EP0689019B1 - Verfahren und Einrichtung zur Herstellung von gasförmigem Drucksauerstoff - Google Patents

Verfahren und Einrichtung zur Herstellung von gasförmigem Drucksauerstoff Download PDF

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Publication number
EP0689019B1
EP0689019B1 EP95401443A EP95401443A EP0689019B1 EP 0689019 B1 EP0689019 B1 EP 0689019B1 EP 95401443 A EP95401443 A EP 95401443A EP 95401443 A EP95401443 A EP 95401443A EP 0689019 B1 EP0689019 B1 EP 0689019B1
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European Patent Office
Prior art keywords
pressure
air
column
heat exchange
fraction
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Revoked
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EP95401443A
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English (en)
French (fr)
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EP0689019A1 (de
Inventor
Maurice Grenier
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J3/04012—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
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • F25J3/04078—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
    • F25J3/04078—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
    • 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
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • 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
    • F25J3/04187—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
    • 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
    • F25J3/04296—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
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—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
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the present invention relates to a process for producing gaseous oxygen under pressure as defined in the preamble of claim 1. Such a process is known from document FR-A-2 688 052.
  • the pressures shown are absolute pressures.
  • condensation and vaporization is a condensation or an actual spray, either pseudo-condensation or pseudo-vaporization, depending on whether the pressures are subcritical or supercritical.
  • the object of the invention is to provide a method "pump" offering great freedom of regulation of operating parameters and particularly well adapted, from the point of view of energy consumption specific as well as liquid production, large installations, i.e. producing at least 700 tonnes of oxygen per day.
  • the subject of the invention is a process for the production of gaseous oxygen gas of the aforementioned type, in which the first press is the average pressure and part of the air at the first press is sent to the medium pressure column without being relaxed.
  • the subject of the invention is also a installation for the production of gaseous oxygen intended for the implementation of the process defined above and comprising the features of claim 7.
  • the installation may in particular comprise a single air compressor with n stages, said first compression means being constituted by a certain number p of stages, with p ⁇ n , and said second compression means being constituted by the whole of the compressor.
  • the air distillation system shown in Figure 1 essentially comprises: a air compressor 1; an air cleaning device 2 compressed into water and CO2 by adsorption, this device comprising two adsorption bottles 2A, 2B, one of which works in adsorption while the other is in progress regeneration; a fan-blower assembly 3 comprising an expansion turbine 4 and a blower or blower 5 whose shafts are coupled, the blower possibly being equipped with a refrigerant (not represented); a heat exchanger 6 constituting the installation heat exchange line; a double distillation column 7 comprising a medium column pressure 8 surmounted by a low pressure column 9, with a vaporizer-condenser 10 putting the overhead vapor (nitrogen) from column 8 in heat exchange relationship with the tank liquid (oxygen) of column 9; a liquid oxygen tank 11, the bottom of which is connected to a liquid oxygen pump 12; and a nitrogen tank liquid 13, the bottom of which is connected to a nitrogen pump liquid 14.
  • This installation is mainly intended to supply, via a line 15, oxygen gaseous under a predetermined high pressure, which can be between approximately 13 bars and a few tens bars. These are significant amounts of oxygen gaseous, at least equal to around 700 t / day and capable of reach several thousand tonnes per day.
  • liquid oxygen drawn from the column 9 tank via line 16 is stored in the reservoir 11.
  • a flow of oxygen, withdrawn from this tank, is brought to high pressure by pump 12 in the liquid state, then vaporized and reheated under this high pressure in passages 17 of exchanger 6.
  • the heat necessary for this vaporization and to this reheating, as well as to reheating and possibly vaporization of other fluids drawn from the double column, is supplied by the air to be distilled, in the following conditions.
  • Compressor 1 is a multi-stage compressor, with n stages. All of the incoming atmospheric air is compressed by the first p stages at medium pressure, which is the operating pressure of column 8, then is precooled in 18 and cooled to around ambient temperature in 19, is purified in one, 2A for example, adsorption bottles, and divided into two fractions.
  • the first fraction at medium pressure, representing for example approximately 40% of the flow of treated air, is cooled from the hot end to the cold end of the heat exchange line 6, in passages 20 thereof, up to '' in the vicinity of its dew point, then is directly introduced into the tank of column 8.
  • the rest of the purified air in 2A is returned to the inlet of the ( p + 1) th stage of compressor 1 and is compressed by the following stages up to a first high air pressure, significantly higher than the average pressure of column 8, in practice greater than 9 bars.
  • the compressed air, precooled in 19A, is again divided into two streams.
  • the first flow representing at least 45% of the treated air flow, is boosted to a second high pressure by the booster 5, which is driven by the turbine 4.
  • This second high air pressure is between approximately 25 bars and the condensing pressure air by vaporizing oxygen under the high oxygen pressure.
  • the first air flow is then introduced to the hot end of exchanger 6 and completely cooled up to an intermediate temperature. At this temperature, a fraction of the air continues to cool and is liquefied in passages 20A of the exchanger, then is partially relaxed at low pressure in a relief valve 21 and partly to the average pressure in an expansion valve 21A and introduced respectively at an intermediate level in the column 9 and at the bottom of column 8. The rest air is relaxed at medium pressure in the turbine 4 then sent directly, via a line 22, at the bottom of column 8.
  • the second stream is introduced under the first high pressure in exchange line 6, cooled and liquefied until the cold end of it in passages 20B, expanded in an expansion valve 21B and connected to the current from the expansion valve 21A.
  • 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, bottle 2B in the example considered, before to be evacuated via a pipe 31.
  • part medium pressure liquid nitrogen is, after expansion in an expansion valve 32, stored in the tank 13, and that a production of liquid nitrogen and / or oxygen liquid is supplied via line 33 (for nitrogen) and / or 34 (for oxygen).
  • the installation product in addition to low pressure nitrogen gas from directly from the head of column 9 and oxygen high pressure gas, pressurized nitrogen gas, obtained by vaporization in the heat exchange line a flow of liquid nitrogen taken from line 33 via a pipe 35. This nitrogen vaporization can especially by condensation of the air contained in passages 20A or 20B.
  • FIG. 2 The installation shown in Figure 2 is intended to produce gaseous oxygen under pressure high, for example of the order of 40 bars. She understands essentially two air compressors 41 and 42, one apparatus 43 for adsorption purification, a double distillation column 44 consisting of a column medium pressure 45, operating at around 6 bars, surmounted by a low pressure column 46, operating at a pressure slightly higher than 1 bar, a heat exchange line 47, a sub-cooler 48, a liquid oxygen pump 49, a cold blower 50, a first turbine 51 whose wheel is mounted on the same tree as that of the cold blower, and a second turbine 52 braked by an appropriate brake 53 such than an alternator.
  • a double distillation column 44 consisting of a column medium pressure 45, operating at around 6 bars, surmounted by a low pressure column 46, operating at a pressure slightly higher than 1 bar
  • a heat exchange line 47 a sub-cooler 48
  • a liquid oxygen pump 49 a cold blower 50
  • a first turbine 51 whose wheel is mounted
  • the first stream is directly cooled in passages 62 of the exchange line 47.
  • a fraction of this air came out of the exchange line, relaxed at the low pressure in turbine 52, and blown into a intermediate point of the column 46 via a pipe 63.
  • the rest of the medium pressure air continues to cool to the cold end of the exchange line, where it is near its dew point and then is sent to the bottom of column 45.
  • the rest of the air from the device 43 is compressed at a first high pressure, for example from 16.5 bars, by compressor 42, then enters air cooling passages 64 of the exchange line.
  • the blower 50 which provides this compression is driven by the turbine 51, so that none external energy is required. Take in account the mechanical losses, the amount of cold produced by this turbine is slightly higher than the heat of compression, and the excess contributes to keeping cold of the installation. The balance of the necessary frigories for this keeping cold is provided by the turbine 52, or, alternatively, if the oxygen to be produced must have a high purity, by air or nitrogen expansion to medium pressure in a turbine, in a conventional manner.
  • the installation can also generate oxygen at a pressure low enough to allow vaporization of oxygen by condensation at the highest process air pressure.
  • This oxygen pressure would be less than 8 for example bars.
  • a second pump 70 compressing liquid oxygen reduced purity at lower intermediate pressure at 8 bars. This oxygen is vaporized by condensation of a corresponding part of the air supercharged by the blower 50, which only has to supply the heat of compensation for excess cold due to vaporization high pressure oxygen.
  • mixed lines have been indicated on the Figure 2 a medium pressure liquid nitrogen pump 71 bringing this nitrogen, withdrawn from column 45, to a intermediate pressure low enough to allow its vaporization by air condensation at the highest process pressure, i.e. 23 bars.
  • FIG. 2 Also shown in Figure 2 is a line 72 for the production of liquid oxygen withdrawn from the tank of the column 46, as well as a pipe 72A of production of liquid nitrogen from the head of the column 45.
  • FIG. 3 The installation in Figure 3 is a variant of that of Figure 2.
  • a fraction of the air coming from the compressor 42 is overpressed by a hot blower 73, cooled in 47 to temperature T2, again boosted by the blower cold 50, reintroduced into the exchange line at a temperature T3 higher than T2, then treated in two different flows from temperature T4, like previously.
  • the rest of the air from compressor 42 is cooled in additional passages 74 of the exchange line 47 up to a temperature T5 included between temperatures T4 and T1, and, at this temperature, some of this air has come out of the exchange line, expanded at medium pressure in an additional turbine 75 coupled to the blower 73, then sent to the tank from column 45.
  • the rest of the air carried by the passages 74 continues to cool down to the end cold of the exchange line, where it is liquefied and sub-cooled, then is relaxed at medium pressure in a expansion valve 76 and sent in the lower part from column 45.
  • the invention is particularly advantageous, from an energy point of view, when the pressure of oxygen vaporization is greater than approximately 20 bars.

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  • 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)
  • Oxygen, Ozone, And Oxides In General (AREA)

Claims (12)

  1. Verfahren zur Herstellung von gasförmigem Sauerstoff unter Druck, bei dem Luft in einer Vorrichtung mit Destillationsdoppelsäule (7; 44) destilliert wird, die eine Mitteldrucksäule (8; 45), die unter einem sogenannten Mitteldruck arbeitet, eine Niederdrucksäule (9; 46), die unter einem sogenannten Niederdruck arbeitet, und eine Wärmeaustauschleitung (6; 47) zum Wärmeaustausch zwischen der zu destillierenden Luft und den der Doppelsäule entnommenen Produkten umfaßt; der Niederdrucksäule flüssiger Sauerstoff entnommen wird; der flüssige Sauerstoff auf einen Sauerstoffverdampfungsdruck von mindestens etwa 13 bar gebracht und verdampft wird und unter dem Verdampfungsdruck durch Wärmeaustausch mit der zu destillierenden Luft während deren Abkühlung erwärmt wird;
    eine erste Fraktion der zu destillierenden Luft (bei 1; 41) auf einen ersten Druck verdichtet wird und diese Luft in der Wärmeaustauschleitung (6; 47) bis nahe an ihren Taupunkt gekühlt und in die Doppelsäule (7; 44) geleitet wird;
    eine zweite Fraktion der zu destillierenden Luft (bei 1, 5; 41, 42, 50; 41, 42, 73, 50) durch Wärmeaustausch mit dem Sauerstoff während dessen Verdampfung unter dem Sauerstoffverdampfungsdruck auf einen Lufthochdruck, der insbesondere mindestens etwa 25 bar beträgt und kleiner als der Kondensationsdruck der Luft ist, verdichtet wird, diese Luft gekühlt wird, und ein Teil davon, der dann (bei 21, 21A; 68) vor dem Einleiten in die Doppelsäule entspannt wird, verflüssigt wird, während ein anderer Teil der unter dem Lufthochdruck stehenden Luft der Wärmeaustauschleitung (6; 47) bei einer Kühlzwischentemperatur entnommen und in einer ersten Entspannungsturbine (4; 51) auf den Mitteldruck entspannt und dann in die Doppelsäule (7; 44) geleitet wird; und
    der Vorrichtung (bei 33, 34; 72, 72A) mindestens ein flüssiges Produkt entnommen wird, dadurch gekennzeichnet, daß der erste Druck dem Mitteldruck entspricht und ein Teil der unter dem ersten Druck stehenden Luft, ohne entspannt zu werden, der Mitteldrucksäule zugeführt wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß eine dritte Fraktion der zu destillierenden Luft (bei 1; 1, 42) bei einem Zwischendruck, der zwischen dem ersten Druck und dem Lufthochdruck liegt, verdichtet, gekühlt, (bei 20B; 64; 74) verflüssigt, (bei 21B; 69; 76) entspannt und in die Doppelsäule (7; 44) geleitet wird.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß die zweite Luftfraktion (bei 42, 42, 73) auf einen Luftzwischendruck gebracht, nur partiell gekühlt und dann (bei 50) mittels eines Kaltverdichters nachverdichtet, in die Wärmeaustauschleitung (47) zurückgeleitet und bis auf die Zwischentemperatur gekühlt wird, bei der die Luft erneut der Wärmeaustauschleitung entnommen und in der Entspannungsturbine (51), die mit dem Kaltverdichter gekoppelt ist, auf den Mitteldruck entspannt und in die Doppelsäule (44) geleitet wird.
  4. Verfahren nach Anspruch 2 und 3, dadurch gekennzeichnet, daß nach partieller Kühlung ein Teil der dritten Luftfraktion in einer zweiten Turbine (75), die mit einem Verdichter (73) zur Nachverdichtung der zweiten Luftfraktion gekoppelt ist, auf den Mitteldruck entspannt und dann in die Mitteldrucksäule (45) geleitet wird.
  5. Verfahren nach Anspruch 3 oder 4, dadurch gekennzeichnet, daß ein Teil der unter dem ersten Druck stehenden Luft der Wärmeaustauschleitung (47) bei einer dritten Kühlzwischentemperatur entnommen und in einer Turbine (52) auf den Niederdruck entspannt wird, bevor er an einer Zwischenstelle der Niederdrucksäule (46) zugeführt wird.
  6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß der Sauerstoffverdampfungsdruck in etwa dem Produktionsdruck entspricht.
  7. Vorrichtung zur Herstellung von gasförmigem Sauerstoff unter Druck, umfassend: eine Luftdestillationsdoppelsäule (7; 44) mit einer Mitteldrucksäule (8; 45), die unter einem sogenannten Mitteldruck arbeitet, und einer Niederdrucksäule (9; 46), die unter einem sogennanten Niederdruck arbeitet; eine Wärmeaustauschleitung (6; 47) zum Wärmeaustausch zwischen der zu destillierenden Luft und den aus der Doppelsäule stammenden Produkten; Mittel zur Entnahme von flüssigem Sauerstoff aus der Niederdrucksäule; und Mittel (12; 49), um den flüssigen Sauerstoff auf einen Sauerstoffverdampfungsdruck von mindestens etwa 13 bar zu bringen, wobei die Wärmeaustauschleitung Mittel zum Wärmeaustausch zwischen dem unter dem Verdampfungsdruck stehenden flüssigen Sauerstoff und der zu destillierenden Luft während deren Abkühlung umfaßt;
    erste Verdichtungsmittel (1; 41) zur Verdichtung einer ersten Fraktion der zu destillierenden Luft auf einen Druck nahe dem Mitteldruck und Kanäle (20; 62) der Wärmeaustauschleitung, die einerseits mit den ersten Verdichtungsmitteln und andererseits mit der Doppelsäule (7; 44) verbunden sind;
    zweite Verdichtungsmittel (1, 5; 41, 42, 50; 41, 42, 73, 50) zur Verdichtung einer zweiten Fraktion der zu destillierenden Luft durch Wärmeaustausch mit unter dem Verdampfungsdruck verfampfendem Sauerstoff auf einen Lufthochdruck, der insbesondere mindestens etwa 25 bar beträgt und kleiner als der Kondensationsdruck der Luft ist;
    wobei die Wärmeaustauschleitung Hochdruckluftkanäle (20A; 64) zum Kühlen der zweiten Luftfraktion bis auf eine Zwischentemperatur und noch weiteren Kühlen und Verflüssigen eines Teils dieser zweiten Fraktion umfaßt und die Vorrichtung Mittel (21A; 68, 69) zum Entspannen des verflüssigten Teils umfaßt, die mit der Doppelsäule verbunden sind;
    eine erste Entspannungsturbine (4; 75), deren Ansaugseite mit den Hochdruckfluftkanälen (74) und deren Auslaßseite mit der Doppelsäule (7; 44) verbunden ist; und
    Mittel (72, 72A) zur Entnahme mindestens eines flüssigen Produkts aus der Vorrichtung dadurch gekennzeichnet, daß die ersten Verdichtungsmittel über andere Mittel als die Entspannungsmittel mit der Mitteldrucksäule verbunden sind.
  8. Vorrichtung nach Anspruch 7, dadurch gekennzeichnet, daß sie Mittel (1; 1, 42) zum Verdichten einer dritten Fraktion der zu destillierenden Luft auf einen zwischen dem ersten Druck und dem Lufthochdruck liegenden Zwischendruck umfaßt, wobei die Wärmeaustauschleitung (6; 47) Kanäle (20B; 64; 74) zum Kühlen und Verflüssigen der dritten Fraktion und eine Leitung umfaßt, die das kalte Ende dieser Kanäle mit der Doppelsäule (7; 44) verbindet und mit einem Druckminderventil (21B; 69; 76) ausgestattet ist.
  9. Vorrichtung nach Anspruch 7 oder 8, dadurch gekennzeichnet, daß sie einen einzigen Luftverdichter (1) mit n Stufen umfaßt, wobei die ersten Verdichtungsmittel aus einer bestimmten Anzahl p an Stufen mit p < n und die zweiten Verdichtungsmittel aus dem gesamten Verdichter bestehen.
  10. Vorrichtung nach Anspruch 7 oder 8, dadurch gekennzeichnet, daß die zweiten Verdichtungsmittel (42, 50) einen Verdichter, dessen Druckseite mit dem warmen Ende der Wärmeaustauschleitung (47) verbunden ist, und einen Verdichter (50) umfassen, dessen Ansaugseite und dessen Druckseite mit Zwischenstellen des letzteren verbunden sind.
  11. Vorrichtung nach Anspruch 8 und 10, dadurch gekennzeichnet, daß die zweiten Verdichtungsmittel einen Verdichter (73) zur Nachverdichtung der zweiten Luftfraktion umfassen, der mit einer zweiten Turbine (75) zur Entspannung eines Teils der dritten Luftfraktion gekoppelt ist.
  12. Vorrichtung nach Anspruch 10 oder 11, dadurch gekennzeichnet, daß der Kaltverdichter (50) mit der ersten Turbine (51) gekoppelt ist, und daß die Vorrichtung eine Turbine (52) umfaßt, die mit einem Teil der unter dem ersten Druck stehenden Luft versorgt wird und deren Auslaß mit der Niederdrucksäule (46) verbunden ist.
EP95401443A 1994-06-20 1995-06-19 Verfahren und Einrichtung zur Herstellung von gasförmigem Drucksauerstoff Revoked EP0689019B1 (de)

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FR9407531A FR2721383B1 (fr) 1994-06-20 1994-06-20 Procédé et installation de production d'oxygène gazeux sous pression.

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US20150114037A1 (en) * 2013-10-25 2015-04-30 Neil M. Prosser Air separation method and apparatus
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FR3062197B3 (fr) 2017-05-24 2019-05-10 Air Liquide Procede et appareil pour la separation de l'air par distillation cryogenique
JP6900241B2 (ja) 2017-05-31 2021-07-07 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 ガス製造システム
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JPH08175806A (ja) 1996-07-09
US5596885A (en) 1997-01-28
DE69511013T2 (de) 2000-01-20
CN1120652A (zh) 1996-04-17
FR2721383A1 (fr) 1995-12-22
CA2152010A1 (fr) 1995-12-21
KR960001706A (ko) 1996-01-25
DE69511013D1 (de) 1999-09-02
FR2721383B1 (fr) 1996-07-19
EP0689019A1 (de) 1995-12-27
ES2136259T3 (es) 1999-11-16
CN1081782C (zh) 2002-03-27

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