US3729943A - Process for separation of ternary gaseous mixtures by rectification - Google Patents

Process for separation of ternary gaseous mixtures by rectification Download PDF

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Publication number
US3729943A
US3729943A US00032613A US3729943DA US3729943A US 3729943 A US3729943 A US 3729943A US 00032613 A US00032613 A US 00032613A US 3729943D A US3729943D A US 3729943DA US 3729943 A US3729943 A US 3729943A
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rectification
zone
auxiliary
liquid
withdrawn
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US00032613A
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English (en)
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P Petit
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GEORGES CLAUDE FR
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • 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
    • F25J3/04406—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 dual pressure main column system
    • F25J3/04412—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 dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04684—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser and a bottom re-boiler
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

Definitions

  • the present invention concerns a process in which a PP 32,613 gaseous fraction is withdrawn from an intermediate level of a main rectification and subjected to a rectifi- [30] Foreign Application Priority Data cation in an auxiliary zone, the liquid fraction obtained in this auxiliary zone being; returned to the said May 5, 1969 France ..69l4244 intermediate level of the main reclificatior 52 us. 01 ..62/22 62/29
  • the improvement acwrding concerns Int.
  • the process is applicable to the separation by rectification of a mixture formed U E STATES PATENTS of at least three constituents, two of which are in major proportions, the boiling point of the constituent 2,700,282 1/1955 Roberts ..62/22 i small proportions being between the boiling points of the two constituents in major proportions and being 344733] 6/1969 "62/39 closer to that of the less volatile of these two conlssogsl 10/1932 g ⁇ "62/3! stituents.
  • the invention is applicable to a 2 559 132 7 1951 Roberts.::.
  • the present invention relates to an improved process by which a mixture composed of at least three constituents is separated by rectification.
  • the present invention is more specifically concerned with a process which makes possible an increase in the extraction yield of a constituent which is in small proportions in a mixture of at least three constituents, of which two are in major proportions, the boiling point of this constituent present in small proportions being between the boiling pointsof the two constituents in major proportions and being closer to that of the less volatile of these two constituents.
  • the present invention is particularly applicable to the separation of air by rectification and has for its object a process permitting the rate of extraction of argon to be increased.
  • the present invention is also concerned with any installation for carrying the above processes into effect.
  • the amount blown in is generally between 5 and percent by volume, relatively to the volume of supply air. If the amount blown in is too high, however, this causes firstly an appreciable decrease in yield of oxygen in the separating operation and secondly an almost total impossibility of separating the argon.
  • the present invention consists in an improvement in existing processes and installations, which permits the aforesaid inconveniences to be obviated and the cost price and also the energy consumption to be reduced to the greatest possible degree.
  • the improvement forming the subject of the present invention makes possible an improvement in the extraction yield of a constituent which is in small proportions in a mixture; it is possible to operate without any special installation being required.
  • the present invention has for its object an improved separation process by rectification, making possible an increase in the extraction yield of a constituent which is in small proportions in a mixture of at least three constituents, two of which are in major proportions, the boiling point of this constituent in small proportions being between the boiling points of the two constituents in major proportions and being closer to that of the less volatile of these two constituents, in which a gaseous fraction is withdrawn from an intermediate level of a main rectification and subjected to a rectification in an auxiliary zone, the liquid fraction obtained in this auxiliary zone being returned to the said intermediate level of the main rectification, and in which the condensation of the said withdrawn gaseous fraction is effected at the bottom and simultaneously at the top of the said auxiliary zone by the vaporization of liquid fractions originating from themainrectification.
  • the said withdrawn gaseous fraction is at least partly condensed at the bottom of the said auxiliary zone by the vaporization of at least a part of the liquid fraction collected at the bottom of the second zone of the said main rectification.
  • the said withdrawn gaseous fraction is at least partly condensed at the bottom of the said auxiliary zone bythe vaporization of at least apart of the liquid fraction collected at the top of the first zone of the said main rectification.
  • the withdrawn gaseous fraction is at least partly condensed at the top of the said auxiliary zone by the vaporization of at least a part of the liquid fraction collected at the top of the first zone of the said main rectification.
  • the said withdrawn gaseous fraction is at least partly condensed at the top of the said auxiliary zone by the vaporization of at least a part of the liquid fraction collected at the top of the first zone of the said main rectification, and simultaneously by the vaporization of at least a part of the liquid fraction collected at the bottom of the first zone of the said rectification.
  • the concentration in the withdrawn gaseous fraction of the said constituent in small proportions, relatively to the least volatile constituent is the highest possible, and the concentration of the most volatile constituent is the lowest possible.
  • the liquid fractions originating from the said zones of the main rectification are, after at least partial vaporization in the auxiliary rectification zone, preferably returned into the second zone of the said main rectification.
  • At least one of the liquid fractions originating from the said zones of the main rectification is, after at least partial vaporization in the auxiliary rectification zone, preferably expanded in a turbine so as to assure a supply of cold to the installation.
  • the said mixture of at least three constituents is air, from which it is desired to extract the argon (which is found therein in small proportions), of which the boiling point is between that of the nitrogen and that of the oxygen and is closer to that of oxygen, which is the least volatile.
  • the present invention is also concerned with any installation for carrying out the process according to the present invention.
  • FIGS. 1 and 2 represent different embodiments of the present invention. For the purpose of simplification the similar parts of these figures bear the same references.
  • FIG. 1 represents an embodiment in which the low pressure oxygen is at least partly vaporized at the bottom of the auxiliary column and the liquid with high oxygen content from the medium pressure column is possibly partly vaporized at the top of the auxiliary column.
  • FIG. 2 shows an embodiment in which the medium pressure liquid nitrogen is at least partly vaporized at the bottom of the auxiliary column.
  • the auxiliary rectifier column 4 comprises a condenser 6 at the top and a condenser 7 at the bottom.
  • the liquid oxygen is drawn off from the double rectifier column through the pipe 14 and the gaseous nitrogen is drawn off through the pipe 10.
  • a gaseous fraction is withdrawn through the pipe 8; this fraction is supplied to the auxiliary rectifier column 4, in which the oxygen which it contains is condensed, and then the fraction thus condensed is returned through the pipe 9 to the low pressure zone.
  • the level at which the withdrawal takes place is a function of the operating conditions: pressure, nature of the constituents of the mixture, etc.
  • the withdrawal takes place at the level where the argon concentration is the highest possible and the nitrogen concentration is the lowest possible.
  • the withdrawal is generally effected at the level of the 15th plate.
  • a much larger proportion of the argon in the air is withdrawn through the pipe 1 1 than is the case with the known processes. Instead of recovering percent of the argon present in the air, as is generally the case in the known processes, it is found, for example, in the case of FIG. 1, that more than 78 percent of the argon present in the air are recovered. A much better separation between oxygen and nitrogen is also obtained.
  • the liquid fraction rich in oxygen and leaving the column 1 through the pipe 12 is introduced by way of the pipe 112 into the condenser 6, in which at least a fraction of the fraction rich in oxygen is vaporized, whereafter this fraction rich in oxygen is conveyed through the pipe 212 into the low pressure column 2.
  • Another part of the cold supply necessary for the rectification is obtained in the condenser 7 by vaporizing a part of the liquid oxygen fraction collected in the column 2.
  • the fraction rich in oxygen and leaving the column 1 by way of the pipe 12 is brought directly into the column 2, another part being supplied through the pipe 1 12 to the condenser 6, in which it is at least partly vaporized, and then by way of the pipe 212 to the column 2.
  • a part of the fraction rich in nitrogen, which is obtained in the column 1, is conducted through a pipe 113 into the condenser 7, which it leaves, ac least partly vaporized, by way of the pipe 213.
  • What I claim is 1.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US00032613A 1969-05-05 1970-04-28 Process for separation of ternary gaseous mixtures by rectification Expired - Lifetime US3729943A (en)

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FR6914244A FR2041701B1 (fr) 1969-05-05 1969-05-05

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US (1) US3729943A (fr)
JP (1) JPS5617584B1 (fr)
BE (1) BE749882A (fr)
DE (1) DE2021140B2 (fr)
ES (1) ES379208A1 (fr)
FR (1) FR2041701B1 (fr)
GB (1) GB1315003A (fr)
LU (1) LU60844A1 (fr)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4433990A (en) 1981-12-08 1984-02-28 Union Carbide Corporation Process to recover argon from oxygen-only air separation plant
WO1986006462A1 (fr) * 1985-04-29 1986-11-06 Erickson Donald C Recuperation amelioree d'argon lors de la distillation d'air
US4715874A (en) * 1986-09-08 1987-12-29 Erickson Donald C Retrofittable argon recovery improvement to air separation
US4775399A (en) * 1987-11-17 1988-10-04 Erickson Donald C Air fractionation improvements for nitrogen production
US4783208A (en) * 1986-11-24 1988-11-08 The Boc Group Plc Air separation
US4790866A (en) * 1986-11-24 1988-12-13 The Boc Group Plc Air separation
US4836836A (en) * 1987-12-14 1989-06-06 Air Products And Chemicals, Inc. Separating argon/oxygen mixtures using a structured packing
US4838785A (en) * 1988-07-05 1989-06-13 Cameron Forge Company Walking beam furnace insulation
US4838913A (en) * 1988-02-10 1989-06-13 Union Carbide Corporation Double column air separation process with hybrid upper column
US4842625A (en) * 1988-04-29 1989-06-27 Air Products And Chemicals, Inc. Control method to maximize argon recovery from cryogenic air separation units
US4871382A (en) * 1987-12-14 1989-10-03 Air Products And Chemicals, Inc. Air separation process using packed columns for oxygen and argon recovery
US4883516A (en) * 1987-04-07 1989-11-28 The Boc Group, Inc. Air separation
US4994098A (en) * 1990-02-02 1991-02-19 Air Products And Chemicals, Inc. Production of oxygen-lean argon from air
US5034043A (en) * 1989-02-23 1991-07-23 Linde Aktiengesellschaft Air separation with argon recovery
US5078766A (en) * 1989-07-28 1992-01-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Equipment for air distillation to produce argon
USRE34038E (en) * 1987-12-14 1992-08-25 Air Products And Chemicals, Inc. Separating argon/oxygen mixtures using a structured packing
US5799508A (en) * 1996-03-21 1998-09-01 Praxair Technology, Inc. Cryogenic air separation system with split kettle liquid
EP1271080A1 (fr) * 2001-06-18 2003-01-02 Air Products And Chemicals, Inc. Production d'azote à moyenne pression et à haut rendement d'extraction d'oxygène
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3983711A (en) * 1975-01-02 1976-10-05 The Lummus Company Plural stage distillation of a natural gas stream

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1880981A (en) * 1930-02-07 1932-10-04 Pollitzer Franz Separation of oxygen, nitrogen, and argon from air
US2559132A (en) * 1948-02-12 1951-07-03 British Oxygen Co Ltd Fractional separation of air
US2699046A (en) * 1947-10-22 1955-01-11 Air Liquide Process for separating fluid mixtures into fractions of different volatilities
US2700282A (en) * 1948-02-12 1955-01-25 British Oxygen Co Ltd Fractional separation of air
GB874001A (en) * 1958-05-20 1961-08-02 Union Carbide Corp Process of and apparatus for low-temperature separation of air
US3079759A (en) * 1961-03-22 1963-03-05 Air Prod & Chem Separation of gaseous mixtures
US3110155A (en) * 1960-04-11 1963-11-12 British Oxygen Co Ltd Improved process for the separation of air to produce a desired separation product in the gaseous phase under pressure
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US3214925A (en) * 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
US3416323A (en) * 1966-01-13 1968-12-17 Linde Ag Low temperature production of highly compressed gaseous and/or liquid oxygen
US3447331A (en) * 1966-06-01 1969-06-03 British Oxygen Co Ltd Air separation employing waste nitrogen reheated by incoming air in work expansion

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US1880981A (en) * 1930-02-07 1932-10-04 Pollitzer Franz Separation of oxygen, nitrogen, and argon from air
US2699046A (en) * 1947-10-22 1955-01-11 Air Liquide Process for separating fluid mixtures into fractions of different volatilities
US2559132A (en) * 1948-02-12 1951-07-03 British Oxygen Co Ltd Fractional separation of air
US2700282A (en) * 1948-02-12 1955-01-25 British Oxygen Co Ltd Fractional separation of air
GB874001A (en) * 1958-05-20 1961-08-02 Union Carbide Corp Process of and apparatus for low-temperature separation of air
US3110155A (en) * 1960-04-11 1963-11-12 British Oxygen Co Ltd Improved process for the separation of air to produce a desired separation product in the gaseous phase under pressure
US3214925A (en) * 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
US3079759A (en) * 1961-03-22 1963-03-05 Air Prod & Chem Separation of gaseous mixtures
US3416323A (en) * 1966-01-13 1968-12-17 Linde Ag Low temperature production of highly compressed gaseous and/or liquid oxygen
US3447331A (en) * 1966-06-01 1969-06-03 British Oxygen Co Ltd Air separation employing waste nitrogen reheated by incoming air in work expansion

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4433990A (en) 1981-12-08 1984-02-28 Union Carbide Corporation Process to recover argon from oxygen-only air separation plant
WO1986006462A1 (fr) * 1985-04-29 1986-11-06 Erickson Donald C Recuperation amelioree d'argon lors de la distillation d'air
US4670031A (en) * 1985-04-29 1987-06-02 Erickson Donald C Increased argon recovery from air distillation
US4715874A (en) * 1986-09-08 1987-12-29 Erickson Donald C Retrofittable argon recovery improvement to air separation
US4783208A (en) * 1986-11-24 1988-11-08 The Boc Group Plc Air separation
US4790866A (en) * 1986-11-24 1988-12-13 The Boc Group Plc Air separation
US4883516A (en) * 1987-04-07 1989-11-28 The Boc Group, Inc. Air separation
US4775399A (en) * 1987-11-17 1988-10-04 Erickson Donald C Air fractionation improvements for nitrogen production
WO1989004942A1 (fr) * 1987-11-17 1989-06-01 Erickson Donald C Fractionnement d'air ameliore a des fins de production d'azote
US4871382A (en) * 1987-12-14 1989-10-03 Air Products And Chemicals, Inc. Air separation process using packed columns for oxygen and argon recovery
US4836836A (en) * 1987-12-14 1989-06-06 Air Products And Chemicals, Inc. Separating argon/oxygen mixtures using a structured packing
USRE34038E (en) * 1987-12-14 1992-08-25 Air Products And Chemicals, Inc. Separating argon/oxygen mixtures using a structured packing
US4838913A (en) * 1988-02-10 1989-06-13 Union Carbide Corporation Double column air separation process with hybrid upper column
US4842625A (en) * 1988-04-29 1989-06-27 Air Products And Chemicals, Inc. Control method to maximize argon recovery from cryogenic air separation units
EP0341854B1 (fr) * 1988-04-29 1992-11-25 Air Products And Chemicals, Inc. Procédé de séparation d'air en utilisant des colonnes garnies pour la récupération de l'oxygène et de l'argon
US4838785A (en) * 1988-07-05 1989-06-13 Cameron Forge Company Walking beam furnace insulation
US5034043A (en) * 1989-02-23 1991-07-23 Linde Aktiengesellschaft Air separation with argon recovery
US5078766A (en) * 1989-07-28 1992-01-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Equipment for air distillation to produce argon
US4994098A (en) * 1990-02-02 1991-02-19 Air Products And Chemicals, Inc. Production of oxygen-lean argon from air
US5799508A (en) * 1996-03-21 1998-09-01 Praxair Technology, Inc. Cryogenic air separation system with split kettle liquid
EP1271080A1 (fr) * 2001-06-18 2003-01-02 Air Products And Chemicals, Inc. Production d'azote à moyenne pression et à haut rendement d'extraction d'oxygène
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

Also Published As

Publication number Publication date
FR2041701A1 (fr) 1971-02-05
FR2041701B1 (fr) 1974-02-01
ES379208A1 (es) 1973-02-01
GB1315003A (en) 1973-04-26
LU60844A1 (fr) 1970-07-07
DE2021140B2 (de) 1980-03-20
JPS5617584B1 (fr) 1981-04-23
DE2021140A1 (de) 1970-11-19
BE749882A (fr) 1970-11-04

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