EP0019905B1 - Dispositif pour la séparation d'un mélange de gaz par rectification - Google Patents

Dispositif pour la séparation d'un mélange de gaz par rectification Download PDF

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Publication number
EP0019905B1
EP0019905B1 EP80102953A EP80102953A EP0019905B1 EP 0019905 B1 EP0019905 B1 EP 0019905B1 EP 80102953 A EP80102953 A EP 80102953A EP 80102953 A EP80102953 A EP 80102953A EP 0019905 B1 EP0019905 B1 EP 0019905B1
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EP
European Patent Office
Prior art keywords
liquid
sump
evaporator
condenser
adsorber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP80102953A
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German (de)
English (en)
Other versions
EP0019905A1 (fr
Inventor
Wilhelm Rohde
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
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Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to AT80102953T priority Critical patent/ATE2178T1/de
Publication of EP0019905A1 publication Critical patent/EP0019905A1/fr
Application granted granted Critical
Publication of EP0019905B1 publication Critical patent/EP0019905B1/fr
Expired legal-status Critical Current

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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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • Y10S62/902—Apparatus
    • Y10S62/903—Heat exchange structure
    • 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
    • Y10S62/902—Apparatus
    • Y10S62/908—Filter or absorber

Definitions

  • the invention relates to a device for the separation of a gas mixture by rectification with a rectification column, an adsorber which is connected on the one hand to the bottom liquid in the rectification column and on the other hand to a condenser-evaporator which is connected to the vapor space above the bottom liquid.
  • Such a device is known from DE-B-1 143 526.
  • a gas separation plant with a rectification column is described, in the sump of which a condenser-evaporator is arranged.
  • the column sump is connected to an adsorber in which undesirable constituents from the rectifying liquid are removed from the column sump.
  • Higher-boiling components such as hydrocarbons, which freeze out on the evaporator walls and can block flow cross sections, are regarded as undesirable constituents.
  • Egungsanlagen at Gutze d is also at a high acetylene concentration in the oxygen-rich rectifier liquid explosion.
  • the downstream end of the adsorber is connected to an outer condenser-evaporator, in which the cleaned rectification liquid is partially evaporated.
  • the upper end of the outer condenser-evaporator is connected to the rectification column by a connecting line. The rising steam creates a flow with which the rectifying liquid is circulated through the adsorber.
  • the present invention is therefore based on the object of developing a device of the type mentioned at the outset in which freezing out of higher-boiling constituents of the rectifying liquid in the condenser-evaporator is largely prevented.
  • the upper end of the condenser-evaporator is open, so that the non-evaporated portions of the rectifying liquid, which are carried upwards with the rising steam, can pass freely over the edge of the condenser-evaporator and can flow into the surrounding bottom liquid.
  • the lower end of the condenser-evaporator is sealed off from the rectifying liquid so that only rectifying liquid that has been freed of impurities in the adsorber can get into the evaporator cross-sections.
  • the subject of the invention prevents the formation of freezes on the evaporator walls of the condenser-evaporator and the formation of undesirably high concentrations of higher-boiling components in the rectifying liquid in a simple, yet effective manner.
  • a header is provided on the underside of the condenser-evaporator.
  • the header serves on the one hand to seal the condenser-evaporator against the bottom liquid and on the other hand to distribute the rectifying liquid supplied by the adsorber over the flow cross-sections of the evaporator.
  • the adsorber is bridged by a lockable bypass. In this way, the amount of liquid passed through the adsorber can be set independently of the amount of liquid circulated.
  • a liquid indicator be arranged parallel to the condenser-evaporator. This allows the liquid level in the condenser-evaporator to be checked from the outside and, if necessary, changed by throttling or increasing the circulated amount of liquid.
  • a further embodiment of the invention is particularly advantageous, in which the connecting line between the condenser-evaporator and the adsorber is connected to a gas separator.
  • the pipeline runs in front of the connection point of the liquid level indicator vertical direction upwards and has a horizontal or downward sloping section between the connection point and the condenser-evaporator at least for a short time, while the gas separator is arranged essentially perpendicularly above the connection point. Gas bubbles contained in the liquid can therefore rise freely into the gas separator.
  • Analog components have the same reference numbers in both figures.
  • 1 denotes a two-stage rectification column, as is used for the low-temperature separation of air.
  • the device according to the invention is also suitable for use in the rectification of another gas mixture.
  • a single-stage rectification column could be used instead of the two-stage rectification column with a high-pressure stage 2 and a low-pressure stage 3 arranged above the high-pressure stage.
  • an oxygen-enriched liquid 4 collects during airing.
  • a nitrogen-rich gaseous gas is removed from the top of the column 2 Fraction removed (line 6) and fed to the condenser-evaporator 5, in which the gas is partially liquefied in the heat exchange with the oxygen-rich bottom liquid 4, a portion of the bottom liquid 4 evaporating.
  • the condensed liquid is returned via line 7 to the high pressure stage 2.
  • the bottom liquid 4 still contains undesirable constituents, especially hydrocarbons such as acetylene
  • part of the liquid is circulated through an adsorber 8, in which these constituents are removed.
  • nitrogen is used, for example, which is supplied via line 9 and discharged via line 10.
  • the adsorber 8 is arranged at a lower level than the liquid bath 4.
  • a condenser-evaporator 11 which is arranged in the sump 4 of the rectification column and which partially immerses in the liquid bath during operation of the column is used for liquid circulation.
  • the condenser-evaporator 11, e.g. a plate heat exchanger, is open at its upper end projecting over the liquid 4 to the inside of the low-pressure stage 3, its lower end immersed in the liquid is closed against the bottom liquid, for example with a header 12.
  • the condenser-evaporator 11 is parallel to the condenser Evaporator 5 connected to nitrogen lines 6, 7.
  • the condenser-evaporator can, as shown in the figure, be an additional evaporator, but it is also possible to form part of the heat exchange channels of the condenser-evaporator 5 such that a direct connection between the heat exchange channels and the bottom liquid is prevented.
  • a liquid extraction line 13 is provided, which is connected to the adsorber 8.
  • a flow meter 14 is arranged in line 13. The other end of the adsorber 8 is connected to a line 15 which opens into the header 12 of the condenser-evaporator 11.
  • liquid is removed from the column sump 4 via line 13, reaches the adsorber 8, where it is freed of hydrocarbons, and from there via line 15 into the header 12, from which it reaches the heat exchange channels of the condenser-evaporator 11 is distributed.
  • the liquid rises in the condenser-evaporator 11 to a height which is the same as the liquid level of the bottom liquid 4 minus an amount which corresponds to the flow resistance in the liquid extraction line 13, 15 and in the adsorber 8.
  • a portion of the liquid in the condenser-evaporator 11 evaporates due to the warm nitrogen, which is supplied via line 6.
  • Liquid is taken away by the withdrawing steam and thrown over the upper edge of the condenser-evaporator 11 into the liquid bath.
  • the evaporated amount of liquid is replaced by liquid flowing out of the rectification trays.
  • the liquid level of the bath which had dropped as a result of the liquid withdrawal, thus rises again and the static liquid pressure in the pipeline 13 increases. The process therefore works continuously.
  • liquid is also thrown over in the evaporator condenser 5.
  • the liquid is supplemented via the connection that the evaporator condenser 5 has on its underside with the liquid bath 4.
  • a direct backflow of liquid through the header 12 is prevented in the heat exchanger 11.
  • the liquid flows here via the pipes 13, 15 back into the heat exchanger until, according to the principle of the communicating tubes, a liquid level corresponding to the liquid level of the sump liquid 4 is reached. Since at the same time further liquid is evaporated from the heat exchanger and thrown over, the liquid level lags behind the state of equilibrium and a continuous liquid circuit is guaranteed.
  • it is conceivable to turn on the condenser-evaporator 11 instead of the one shown, several condenser evaporators can also be provided - instead of heating with air using nitrogen.
  • the amount of liquid circulated through the adsorber 8 should correspond approximately to the amount of oxygen obtained in the rectification.
  • a bypass line 16 is provided parallel to the adsorber 8 and is provided with a control valve 17. With this bypass line 16, the level of the liquid level in the heat exchanger can be influenced at the same time. A total evaporation of the liquid in the condenser-evaporator 11 must namely be avoided in order to prevent the heat exchanger surfaces from encrusting. There is also a risk of explosion if acetylene crystallizes out.
  • the heat exchanger should be filled to about 80% with liquid.
  • Figure 2 shows essentially the same arrangement as Figure 1.
  • a gas separator 18 is also provided here, which is connected in parallel to the condenser-evaporator 11.
  • liquid level indicators 21, 22 the height of the liquid level in the column sump and in the condenser-evaporator 11 can be easily checked from the outside and thus the optimal liquid level can always be adjusted.
  • the bypass line 16 and the line 15 coming from the adsorber run vertically upward after their union below the connection point 19 of the gas separator 18, while the connecting piece 20 between the connection point 19 and the condenser-evaporator 11 runs horizontally at least over a short section.
  • the gas separator 18 is arranged vertically above the connection point 19. If gas bubbles are now contained in the liquid rising via the lines 15, 16, these rise from the connection point 19 into the gas separator 18 and are separated from the liquid which flows via line 20 into the condenser-evaporator 11.
  • the extraction line therefore does not have to be led exactly vertically upward to the connection point 19 and the line 20 can, for example, have a section running downwards from the connection point 19.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Sampling And Sample Adjustment (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Claims (5)

1. Installation pour séparer un mélange gazeux en ses constituants par rectification, comportant une colonne de rectification (1), un adsorbeur (8) qui est relié d'un côté au liquide (4) se trouvant en cuve de la colonne de rectification et de l'autre côté à un évaporateur-condenseur, qui est en communication avec le volume de vapeur se trouvant au-dessus du liquide de cuve, caractérisée en ce que l'évaporateur-condenseur (11) plonge partiellement dans le liquide de cuve son extrémité inférieure reliée à l'adsorbeur (8) étant étanche par rapport au liquide de cuve tandis que son extrémité supérieure est ouverte en direction du volume de vapeur situé au-dessus du liquide de cuve.
2. Installation selon la revendication 1, caractérisé en ce qu'il comporte un collecteur (12) sur le côte inférieur de l'évaporateur-condenseur (11).
3. Installation selon l'une des revendications 1 ou 2, caractérisée en ce que l'adsorber (8) est contourné par un conduit de dérivation (16) obturable.
4. Installation selon l'une des revendications 1 à 3, caractérisée en ce qu'il est prévu un indicateur de niveau de liquide (22) parallèlement à l'évaporateur-condenseur (11).
5. Installation selon l'une des revendications 1 à 4, caractérisée en ce que le conduit de liaison (20) est relié à un séparateur de gaz (18) entre le condenseur (11) et l'adsorbeur (8).
EP80102953A 1979-05-30 1980-05-27 Dispositif pour la séparation d'un mélange de gaz par rectification Expired EP0019905B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT80102953T ATE2178T1 (de) 1979-05-30 1980-05-27 Vorrichtung zur zerlegung eines gasgemisches durch rektifikation.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19792922028 DE2922028A1 (de) 1979-05-30 1979-05-30 Verfahren und vorrichtung zur zerlegung eines gasgemisches durch rektifikation
DE2922028 1979-05-30

Publications (2)

Publication Number Publication Date
EP0019905A1 EP0019905A1 (fr) 1980-12-10
EP0019905B1 true EP0019905B1 (fr) 1983-01-05

Family

ID=6072077

Family Applications (1)

Application Number Title Priority Date Filing Date
EP80102953A Expired EP0019905B1 (fr) 1979-05-30 1980-05-27 Dispositif pour la séparation d'un mélange de gaz par rectification

Country Status (8)

Country Link
US (1) US4337070A (fr)
EP (1) EP0019905B1 (fr)
AT (1) ATE2178T1 (fr)
AU (1) AU535021B2 (fr)
BR (1) BR8003260A (fr)
DE (2) DE2922028A1 (fr)
IN (1) IN153137B (fr)
ZA (1) ZA803204B (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4883519A (en) * 1988-10-06 1989-11-28 Air Products And Chemicals, Inc. Process for the production of high pressure nitrogen with split reboil-condensing duty
US4957524A (en) * 1989-05-15 1990-09-18 Union Carbide Corporation Air separation process with improved reboiler liquid cleaning circuit
US5669236A (en) * 1996-08-05 1997-09-23 Praxair Technology, Inc. Cryogenic rectification system for producing low purity oxygen and high purity oxygen
US5836174A (en) * 1997-05-30 1998-11-17 Praxair Technology, Inc. Cryogenic rectification system for producing multi-purity oxygen
US5956972A (en) * 1997-12-23 1999-09-28 The Boc Group, Inc. Method of operating a lower pressure column of a double column distillation unit
US6330812B2 (en) * 2000-03-02 2001-12-18 Robert Anthony Mostello Method and apparatus for producing nitrogen from air by cryogenic distillation
FR2853723B1 (fr) * 2003-04-10 2007-03-30 Air Liquide Procede et installation de traitement d'un bain de liquide riche en oxygene recueilli en pied d'une colonne de distillation cryogenique
CN110388241B (zh) * 2019-07-31 2021-07-20 东北师范大学 一种汽车发动机废热回收热力循环系统

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE624966C (de) * 1934-09-28 1936-01-31 Linde Eismasch Ag Verfahren zur Herabsetzung des Kondensationsdruckes bei der Zerlegung der Luft durch Verfluessigung und Rektifikation
US2650482A (en) * 1948-04-29 1953-09-01 Kellogg M W Co Method of separating gas mixtures
US2590909A (en) * 1948-10-08 1952-04-01 Hanson Vegetable cutter
US2903859A (en) * 1955-09-22 1959-09-15 Union Carbide Corp Process and apparatus for separating gas mixtures
DE1033689B (de) * 1957-03-20 1958-07-10 Linde Eismasch Ag Verfahren zum Eindampfen kohlenwasserstoffhaltigen, fluessigen Sauerstoffes und Einrichtung zur Durchfuehrung des Verfahrens
US3174293A (en) * 1960-11-14 1965-03-23 Linde Eismasch Ag System for providing gas separation products at varying rates
DE1143526B (de) * 1962-01-12 1963-02-14 Linde Eismasch Ag Verfahren und Einrichtung zur Tieftemperatur-Gaszerlegung, insbesondere Luftzerlegung
GB1325166A (en) * 1969-10-20 1973-08-01 Kobe Steel Ltd Air rectification process for the production of gaseous or liquid nitrogen

Also Published As

Publication number Publication date
AU535021B2 (en) 1984-03-01
EP0019905A1 (fr) 1980-12-10
BR8003260A (pt) 1980-12-30
AU5864580A (en) 1980-12-04
ZA803204B (en) 1981-05-27
ATE2178T1 (de) 1983-01-15
DE3061536D1 (en) 1983-02-10
IN153137B (fr) 1984-06-02
DE2922028A1 (de) 1980-12-11
US4337070A (en) 1982-06-29

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