchanger 2 will exist in a uid state above its critical pressure, rather than in a liquid state.
  • the heat content of the methane at 1,000 p.s.i.a. (as it discharges from the heat exchanger 2) is substantially equal to the heat content of liquid methane at atmospheric pressure, the methane may be throttled to atmospheric pressure without any appreciable gas and refrigeration being produced. It will also be understood by those skilled in the art that Athe pressure of the methane may be reduced in steps between the successive heat exchangers to obtain a liquid methane discharging from the flow passageway 10 of the last heat exchanger 2, as long as such pressure drops do not upset the supply and demand balance between the exchanging streams.
  • the liquid nitrogen is pressurized by the compressor 28 to an elevated pressure, preferably above its critical pressure, such as 90 atmospheres.
  • the nitrogen will then have a temperature of approximately 315 F. and a heat content of approximately 10 B.t.u./1b. It will be noted that this pressurization takes Vplace prior to any heat exchange by the nitrogen.
  • kThepressurized nitrogen is then passed sequentially through the heat exchangers 2, 4, and'6 via the ow passageways 8, 14, and 20, respectively, Ato obtain a transfer of heat from the methane to the nitrogen in each of the heat exchangers. It will be observed from the various process 'conditions on the drawing that a temperature difference exists between the nitrogen and methane in each of the heat exchangers to'provide a transfer of heat from the methane to the nitrogen. When the nitrogen is discharged from the last heat exchanger 6, it will exist at approximately 80 F. and at a pressure approximating 90 atmospheres. Thus, the first passage of the nitrogen through the heat exchangers is made at substantially a constant elevated pressure.
  • the heated nitrogen is transferred through the conduit 34 tothe inlet of the turboexpander 36 at its elevated pressure.
  • the pressure of the nitrogen is reduced to approximately atmospheric, and the temperature of the nitrogen will be reduced to approximately 233 F.
  • the expansion of the nitrogen provides approximately 70 B.t.u./lb. of power which will be developed by the turboexpander and utilized as will be subsequently described.
  • the cooled nitrogen is then passed through the heat exchangers 4 and 6 via the flow passageways 12 and 18 to provide a further cooling of the methane.
  • the temperature of the cooled gaseous nitrogen in the ow passageways 12 and 18 will be substantially the same as the temperature of the compressed nitrogen passing through the passageways 14 and 20, respectively, toprevent a heat transfer between the passageways 12 and 14, and the passageways 18 and 20, respectively.
  • the nitrogen gas exhausting from the flow passageway 18 of the larger heat exchanger 6 v may be utilized in any desired manner.
  • the kind of refrigerant circulated through the tlow passageway 24 is immaterial, except that it must be colder than the methane to provide a transfer of heat from the flow passageway 22 ito the ow passageway 24. Also, the temperature of the additional refrigerant owing through the flow, passageway 24 should be equal to the temperature of the nitrogen passing through the passageways 18 and 20'to prevent a transfer of heat between the two types of refrigerants. It will be observed, however, that the vadditional refrigeration is obtained at a relative high temperature level, therefore the more common refrigerants may be used.
  • the 70 B.t.u./1b. of power obtainable from the turboexpander 36 may be conveniently used in the operation of the outside refrigeration source 26. Also, a portion of the power obtainable from the turboexpander 36 is preferably used in driving the nitrogen compressor 28. However, the power required for driving the compressor Y28 will be relatively small since the nitrogen is in liquid form at this pointin the process and very little work is required to compress or pressurize a liquid. Therefore, the major portion of the power obtainable from the .turboexpander 36 may be utilized withV the source of outside refrigeration 26, thereby requiringl limited additional power for' supplying the supplemental refrigeration through the How passageway 24. Y
  • the present process is primarily designed for a system wherein liquid methaneis produced .at one point and liquid nitrogen is producedat 'a distant point and it is desired tointerchange theY methane iwith ⁇ the nitrogen.
  • the methane can be liquefied by the use of nitrogenronly, ⁇ that is, without the use of outside refrigeration. However, approximately an additional one-half pound ofV nitrogen is required to liquefy each pound of methane.
  • Refrigerant Fluid being liquefied Hydrogen Nitrogen Air Methane Methane Ethylene Methane Propane Methane Butane Nitrogen Oxygen
  • the present invention increases the refrigeration which may be obtained by an initially liquid refrigerant.
  • the refrigerant By pressurizing the liquid refrigerant, the refrigerant may be passed in heat exchange relation with the stream being liquefied to obtain one series of heat transfers from the stream to the refrigerant.
  • the warmed refrigerant may then be expanded and cooled through a work-producing zone; whereupon the refrigerant may be passed in a second heat exchange with the stream to obtain an additional refrigeration of the stream.
  • the process is economical and may be simply performed by standard equipment.
  • the process is not limited to the use only when the mass rates of the stream and refrigerant are equal; however, when they are equal only a minor amount of outside power is required for supplemental refrigeration in order to liquefy the stream.
  • the present process provides mechanical power which may be used in producing the supplemental refrigeration.
  • the method of refrigerating a first fluid which comprises: (a) pressurizing a second liquid to above its critical pressure for presentation as a fiuid whose temperature at any point in the system is below the temperature of said first fiuid at the of said first fiuid in counterfiow heat exchange relation with said second iiuid stream, (c) maintaining substantially constant the pressure of said second fluid stream until its temperature has reached a level at which, when the stream has been expanded to a predetermined lower pressure with resulting drop in temperature, it will exist essentially in the gaseous phase at the lower temperature, (d) causing said second stream to expand to said predetermined pressure in a work-producing zone wherein its temperature is substantially reduced, (e) moving said thus cooled second stream now in the gaseous phase in counterow heat exchange relation with said rst fluid stream utilizing the work produced in said work producing zone to pressurize said second stream.
  • the method of refrigerating the first fluid which comprises: (a) moving a stream of said first fiuid in counterfiow heat exchange relation with (b) a pressurized initially liquid stream of a second fluid whose temperature at any point in the system is below the temperature of said first fiuid at the same point, (c) maintaining subsame point, (b) moving a stream stantially constant the pressure of said second fluid stream until its temperature has reached a level at which, when the stream has been'expanded to a predetermined lower pressure with resulting drop in temperature, it will exist essentially in the gaseous phase at the lower temperature (d) causing said pressurized second stream of fluid to expand to said predetermined pressure in a work producing zone wherein its temperature is substantially reduced, (e) moving said thus cooled second stream in counterflow heat exchange relation with said first stream, and then (f) using the energy derived in said work producing zone to additionally refrigerate said first stream.
  • each pass of the first stream of gas is passed in heat exchange relation with the streams of the second gas in a series of heat exchange steps for stepwise increase in the temperature of the stream of said second gas and stepwise decrease in temperature lof said stream of said first gas.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Chemical & Material Sciences (AREA)
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US531125A 1955-08-29 1955-08-29 Low temperature refrigeration Expired - Lifetime US2909906A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
LU37632D LU37632A1 (xx) 1955-08-29
US531125A US2909906A (en) 1955-08-29 1955-08-29 Low temperature refrigeration
GB29696/59A GB860723A (en) 1955-08-29 1959-08-31 Low temperature refrigeration
DEC19759A DE1126435B (de) 1955-08-29 1959-09-07 Verfahren zum Verfluessigen eines Gases

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Cited By (12)

* Cited by examiner, † Cited by third party
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
US3018634A (en) * 1958-04-11 1962-01-30 Phillips Petroleum Co Method and apparatus for vaporizing liquefied gases and obtaining power
US3018632A (en) * 1959-05-11 1962-01-30 Hydrocarbon Research Inc Cyclic process for transporting methane
US3034309A (en) * 1955-01-19 1962-05-15 Otto H Muck Method for transporting gas
DE1232174B (de) * 1960-06-16 1967-01-12 Conch Int Methane Ltd Verfahren zum Verdampfen von fluessigem Methan unter Verfluessigung von gasfoermigem Stickstoff aus einer Luftzerlegungssaeule
US4604115A (en) * 1984-03-23 1986-08-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for treating a storage site
US5060480A (en) * 1990-10-30 1991-10-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the liquefaction of a flow of gaseous oxygen
US5415001A (en) * 1994-03-25 1995-05-16 Gas Research Institute Liquefied natural gas transfer
US20040083756A1 (en) * 2002-11-01 2004-05-06 Jean-Pierre Tranier Combined air separation natural gas liquefaction plant
WO2008009930A2 (en) * 2006-07-18 2008-01-24 Ntnu Technology Transfer As Apparatus and methods for natural gas transportation and processing
US20090199590A1 (en) * 2004-09-24 2009-08-13 Linde Aktiengesellschaft Method and apparatus for compressing a natural gas stream
WO2022197526A3 (en) * 2021-03-15 2022-12-08 Air Water Gas Solutions, Inc. System and method for precooling in hydrogen or helium liquefaction processing

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL287922A (xx) * 1962-02-12
GB8505930D0 (en) * 1985-03-07 1985-04-11 Ncl Consulting Engineers Gas handling
DE4304673A1 (de) * 1993-01-05 1994-09-15 Rauscher Georg Verfahren zur Verflüssigung von Gasen, dadurch gekennzeichnet, daß flüssiges Gas bei hohem Druck verdampft, entspannt, verflüssigt, unterkühlt und im Wärmetauscher als Kühlmittel verwendet wird

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US655148A (en) * 1900-05-31 1900-07-31 Tripler Liquid Air Company System of cooling and ventilating.
US683010A (en) * 1900-11-08 1901-09-17 Gabriel A Bobrick System for utilizing liquid air or other gases for purposes of refrigeration and power.
FR736736A (fr) * 1931-09-07 1932-11-28 Procédé pour la production, le stockage et le transport des fluides liquéfiés ou solidifiés par le froid
US2458894A (en) * 1940-10-14 1949-01-11 Little Inc A Low-temperature refrigeration system
US2685181A (en) * 1952-04-30 1954-08-03 Emily C Schlitt Separation of the constituents of gaseous mixtures
US2685180A (en) * 1952-04-30 1954-08-03 Emily C Schlitt Gasifying an extraneous liquefied gas and simultaneously liquefying another gas

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE539478C (de) * 1929-05-14 1931-11-26 Richard Leiser Dr Verfahren zum Transport verfluessigter Gase bei tiefer Temperatur
DE1036884B (de) * 1954-10-28 1958-08-21 Johanna Muck Geb Roth Verfahren zur periodischen Entnahme und Speicherung von Tiefkaelte fuer die Verfluessigung bzw. Wiederverdampfung von Heizgasen, insbesondere von Erdgas

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US655148A (en) * 1900-05-31 1900-07-31 Tripler Liquid Air Company System of cooling and ventilating.
US683010A (en) * 1900-11-08 1901-09-17 Gabriel A Bobrick System for utilizing liquid air or other gases for purposes of refrigeration and power.
FR736736A (fr) * 1931-09-07 1932-11-28 Procédé pour la production, le stockage et le transport des fluides liquéfiés ou solidifiés par le froid
US2458894A (en) * 1940-10-14 1949-01-11 Little Inc A Low-temperature refrigeration system
US2685181A (en) * 1952-04-30 1954-08-03 Emily C Schlitt Separation of the constituents of gaseous mixtures
US2685180A (en) * 1952-04-30 1954-08-03 Emily C Schlitt Gasifying an extraneous liquefied gas and simultaneously liquefying another gas

Cited By (15)

* 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
US2975604A (en) * 1956-05-07 1961-03-21 Little Inc A Method of distribution of condensable gases
US3018634A (en) * 1958-04-11 1962-01-30 Phillips Petroleum Co Method and apparatus for vaporizing liquefied gases and obtaining power
US3018632A (en) * 1959-05-11 1962-01-30 Hydrocarbon Research Inc Cyclic process for transporting methane
DE1232174B (de) * 1960-06-16 1967-01-12 Conch Int Methane Ltd Verfahren zum Verdampfen von fluessigem Methan unter Verfluessigung von gasfoermigem Stickstoff aus einer Luftzerlegungssaeule
US4604115A (en) * 1984-03-23 1986-08-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for treating a storage site
US5060480A (en) * 1990-10-30 1991-10-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the liquefaction of a flow of gaseous oxygen
US5415001A (en) * 1994-03-25 1995-05-16 Gas Research Institute Liquefied natural gas transfer
US20040083756A1 (en) * 2002-11-01 2004-05-06 Jean-Pierre Tranier Combined air separation natural gas liquefaction plant
US7143606B2 (en) * 2002-11-01 2006-12-05 L'air Liquide-Societe Anonyme A'directoire Et Conseil De Surveillance Pour L'etide Et L'exploitation Des Procedes Georges Claude Combined air separation natural gas liquefaction plant
US20090199590A1 (en) * 2004-09-24 2009-08-13 Linde Aktiengesellschaft Method and apparatus for compressing a natural gas stream
WO2008009930A2 (en) * 2006-07-18 2008-01-24 Ntnu Technology Transfer As Apparatus and methods for natural gas transportation and processing
WO2008009930A3 (en) * 2006-07-18 2009-01-15 Ntnu Technology Transfer As Apparatus and methods for natural gas transportation and processing
US20100251763A1 (en) * 2006-07-18 2010-10-07 Ntnu Technology Transfer As Apparatus and Methods for Natural Gas Transportation and Processing
WO2022197526A3 (en) * 2021-03-15 2022-12-08 Air Water Gas Solutions, Inc. System and method for precooling in hydrogen or helium liquefaction processing

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LU37632A1 (xx)
DE1126435B (de) 1962-03-29

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