US3736762A - Method of producing the gaseous and liquefied nitrogen and an apparatus used therefor - Google Patents

Method of producing the gaseous and liquefied nitrogen and an apparatus used therefor Download PDF

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US3736762A
US3736762A US00082394A US3736762DA US3736762A US 3736762 A US3736762 A US 3736762A US 00082394 A US00082394 A US 00082394A US 3736762D A US3736762D A US 3736762DA US 3736762 A US3736762 A US 3736762A
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gas
air
nitrogen
passed
control valve
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US00082394A
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A Toyama
I Matsumoto
T Izumichi
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Kobe Steel Ltd
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Kobe Steel Ltd
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04242—Cold end purification of the feed air
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"

Definitions

  • ABSTRACT In a method of producing gaseous and liquefied nitrogen having a pressure higher than atmospheric pressure, by the use of an apparatus comprising a reversible heat exchanger and a single column rectifer, the combination of following steps: the impure gas obtained by heat-exchanging, in a condenser-evaporator, of liquefied air with nitrogen gas, each of which has been separated in the column, is divided into two parts; one of these parts is again divided into two parts; one part of this second division is passed through a control valve and then through the heat exchanger, after which it is united and admixed with the remaining part of the gas resulting from the second division, which has passed through a control valve; this admixture is supplied to an expansion tur' bine; the expanded impure gas is united and admixed with the remaining part of the gas resulting from the original division, which has passed through a control valve: and this admixture, after having been
  • the present invention offers a rationalized method of producing nitrogen of high pressure, entirely eliminating the drawbacks or disadvantages which have hitherto been encountered in practicing those systems of known devices.
  • One feature of this invention is that the reversible heat exchanger is used for the purpose of eliminating the impurities contained in the air supplied as raw material, such as carbon dioxide and moisture; and by adopting this reversible heat exchanger, compactness of the processing system and simplification of operating and maintenance procedures have been effectively accomplished.
  • Another noteworthy feature of this invention is a provision of such mechanism that the intermediate-pressure impure gas which has been heated up to some extent in the air-liquefier, after having left the condenser-evaporator which is attached to the single column rectifier, is introduced into the reversible heat exchanger, which gas operates as a low temperature fluid, an indispensable requisite for thorough elimination of CO, and other impurities which are drifting about the lower-temperature portion of the reversible heat exchanger; and therefrom, said impure gas is taken out of the middle portion of said reversible heat exchanger, and is made to mingle with the impure gas which has been divided at the discharge port of the air-liquefier; and further, said admixture of gases is subjected to the expansion turbine, where a certain amount of cold is generated for satisfying the functional need of the whole device.
  • Still another feature of this invention lies in the provision of three control valves.
  • the impure gas which has passed through the airliquefier, after having left the condenser-evaporator, is divided into two parts, one part of which is introduced into the reversible heat exchanger, and the other part of which is guided directly into the expansion turbine; and for both of those parts, control valves are provided respectively.
  • the impure gas can be satisfactorily adjusted to an optimal quantity of the gas, as best suited for thorough elimination of CO and other impurities staying around the lower-temperature portion of the reversible heat exchanger.
  • the accompanying drawing is a process-flow sheet which illustrates the functional phases of one preferred embodiment of the gaseous or liquefied nitrogen producing apparatus to be used for realizing the method of this invention.
  • the air coming through the suction pipe 1 first goes into the supplied-air compressor 2, where the air is compressed (in the case when the production of gaseous nitrogen alone is intended, the compression shall extend up to around 6 to 7 kg/cm', whereas in the case where it is intended to produce liquefied nitrogen concurrently with the gaseous nitrogen compression shall be up to around 8 to 9 kg/cm); and then, the compressed air is directed through the conduit tube 3, further going on to run through the higher-temperature portion '4 and the lower-temperature portion-5, of the reversible heat exchanger respectively.
  • the air is subjected to heat exchanging with the returning gas, then being cooled down to the proximity of liquefying point; and furtheron, passing through the check valve 6, conduit tube 7, and the gas-phase adsorber 39, the air finally enters into the bottom portion of the single column rectifier 8.
  • impurities contained in the air such as C0,, hydrocarbon and the like, are eliminated by way of adsorption; and inside of the single column rectifier, rectification is operated in accordance with the system of the generally known art.
  • the air is thereafter separated into two, i.e., the liquefied air which is abundant in oxygen and which is to be withdrawn from the bottom portion, and the high-purity nitrogen which is to be withdrawn from the top portion.
  • the single column rectifier 8 there is attached the air-liquefier 9.
  • the gaseous air which has been taken out through the conduit tube is subjected to heat-exchanging with the returning gas inside the air-liquefier 9, where the air is to be liquefied; and this liquefied gas is returned to the bottom portion of the single column rectifier 8, passing through the conduit tube 11.
  • the liquefied air sustains pressure reduction down to around 3 to 4 kg/cm, and finally enters the outer shell of the condenser-evaporator.
  • the liquefied air Upon coming into the condenser-evaporator 16, the liquefied air is placed under heat exchanging with the highly pure nitrogen gas which has been guided down there from the top portion of the single column rectifier 8, through the conduit tube 17; and the high-purity nitrogen gas is condensed into liquid form, and is made to pass through the conduit tube 18 to return to the top portion of the single column rectitier 8, thus after all becoming the reflux which is oriented toward the receifier.
  • the liquefied air is vaporized, and is withdrawn as the impure gas, from out of the conduit tube 19.
  • Part of the impure gas which has been taken out of the conduit tube 19 travels through the conduit tube 20 and the air-liquefier 9. After having run through the conduit tube 21 at the discharge port, part of the gas is again divided into two parts. A part of this second division goes on through the control valve 22 and the conduit tube 23, thus to be introduced, as into the lower-temperature portion 5 of the reversible heat exchanger, where said part of divided impure gas deservedly acts in compensating for the cold of sufficient amount to condense and eliminate the carbon dioxide which is contained in the supplied material air; meanwhile the impure gas itself sustains temperature rise, and is then taken out through the conduit tube 24; and thereafter going on through the inlet port control valve 25 of the expansion turbine, finally enters the expansion turbine 26.
  • the remaining part of the impure gas which has secondarily been divided as above described goes on through the control valve 27, and unites with part of the second division, and after passing through the control valve 25, enters the expansion turbine 26.
  • the impure gas which has thus entered the expansion turbine 26 is made to expand up to the proximity of atmospheric pressure; and through the thermodynamic external work which itself performs, the impure gas sustains a remarkable temperature drop, thereby generating the cold of such amount as is required for operational function of the entire device.
  • the impure gas still goes on through the conduit tubes 28 and 29, and again enters the air-liquefier 9, and further passes through the conduit tube 30 and the check valve 6, to enter the reversible heat exchangers 5 and 4; and after having entered there, the impure gas is subjected to heat exchanging with the supplied air, thereby being warmed to room temperature, and finally being discharged outside the apparatus, through the conduit tube 31.
  • This by-pass control valve 32 acts in such way that it co-operates with the control valves 22 and 27, just as described in the foregoing, in taking the role of regulating various factors such as the operating pressure of the condenserevaporator 16, and the flow rate of the expansion turbine 26 together with the cold-generating amount in said expansion turbine.
  • the opening of the by-pass control valve 32 by adjusting the opening of the by-pass control valve 32, the flow rate of the impure gas that travels through the conduit tube 20 towards the expansion turbine can be adjusted; and further, by the mutual interaction between the control valve 22 which is provided on the passage which guides the impure gas to the heat exchanger and the control valve 27 which is provided on the passage which guides said impure gas directly to the expansion turbine 26, the flow rate of the passage which is the heating passage for said impure gas and the rate of flow which is directly supplied to the expansion turbine are both to be controlled; and in turn, the inlet-port temperature of the expansion turbine 26 as well as the outlet temperature can be controlled; and at the same time, the cold generating quantity can be controlled.
  • the high-purity nitrogen gas product which has been separated at the top portion of the single column rectifier 8 travels through the conduit tube 33; and then, passing through the air-liquefier 9, the conduit tube 34, and the reversible heat exchangers 5 and 4, in succession, the nitrogen product is warmed to room temperature and is further sent out through from the conduit tube 35, then being at a pressure which is slightly lower than the given pressure of the supplied air.
  • the high-purity liquefied nitrogen product which has been separated at the top portion of the single column rectifier 8 is withdrawn outside after having passed through the conduit tube 36, the liquefled-nitrogen weighing tank 37, and the conduit tube 38, in succession.
  • the apparatus is operated at the level of given pressure of the supplied air, of the order of 6 to 7 kg/cm; whereas in such case that simultaneous production of both gaseous nitrogen and liquefied nitrogen is intended, the respective control valves are to work for regulation and adjustments just as described in the foregoing; and under that condition, the flow rate of the expansion turbine is to be raised to a required higher rate, as compared to the case of producing gaseous nitrogen only; and the pressure on the side of the impure gas inside the condenser-evaporator is also to be raised; and in turn, the operating pressure of the single column rectifier and the given pressure of the supplied air are both raised to an appreciably higher level (around 8 to 9 kg/cm), for securing the perfect operation of the apparatus.
  • the production of gaseous nitrogen only and the simultaneous production of both gaseous and liquefied nitrogen can be optionally and alternately achieved, through a simple operational manipulation; and the desired object of production can be effectively attained by using the simple and compact apparatus which embodies the producing method of this invention.
  • a method of producing gaseous and liquefied nitrogen having a pressure higher than atmospheric pressure which comprises cooling compressed air down to approximately its liquefying point by passing the compressed air through a reversible heat exchanger, introducing the air into a single column rectifier, where it is separated into liquefied air rich in oxygen and nitrogen, removing the gaseous air from the column, liquefying the gaseous air in an air-liquefier, returning the liquefied air into the column, withdrawing nitrogen gas from the top portion of the column, introducing at least a part of the withdrawn nitrogen gas into a condenserevaporator and liquefying it by means of heat-exchange with the liquefied air, which has been withdrawn from the bottom portion of the column and introduced into the outer shell of the condenser-evaporator, returning the liquefied nitrogen into the column, removing part of the liquefied nitrogen from the system, dividing impure gas obtained from the liquefied air as a result of said heat-exchange into two original parts
US00082394A 1969-10-20 1970-10-20 Method of producing the gaseous and liquefied nitrogen and an apparatus used therefor Expired - Lifetime US3736762A (en)

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DE (1) DE2051476C3 (de)
FR (1) FR2064440B1 (de)
GB (1) GB1325166A (de)
SU (1) SU417959A3 (de)

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4299607A (en) * 1979-05-16 1981-11-10 Hitachi, Ltd. Process for recovering nitrogen in low pressure type air separation apparatus
US4337070A (en) * 1979-05-30 1982-06-29 Linde Aktiengesellschaft Continuous system of rectification
US4400188A (en) * 1981-10-27 1983-08-23 Air Products And Chemicals, Inc. Nitrogen generator cycle
US4439220A (en) * 1982-12-02 1984-03-27 Union Carbide Corporation Dual column high pressure nitrogen process
US4453957A (en) * 1982-12-02 1984-06-12 Union Carbide Corporation Double column multiple condenser-reboiler high pressure nitrogen process
US4464188A (en) * 1983-09-27 1984-08-07 Air Products And Chemicals, Inc. Process and apparatus for the separation of air
US4560397A (en) * 1984-08-16 1985-12-24 Union Carbide Corporation Process to produce ultrahigh purity oxygen
US4662917A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Process for the separation of air
US4662916A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Process for the separation of air
US4662918A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Air separation process
US4783210A (en) * 1987-12-14 1988-11-08 Air Products And Chemicals, Inc. Air separation process with modified single distillation column nitrogen generator
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
US4872893A (en) * 1988-10-06 1989-10-10 Air Products And Chemicals, Inc. Process for the production of high pressure nitrogen
US4874413A (en) * 1987-01-16 1989-10-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for supplying nitrogen to an apparatus
US5074898A (en) * 1990-04-03 1991-12-24 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation method for the production of oxygen and medium pressure nitrogen
US5170630A (en) * 1991-06-24 1992-12-15 The Boc Group, Inc. Process and apparatus for producing nitrogen of ultra-high purity
US5309721A (en) * 1992-04-22 1994-05-10 The Boc Group Plc Air separation
US5462833A (en) * 1993-04-05 1995-10-31 Agfa-Gevaert, N.V. Lithographic base and a method for making a lithographic printing plate therewith
US5794458A (en) * 1997-01-30 1998-08-18 The Boc Group, Inc. Method and apparatus for producing gaseous oxygen
US6082136A (en) * 1993-11-12 2000-07-04 Daido Hoxan Inc. Oxygen gas manufacturing equipment
US20050233463A1 (en) * 2004-04-14 2005-10-20 Powertech Labs Inc. Method and device for the detection of SF6 decomposition products
US9726427B1 (en) 2010-05-19 2017-08-08 Cosmodyne, LLC Liquid nitrogen production
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2694383B1 (fr) * 1992-07-29 1994-09-16 Air Liquide Production et installation de production d'azote gazeux à plusieurs puretés différentes.
RU2522132C2 (ru) * 2012-07-10 2014-07-10 Ооо "Зиф" Способ разделения воздуха

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2627731A (en) * 1949-06-18 1953-02-10 Hydrocarbon Research Inc Rectification of gaseous mixtures
US3203193A (en) * 1963-02-06 1965-08-31 Petrocarbon Dev Ltd Production of nitrogen
US3217502A (en) * 1963-04-22 1965-11-16 Hydrocarbon Research Inc Liquefaction of air
US3312074A (en) * 1964-05-06 1967-04-04 Hydrocarbon Research Inc Air separation plant
US3319427A (en) * 1964-05-06 1967-05-16 Hydrocarbon Research Inc Air separation with a nitrogen refrigeration circuit
US3340697A (en) * 1964-05-06 1967-09-12 Hydrocarbon Research Inc Heat exchange of crude oxygen and expanded high pressure nitrogen
US3375673A (en) * 1966-06-22 1968-04-02 Hydrocarbon Research Inc Air separation process employing work expansion of high and low pressure nitrogen
US3546892A (en) * 1968-03-12 1970-12-15 Hydrocarbon Research Inc Cryogenic process

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2627731A (en) * 1949-06-18 1953-02-10 Hydrocarbon Research Inc Rectification of gaseous mixtures
US3203193A (en) * 1963-02-06 1965-08-31 Petrocarbon Dev Ltd Production of nitrogen
US3217502A (en) * 1963-04-22 1965-11-16 Hydrocarbon Research Inc Liquefaction of air
US3312074A (en) * 1964-05-06 1967-04-04 Hydrocarbon Research Inc Air separation plant
US3319427A (en) * 1964-05-06 1967-05-16 Hydrocarbon Research Inc Air separation with a nitrogen refrigeration circuit
US3340697A (en) * 1964-05-06 1967-09-12 Hydrocarbon Research Inc Heat exchange of crude oxygen and expanded high pressure nitrogen
US3375673A (en) * 1966-06-22 1968-04-02 Hydrocarbon Research Inc Air separation process employing work expansion of high and low pressure nitrogen
US3546892A (en) * 1968-03-12 1970-12-15 Hydrocarbon Research Inc Cryogenic process

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4299607A (en) * 1979-05-16 1981-11-10 Hitachi, Ltd. Process for recovering nitrogen in low pressure type air separation apparatus
US4337070A (en) * 1979-05-30 1982-06-29 Linde Aktiengesellschaft Continuous system of rectification
US4400188A (en) * 1981-10-27 1983-08-23 Air Products And Chemicals, Inc. Nitrogen generator cycle
US4439220A (en) * 1982-12-02 1984-03-27 Union Carbide Corporation Dual column high pressure nitrogen process
US4453957A (en) * 1982-12-02 1984-06-12 Union Carbide Corporation Double column multiple condenser-reboiler high pressure nitrogen process
US4464188A (en) * 1983-09-27 1984-08-07 Air Products And Chemicals, Inc. Process and apparatus for the separation of air
US4560397A (en) * 1984-08-16 1985-12-24 Union Carbide Corporation Process to produce ultrahigh purity oxygen
US4662917A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Process for the separation of air
US4662916A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Process for the separation of air
US4662918A (en) * 1986-05-30 1987-05-05 Air Products And Chemicals, Inc. Air separation process
US4874413A (en) * 1987-01-16 1989-10-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for supplying nitrogen to an apparatus
US4783210A (en) * 1987-12-14 1988-11-08 Air Products And Chemicals, Inc. Air separation process with modified single distillation column nitrogen generator
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
US4872893A (en) * 1988-10-06 1989-10-10 Air Products And Chemicals, Inc. Process for the production of high pressure nitrogen
US5074898A (en) * 1990-04-03 1991-12-24 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation method for the production of oxygen and medium pressure nitrogen
US5170630A (en) * 1991-06-24 1992-12-15 The Boc Group, Inc. Process and apparatus for producing nitrogen of ultra-high purity
US5309721A (en) * 1992-04-22 1994-05-10 The Boc Group Plc Air separation
US5462833A (en) * 1993-04-05 1995-10-31 Agfa-Gevaert, N.V. Lithographic base and a method for making a lithographic printing plate therewith
US6082136A (en) * 1993-11-12 2000-07-04 Daido Hoxan Inc. Oxygen gas manufacturing equipment
US5794458A (en) * 1997-01-30 1998-08-18 The Boc Group, Inc. Method and apparatus for producing gaseous oxygen
US20050233463A1 (en) * 2004-04-14 2005-10-20 Powertech Labs Inc. Method and device for the detection of SF6 decomposition products
US9726427B1 (en) 2010-05-19 2017-08-08 Cosmodyne, LLC Liquid nitrogen production
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

Also Published As

Publication number Publication date
DE2051476C3 (de) 1978-11-16
GB1325166A (en) 1973-08-01
DE2051476B2 (de) 1978-03-09
FR2064440B1 (de) 1973-11-23
FR2064440A1 (de) 1971-07-23
DE2051476A1 (de) 1971-04-29
SU417959A3 (de) 1974-02-28

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