EP0611218B2 - Verfahren und Anlage zur Herstellung von Drucksauerstoff - Google Patents

Verfahren und Anlage zur Herstellung von Drucksauerstoff Download PDF

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Publication number
EP0611218B2
EP0611218B2 EP94400300A EP94400300A EP0611218B2 EP 0611218 B2 EP0611218 B2 EP 0611218B2 EP 94400300 A EP94400300 A EP 94400300A EP 94400300 A EP94400300 A EP 94400300A EP 0611218 B2 EP0611218 B2 EP 0611218B2
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EP
European Patent Office
Prior art keywords
pressure
air
fraction
column
turbine
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 - Lifetime
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EP94400300A
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English (en)
French (fr)
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EP0611218B1 (de
EP0611218A1 (de
Inventor
Maurice Grenier
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0611218A1 publication Critical patent/EP0611218A1/de
Publication of EP0611218B1 publication Critical patent/EP0611218B1/de
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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
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    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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    • 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
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
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    • 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
    • F25J3/0429—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 of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—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
    • F25J3/0429—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 of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • 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
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    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
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    • 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
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    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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    • 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
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods
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    • F25J2290/62—Details of storing a fluid in a tank
    • 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
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    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas
    • 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
    • Y10S62/939—Partial feed stream expansion, air
    • Y10S62/94—High pressure column

Definitions

  • the present invention relates to a method of production of gaseous oxygen under high pressure oxygen.
  • EP-A-0 504 029 describes a process of this type in which the fraction of the air that is overpressed to the second high pressure is constituted by a very low air flow, the only function of which is to supply calories near the intake temperature of the turbine which expands the fraction of unpressurized air.
  • the invention aims to improve this process known in order to increase thermodynamic performance without increasing the corresponding investment.
  • the invention relates to a method of aforementioned type, according to claim 1.
  • the air distillation installation shown in Figure 1 essentially comprises: a compressor air 1; a device 2 for purifying compressed air in water and CO2 by adsorption, this device comprising two adsorption bottles 2A, 2B, one of which works in adsorption while the other is being regeneration; a turbine-blower assembly 3 comprising an expansion turbine 4 and a blower or booster 5 with shafts coupled, the blower possibly being fitted with a retrigrant (not shown); a heat exchanger 6 constituting the line heat exchange of the installation; a double distillation column 7 comprising a column medium pressure B surmounted by a low column pressure 9, with a vaporizer-condenser 10 putting the overhead vapor (azole) of column 8 in relation heat exchange with the tank liquid (oxygen) from column 9; a liquid oxygen tank 11 of which the bottom is connected to a liquid oxygen pump 12; and a liquid nitrogen tank 13, the bottom of which is connected to a liquid nitrogen pump 14.
  • This installation is intended to supply, via a pipe 15, gaseous oxygen under high pressure predetermined, which can be between a few bars and a few dozen bars (in this brief, the pressures considered are absolute pressures).
  • liquid oxygen drawn from the tank from column 9 via line 16 and stored in the tank 11, is brought to high pressure by the pump 12 in the liquid state, then vaporized and reheated under this high pressure in passages 17 of the exchanger 6.
  • the heat necessary for this vaporization and reheating, as well as reheating and possibly to the vaporization of other fluids drawn from the double column, is supplied by the air to be distilled, under the conditions following.
  • All of the air to be distilled is compressed by the compressor 1 at a first high pressure markedly higher than average column pressure 8, in practice greater than 9 bars. Then the air, precooled in 18 and cooled to around room temperature in 19, is purified in one, 2A for example, bottles adsorption, and divided into two fractions.
  • the first fraction representing at least 70% of the treated air flow, is boosted to a second high pressure by the booster 5, which is driven by the turbine 4.
  • the first fraction of air is then introduced at the end heat exchanger 6 and completely cooled to an intermediate temperature. At this temperature, a fraction of the air continues to cool and is liquefied in passages 20 of the exchanger, then is relaxed at low pressure in an expansion valve 21 and introduced at an intermediate level in the column 9. The rest of the air is relaxed to average pressure in turbine 4 then sent directly, via a pipe 22, at the base of column 8.
  • the second fraction is introduced under the first high pressure in exchange line 6, cooled and liquefied until cold end of it in passages 20A, relaxed in an expansion valve 21A and connected to the current from the expansion valve 21.
  • Low pressure nitrogen is heated in passages 28 of exchanger 6 then recovered via a pipe 29, while the waste gas, after heating in passages 30 of the exchanger, is used to regenerate an adsorption bottle, the bottle 2B in the example considered, before being evacuated via a pipe 31.
  • this air pressure is the pressure of air condensation by heat exchange with oxygen during vaporization under high pressure, i.e. the pressure at which the knee G liquefies of one of the two air fractions, on the diagram heat exchange (temperatures on the abscissa, amounts of heat exchanged on the ordinate) is located slightly to the right of the vertical spraying stage P oxygen under high pressure ( Figure 2).
  • the temperature difference at the hot end of the line is adjusted by means of the turbine 4, the suction temperature is indicated in A.
  • the diagram in Figure 2 corresponds to the values following digital: first high pressure: 24.5 bars; high oxygen pressure: 10 bars; second high pressure: 31 bars; second fraction of air: 28% of the incoming flow liquefied fraction in 20: very low; liquid production: 40% of the amount of oxygen separate.
  • the diagram in Figure 3 corresponds to the values following digital: first high pressure: 28.5 bars; purification temperature: + 12 ° C; second air fraction: 11% of the incoming flow; second high pressure: 36.4 bars; fraction relaxed in 4 to 5.7 bars: 77% of the incoming flow; liquefied fraction in 20: 12% of incoming air flow; high oxygen pressure: 40 bars: liquid production: 35% of the amount of oxygen separated.
  • the air from the turbine 4 is sent to a separator pot 35.
  • the phase resulting liquid is sent directly to the column 8, while the gas phase is, after heating partial in the heat exchange line, relaxed at low pressure in a second turbine 36 fitted with an appropriate brake 37, then blown into the column 9.
  • This variant allows either to produce oxygen impure under good energy conditions thanks to the increased production of liquid which results from the presence of the second turbine, soil increase liquid production at the expense of amount of oxygen separated, or produce only liquid oxygen.
  • Figure 6 illustrates another variant in which the first high pressure is that of the penultimate main compressor stage 1.
  • the air is divided into two fractions as previously.
  • the first fraction is reintroduced at the suction of the last stage of compressor 1, and comes out at higher pressure.
  • this air is overpressed every second high pressure in 5 then is treated as explained more high.
  • the second fraction of air is directly introduced in the passages 20A of the heat exchange line.
  • the installation can produce, in addition to low pressure nitrogen gas coming directly from the head of column 9 and high pressure oxygen gas, nitrogen gas under pressure, obtained by spraying in the line heat exchange of a flow of liquid nitrogen sampled in line 33.
  • This nitrogen vaporization can in particular by condensation of the contained air in passages 20 or 20A.
  • the installation can produce gaseous oxygen and / or nitrogen gas under at least two pressures different, as explained in EP-A-0 504 029 cited above.
  • a small part of the air coming from the blower 5 can be overpressed again by a second blower (not shown), for example coupled to the turbine 36 of FIG. 5, before being cooled and liquefied in the heat exchange line, according to the teaching of the request FR 91 15 935.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (5)

  1. Verfahren zur Erzeugung von gasförmigem Sauerstoff unter hohem Sauerstoffdruck durch Destillation von Luft in einer Doppelsäulenanlage (7), die eine unter einem sogenannten mittleren Druck arbeitende Mitteldrucksäule (8) und eine unter einem sogenannten niedrigen Druck arbeitende Niederdrucksäule (9) aufweist, Pumpen (bei 12) von aus dem Sumpf der Niederdrucksäule (9) abgezogenem flüssigem Sauerstoff und Verdampfen (bei 6) des verdichteten flüssigen Sauerstoffs durch Wärmeaustausch mit Luft in einer Wärmeaustauschleitung (6) der Anlage, bei dem man:
    die gesamte zu destillierende Luft mit Hilfe eines Hauptluftverdichters (1) der Anlage auf einen ersten hohen Druck verdichtet, der deutlich über dem mittleren Druck liegt, und in eine erste und eine zweite Fraktion aufteilt,
    die erste Fraktion auf einen zweiten hohen Druck nachverdichtet und
    die gesamte erste Fraktion in der Wärmeaustauschleitung auf eine Zwischentemperatur abkühlt, bei der ein Teil in einer ersten Turbine (4) auf den mittleren Druck entspannt und dann in die Mitteldrucksäule (8) eingespeist wird, während der Rest weiter gekühlt und verflüssigt, in einem Druckminderventil (21) entspannt und in die Doppelsäule (7) eingespeist wird,
    wobei die erste Fraktion mindestens 70% des behandelten Luftdurchsatzes darstellt und bei dem man die zweite Fraktion zu einem einzigen Strom bei dem ersten hohen Druck abkühlt und verflüssigt, dann in einem Druckminderventil (21 A) entspannt und in die Doppelsäule einspeist.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß man die gasförmige Fraktion der von der ersten Turbine (4) kommenden Luft auf den niedrigen Druck entspannt, wobei diese gasförmige Fraktion vor ihrer Entspannung in der zweiten Turbine teilweise angewärmt wird und der Ausstoß dieser Turbine gegebenenfalls nach Abkühlung in die Niederdrucksäule (9) eingeleitet wird.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß man die Luft mit Hilfe nur eines Teils der Stufen des Luftverdichters (1) auf den ersten hohen Druck bringt, die Luft bei diesem ersten hohen Druck von Wasser und Kohlendioxid befreit (bei 2) und dann die erste Fraktion mit Hilfe der letzten Stufe bzw. der letzten Stufen dieses Verdichters verdichtet.
  4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß man mindestens einen Teil der aus der letzten Stufe des Verdichters (1) austretenden Luft mit Hilfe eines mit der ersten Turbine (4) gekoppelten Gebläses (5) nachverdichtet.
  5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß man die zweite Fraktion vor dem Einspeisen in die Wärmeaustauschleitung (6) mit Hilfe eines Kühlaggregats (6A) vorkühlt.
EP94400300A 1993-02-12 1994-02-11 Verfahren und Anlage zur Herstellung von Drucksauerstoff Expired - Lifetime EP0611218B2 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9301622 1993-02-12
FR9301622A FR2701553B1 (fr) 1993-02-12 1993-02-12 Procédé et installation de production d'oxygène sous pression.

Publications (3)

Publication Number Publication Date
EP0611218A1 EP0611218A1 (de) 1994-08-17
EP0611218B1 EP0611218B1 (de) 1998-11-04
EP0611218B2 true EP0611218B2 (de) 2002-08-07

Family

ID=9444023

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Application Number Title Priority Date Filing Date
EP94400300A Expired - Lifetime EP0611218B2 (de) 1993-02-12 1994-02-11 Verfahren und Anlage zur Herstellung von Drucksauerstoff

Country Status (10)

Country Link
US (1) US5426947A (de)
EP (1) EP0611218B2 (de)
JP (1) JPH06241650A (de)
CN (1) CN1101924C (de)
AU (1) AU660385B2 (de)
CA (1) CA2115399C (de)
DE (1) DE69414282T3 (de)
ES (1) ES2124856T5 (de)
FR (1) FR2701553B1 (de)
ZA (1) ZA94968B (de)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19815885A1 (de) * 1998-04-08 1999-10-14 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt bei der Tieftemperaturzerlegung von Luft
FR2782544B1 (fr) * 1998-08-19 2005-07-08 Air Liquide Pompe pour un liquide cryogenique ainsi que groupe de pompage et colonne de distillation equipes d'une telle pompe
FR2828273A1 (fr) * 2001-07-31 2003-02-07 Air Liquide Procede d'alimentation en air epure d'une unite de distillation d'air cryogenique et installation de mise en oeuvre de ce procede
US7437890B2 (en) * 2006-01-12 2008-10-21 Praxair Technology, Inc. Cryogenic air separation system with multi-pressure air liquefaction
US7487648B2 (en) * 2006-03-10 2009-02-10 Praxair Technology, Inc. Cryogenic air separation method with temperature controlled condensed feed air
FR2928446A1 (fr) * 2008-03-10 2009-09-11 Air Liquide Procede de modification d'un appareil de separation d'air par distillation cryogenique
DE102009048456A1 (de) * 2009-09-21 2011-03-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren

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US4303428A (en) † 1979-07-20 1981-12-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic processes for separating air
EP0464630A1 (de) † 1990-06-27 1992-01-08 Praxair Technology, Inc. Tieftemperatur-Lufttrennung mit Nebenverdampfer für beide Produkte
US5157926A (en) † 1989-09-25 1992-10-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for refrigerating, corresponding refrigerating cycle and their application to the distillation of air
EP0588690A1 (de) † 1992-09-16 1994-03-23 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Kryogenische Behandlungsanlage, insbesonders für die Lufttrennung

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JP2909678B2 (ja) * 1991-03-11 1999-06-23 レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード 圧力下のガス状酸素の製造方法及び製造装置
FR2674011B1 (fr) * 1991-03-11 1996-12-20 Maurice Grenier Procede et installation de production d'oxygene gazeux sous pression.

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4303428A (en) † 1979-07-20 1981-12-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic processes for separating air
US5157926A (en) † 1989-09-25 1992-10-27 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for refrigerating, corresponding refrigerating cycle and their application to the distillation of air
EP0464630A1 (de) † 1990-06-27 1992-01-08 Praxair Technology, Inc. Tieftemperatur-Lufttrennung mit Nebenverdampfer für beide Produkte
EP0588690A1 (de) † 1992-09-16 1994-03-23 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Kryogenische Behandlungsanlage, insbesonders für die Lufttrennung

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Title
De Percin, G.: "La production d'oxygène sous pression", Bulletin of the International Institute of Refrigeration (Supplement) 1955, pp. 27 to 37 †

Also Published As

Publication number Publication date
EP0611218B1 (de) 1998-11-04
FR2701553A1 (fr) 1994-08-19
ES2124856T3 (es) 1999-02-16
CN1100514A (zh) 1995-03-22
JPH06241650A (ja) 1994-09-02
DE69414282D1 (de) 1998-12-10
CA2115399A1 (fr) 1994-08-13
CN1101924C (zh) 2003-02-19
AU5506094A (en) 1994-08-18
AU660385B2 (en) 1995-06-22
CA2115399C (fr) 2005-04-26
EP0611218A1 (de) 1994-08-17
US5426947A (en) 1995-06-27
ZA94968B (en) 1994-08-24
DE69414282T2 (de) 1999-06-17
ES2124856T5 (es) 2003-03-01
FR2701553B1 (fr) 1995-04-28
DE69414282T3 (de) 2003-03-20

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