US2760356A - Method of liquefying gases - Google Patents

Method of liquefying gases Download PDF

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Publication number
US2760356A
US2760356A US347513A US34751353A US2760356A US 2760356 A US2760356 A US 2760356A US 347513 A US347513 A US 347513A US 34751353 A US34751353 A US 34751353A US 2760356 A US2760356 A US 2760356A
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Prior art keywords
gas
cooler
stream
fraction
expanded
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US347513A
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English (en)
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Sixsmith Herbert
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National Research Development Corp UK
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National Research Development Corp UK
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02K—JET-PROPULSION PLANTS
    • F02K3/00—Plants including a gas turbine driving a compressor or a ducted fan
    • F02K3/08—Plants including a gas turbine driving a compressor or a ducted fan with supplementary heating of the working fluid; Control thereof
    • F02K3/10—Plants including a gas turbine driving a compressor or a ducted fan with supplementary heating of the working fluid; Control thereof by after-burners
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box

Definitions

  • the invention consists ofarranging for the net mass flow of compressed gas through the first stage heat exchanger or cooler to be substantially equalto the mass flow of expanded gas therethrough.
  • maximum efiiciency of heat exchange is obtainable, and the temperature difference between the incoming expanded gas and the efiluent compressed gas is Since, however, the flow of expanded gas is equal to the total available compressed gas less the fraction liquefied (neglecting any losses due to condensation of water vapour and sublimation of CO2), the above-mentioned balance of mass flow through the first stage cooler can; only be achieved if a proportion, equal to the fraction to be liquefied, is divided off from the total available compressed gas flow and either caused to by-passthe cooleror, having passed through the cooler with the; remainder, is recirculated therethrough in the reverse sense. In the latter case, the recirculating proportion isre-heated by the incoming gas, so that the net mass flow of compressed gas is substantially equal to the mass flow of expanded gas.
  • the by-passing proportion may actually constitute the fraction to be liquefied, being-supplied direct to the condenser; alternatively, the fraction tobe liquefied is split off after the first stage cooler, and the equivalent proportion which by-passes the cooler is re united with-the balance of the compressed gas after this splitting oil and before expansion.
  • the fraction to be liquefied is also split off from the cooled compressed gas, but after division therefrom of the recirculatory proportion, and this pro portion now re-heated, is reunited with the residual cold compressed eflluent from the cooler before expansion.
  • the gas to be liquefied is a permanent gas, for example air
  • the temperature at the cold end of the first stage cooler is suchthat the said constituents solidify in the cooler, and at least thecompress'ed' efiluent from the cooler is
  • the fraction to be liquefied, or an ec uivalent proportion thereto, by-pa'sse's the cooler it is preferable to 2,760,356 Eatent d u 1956.
  • the temperature of this cooled gas is in, certain cases" lower'than that at which maximum thermal efiiciency can be obtained from the expansion stage.
  • the; balancing of the mass flows is achieved by splitting oil? a proportion of the compressed gas equivalent to the fraction to be liquefied, this equivalent proportion being already at, or then raised to, substantially the initial temperature and recombined with the cooled residual part of the gas which isfto be expahded' as this latter part passes tov the expansion stage.
  • the effect of this splitting oh and recombination' of an equivalent proportion is to raise thetemperature of the. gas entering the expansion stage.
  • the methods of the invention are efiiciently operable at eoin'par'ativelylow pressures and the compressed gas may, forexample, be at a pressure of between 8 and 15, at rn'ospheres.
  • the heat exchanger used in the invention is preferably of the're'g'enerative type, in which a number of chambers or compartments; are successively opened to gas flow in appropriate directions by a' valve device moving relatively to the said chambers or'com'partinents (hereinafter called; chambers for convenience) or to ducts serving them.
  • At least one chamber is provided for the or each stream oi compressed gas which is to fiow through the. regen-v erator; and for the stream of expanded gas. It is desirable that the total regenerator volumes provided for the expanded and the compressed gas should be in inverse r'atio' to the respective gas" pressures. This would, however, involve providing an unduly large number of chambers, for the expanded gas.
  • the invention comprises a turbine adapted for use in the above-described methods, in which at least one main bearing. for the rotor shaft is mounted ouFa member which is freeto carry out-small ing component of force of the air jets. It is furthermore an advantage of this arrangement that the amplitudes of oscillation of the rotor at the critical speeds are greatly reduced.
  • the rotor shaft may be made long and slender, thus having a comparatively low heat conductivity.
  • the bearings can thus be'maintained at a temperature sufficiently high to enable them to be lubricated.
  • the turbine is preferably of the axial flow impulse type.
  • Figure 1 is a diagram illustrating the method of the invention.
  • FIG 4 shows, in diagrammatic form, an apparatus for carrying out the method of the invention as shown in Figure3;
  • Figure 5 is a part sectional, part elevational view of a part of the axial flow impulse turbine used in the apparatus of Figure 4.
  • an input stream of air A from a compressor and pre-cooler (at a pressure of, for example, 8 atmospheres) is divided into first and second fractions or streams a, b respectively, and the first fraction a is passed through a first heat exchange stage or cooler E1, from which it passes to an expansion turbine T provided with an air brake T1.
  • the expanded and cooled fraction After leaving the expansion turbine, the expanded and cooled fraction enters a condenser E2 from which it flows in reverse direction through the first stage cooler E1 and thenceto atmosphere. Since the expanded gas stream is wholly constituted by the compressed fraction 11 (neglecting'losses due to condensation of water or sublimation of CO2) the etfective'mass flows in opposite directions through the first stage cooler E1 are substantially equal.
  • the second fraction or stream b enters the condenser'Ez at atmospheric temperature.
  • the temperature of the first fraction a leaving the turbine may be approximately 80 absolute, a temperature low enough to cause liquefaction of the compressed second fraction b in the condenser E2.
  • the liquid is expanded in a valve V1 to atmospheric pressure and collected in a reservoir R from which it is tapped oif at intervals through a valve V2.
  • a pre-cooling and cleaning stage 3 in which it is cooled to atmospheric temperature.
  • the cooled compressed air passes by way of this valve, through the valve port P1, in to the regenerator chamber A1 in which it transfers its heat to the packing therein and is cooled nearly to the temperature of the expanded air stream leaving the condenser in the manner to 'be later described.
  • the stream of cooled compressed air now passes via the valve Vs, the manifold 4, and a restriction R1 to the expansion turbine 5 in which it is cooled by adiabatic expansion.
  • D and B respectively, an equivalent pro portion b and the fraction 0 to be liquefied leave the main stream and accordingly, between points B and C the stream constitutes the residual stream a referred to in the description of Figures 2 and 3.
  • the cold exhaust air from the turbine 5 passes through the pipe 6 to a condenser 7, in which it absorbs heat from the fraction 0 which reaches the condenser via pipe 8 and valve 9.
  • the expanded fraction flows via the valves V2 and V3 to the regenerator chambers Az and A2, and thence to atmosphere via the ports P2 and P3,
  • the fraction 0 is liquefied by heat exchange with the expanded fraction in the con denser 7..
  • the equivalent proportion b after leaving the main stream at D, flows through valve V15 into the regenerator chamber A5, through which it flows in reverse direction to the stream through the chamber A1.
  • the main part b1 flows through a valve VM and pipe 10 to join the stream a at C.
  • the rotary valve I slowly rotates so as,- for example, to bring the port P1 successively into line with theinlets' 0f the re'generator chambers A1 (as shown), A5, A4, As, An, A1 etc.
  • the infiowing air from the pre-cooler 3 is passed, for a predetermined interval of time, through the chamber A1, then for the same interval through the chamber A5, and so on until finally it is again'passed through the chamber A1.
  • regenerator chamber A4 is slowly filled with dry air provided by the stream b2. When the pressure in. A4
  • valve V14 drops 7 V13, V14 and V15 is provided with a cylindrical exten v sion 32 constituting a piston which is slightly smaller in diameter than the tube 33 in which it is free to move;
  • the annular space between the tube and the piston constitutes a restriction, and the pressure drop across the restriction tends to raise the piston, thus closing the valve.
  • the value of the restriction is such that the valve remains open against the by-passing stream b, but closes when the flow slightly exceeds this value, as will happen in the caseof V14 when the port P2 reaches A4 and air from the manifold 4 rushes out to the atmosphere via V14, A4 and P2.
  • Condensed liquid and a slight excess of gas are continually and automatically drawn off from the condenser 7 by means of an automatic expansion valve 12 which is adjusted to give an output pressure slightly above atmospheric pressure, so that the flow rate can be con- After leaving trolled by means of an orifice 12a of normal dimensions.
  • the liquid air is delivered to an automatic float trap 13 of conventional design, which discharges at intervals into a suitable receptacle. Excess air escaping with the liquid is returned to the turbine exhaust pipe 6 by way of a pipe 14.
  • turbine is an axial flow impulse turbine, the rotor, stator, shafting and one bearing of which are shown in Figure 5.
  • a shaft 15 upon which is mounted the rotor 16 also carries a centrifugal blower 17 which acts as the brake 18 shown in Figure 4.
  • the blower is shown as a schematic block in Figure 5, since its design forms no part of the present invention. It may have the form of a drum having radial holes for air flow. High pressure air is fed via the inlet 19 to the stator blades 20 having a shroud ring 21 shrunk thereon to avoid tip leakage.
  • a turbine according to the invention has been constructed, in which the turbine rotor is machined from a solid piece of brass and having a tip diameter of about the rotor blades being about A long and having a chord width of A".
  • the shroud ring is of brass and the rotor is mounted on the shaft 15 which is of silver steel having a diameter of This shaft is about 4" long and is mounted in cup bearings at each end.
  • the shaft 15 is machined conically at its end which seats in balls 22 located in the cup 23; the stalk 24 of the cup being hollow to allow for the passage of oil to the bearing.
  • a stem 27 integral with the cup 26 passes through an externally threaded sleeve 28 as shown, which sleeve is adapted to pass through a hole in the outer case (not shown) and to have a nut screwed thereon to support the shaft and bearing assembly within the casing.
  • the stem 27 is hollow, its bore communicating with the bore through the hollow stalk 24 for the supply of oil thereto.
  • a small clearance is allowed between the cup 26 and the internal wall of the sleeve 28.
  • the hearing as a whole is capable of radial displacement, which is damped by means of two oil-filled dashpot mechanisms of which only one (29) is shown in the drawing and which are mutually at right angles.
  • These dashpots are of conventional design, and the pistonrods 30 are connected to the cup 26 through a close-fitting ring 31.
  • the bearing at the other end of the shaft 15 may be similarly constructed or, alternatively, may be similar except that no allowance is made for radial displacement.
  • the cup 26 may be replaced by a sliding collar to which are attached the piston rods of three-dashpots at 120 to each other.
  • the piston rods are secured to the stem 27 instead of being attached to the cup 26.
  • regenerator chambers A1 to A are to be of the small size necessary to keep the bulk of the machine as small as possible, they require a packing material which is eflicient and simple to construct and has a high conductivity in the direction transverse to the direction of flow therethrough. A low thermal conductivity in the direction of the flow is desirable.
  • a packing consisting of discs of fine wire gauze, which discs are separated by discs of thermally insulating material such as cloth of open weave, for example, rayon net.
  • the method of liquefying a gas comprising compressing the gas, dividing the compressed gas into two parts, a major part and a minor part, passing at least the major part through a first stage cooler to cool it, dividing the major part, after such cooling into two parts, a small part and a large part, after such division passing the small part through a condenser to liquefy it and after such division combining the large part with the minor part which is uncooled, expanding the combined parts adiabatically accompanied by the expenditure of energy to reduce their temperature, and passing the expanded combined parts first through the condenser in counterfiow with respect to the small part liquefied therein and secondly through the first stage cooler in counterfiow with respect to the compressed gas flowing through it, the mass flow per unit time of compressed gas flowing in one direction through the first stage cooler being substantially equal to the mass flow per unit time of gases passing through the first stage cooler in the other direction.
US347513A 1952-04-22 1953-04-08 Method of liquefying gases Expired - Lifetime US2760356A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB339635X 1952-04-22
GB90453X 1953-04-09

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US (1) US2760356A (de)
BE (1) BE519364A (de)
CH (1) CH339635A (de)
DE (1) DE928954C (de)
FR (1) FR1076409A (de)
GB (1) GB727904A (de)

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2929548A (en) * 1956-06-29 1960-03-22 Cooper Bessemer Corp Turbocompressor
US2959020A (en) * 1958-01-29 1960-11-08 Conch Internat Mcthane Ltd Process for the liquefaction and reliquefaction of natural gas
US3021683A (en) * 1959-01-23 1962-02-20 Hymatic Eng Co Ltd Gas liquefiers
US3066492A (en) * 1959-05-15 1962-12-04 Air Liquide Process for the liquefaction of a gas
US3075362A (en) * 1957-09-25 1963-01-29 Linde Eismasch Ag Process for separating so2 and constituents of a similar dew point from gases by means of regenerators
US3116135A (en) * 1960-04-18 1963-12-31 Conch Int Methane Ltd Gas liquefaction process
US3161232A (en) * 1961-08-14 1964-12-15 Hydrocarbon Research Inc Refrigeration-heating circuit
US3180709A (en) * 1961-06-29 1965-04-27 Union Carbide Corp Process for liquefaction of lowboiling gases
US3182461A (en) * 1961-09-19 1965-05-11 Hydrocarbon Research Inc Natural gas liquefaction and separation
US3203191A (en) * 1960-09-02 1965-08-31 Conch Int Methane Ltd Energy derived from expansion of liquefied gas
US3205679A (en) * 1961-06-27 1965-09-14 Air Prod & Chem Low temperature refrigeration system having filter and absorber means
US3213631A (en) * 1961-09-22 1965-10-26 Lummus Co Separated from a gas mixture on a refrigeration medium
US3241327A (en) * 1963-12-18 1966-03-22 Fleur Corp Waste heat recovery in air fractionation
US3250079A (en) * 1965-03-15 1966-05-10 Little Inc A Cryogenic liquefying-refrigerating method and apparatus
US3302865A (en) * 1964-07-16 1967-02-07 Union Carbide Corp Gas-bearing assembly
US3768254A (en) * 1962-07-09 1973-10-30 Boeing Co Rocket propulsion method and means
US4040266A (en) * 1975-08-23 1977-08-09 Linde Aktiengesellschaft Multistage cooling of crude hydrocarbon gases
US6920759B2 (en) 1996-12-24 2005-07-26 Hitachi, Ltd. Cold heat reused air liquefaction/vaporization and storage gas turbine electric power system
US20090293503A1 (en) * 2008-05-27 2009-12-03 Expansion Energy, Llc System and method for liquid air production, power storage and power release
US20090293502A1 (en) * 2008-05-27 2009-12-03 Expansion Energy, Llc System and method for liquid air production power storage and power release
US20110030332A1 (en) * 2008-05-27 2011-02-10 Expansion Energy, Llc System and method for liquid air production, power storage and power release
US8907524B2 (en) 2013-05-09 2014-12-09 Expansion Energy Llc Systems and methods of semi-centralized power storage and power production for multi-directional smart grid and other applications

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1135934B (de) * 1957-09-05 1962-09-06 Nat Res Dev Regenerativer Waermeaustauscher zwischen einer Hochdruckgas erzeugenden Anlage und einer Vorrichtung zur Entspannung und Abkuehlung dieses Gases
DE1235345B (de) * 1961-09-19 1967-03-02 Philips Nv Speicherwaermetauscher mit einer Fuellmasse, die abwechselnd in einer Richtung von zu kuehlendem und in der anderen Richtung von zu erwaermendem Medium durchflossen ist

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1027863A (en) * 1911-10-23 1912-05-28 Carl Von Linde Apparatus for the separation of hydrogen.
GB191501086A (en) * 1914-01-31 1916-01-24 George Francois Jaubert Improvements in or relating to the Liquefaction of Gases.
US1264845A (en) * 1915-03-03 1918-04-30 Jefferies Morton Corp Process of refrigeraiton.
US1901389A (en) * 1928-10-18 1933-03-14 Hazard-Flamand Maurice Process for liquefying and rectifying air
US2165994A (en) * 1933-03-24 1939-07-11 Linde Eismasch Ag Turbine for low temperature gas separation
US2529880A (en) * 1949-03-15 1950-11-14 Elliott Co Turboexpander

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1027863A (en) * 1911-10-23 1912-05-28 Carl Von Linde Apparatus for the separation of hydrogen.
GB191501086A (en) * 1914-01-31 1916-01-24 George Francois Jaubert Improvements in or relating to the Liquefaction of Gases.
US1264845A (en) * 1915-03-03 1918-04-30 Jefferies Morton Corp Process of refrigeraiton.
US1901389A (en) * 1928-10-18 1933-03-14 Hazard-Flamand Maurice Process for liquefying and rectifying air
US2165994A (en) * 1933-03-24 1939-07-11 Linde Eismasch Ag Turbine for low temperature gas separation
US2529880A (en) * 1949-03-15 1950-11-14 Elliott Co Turboexpander

Cited By (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2929548A (en) * 1956-06-29 1960-03-22 Cooper Bessemer Corp Turbocompressor
US3075362A (en) * 1957-09-25 1963-01-29 Linde Eismasch Ag Process for separating so2 and constituents of a similar dew point from gases by means of regenerators
US2959020A (en) * 1958-01-29 1960-11-08 Conch Internat Mcthane Ltd Process for the liquefaction and reliquefaction of natural gas
US3021683A (en) * 1959-01-23 1962-02-20 Hymatic Eng Co Ltd Gas liquefiers
US3066492A (en) * 1959-05-15 1962-12-04 Air Liquide Process for the liquefaction of a gas
US3116135A (en) * 1960-04-18 1963-12-31 Conch Int Methane Ltd Gas liquefaction process
US3203191A (en) * 1960-09-02 1965-08-31 Conch Int Methane Ltd Energy derived from expansion of liquefied gas
US3205679A (en) * 1961-06-27 1965-09-14 Air Prod & Chem Low temperature refrigeration system having filter and absorber means
US3180709A (en) * 1961-06-29 1965-04-27 Union Carbide Corp Process for liquefaction of lowboiling gases
US3161232A (en) * 1961-08-14 1964-12-15 Hydrocarbon Research Inc Refrigeration-heating circuit
US3182461A (en) * 1961-09-19 1965-05-11 Hydrocarbon Research Inc Natural gas liquefaction and separation
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Also Published As

Publication number Publication date
FR1076409A (de) 1954-10-26
BE519364A (de)
CH339635A (fr) 1959-07-15
DE928954C (de) 1955-06-16
GB727904A (en) 1955-04-13

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