EP0576314B2 - Verfahren und Apparat zur Herstelling von gasförmigem Sauerstoff unter Druck - Google Patents

Verfahren und Apparat zur Herstelling von gasförmigem Sauerstoff unter Druck Download PDF

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Publication number
EP0576314B2
EP0576314B2 EP93401395A EP93401395A EP0576314B2 EP 0576314 B2 EP0576314 B2 EP 0576314B2 EP 93401395 A EP93401395 A EP 93401395A EP 93401395 A EP93401395 A EP 93401395A EP 0576314 B2 EP0576314 B2 EP 0576314B2
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EP
European Patent Office
Prior art keywords
air
pressure
turbine
column
oxygen
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French (fr)
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EP0576314A1 (de
EP0576314B1 (de
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Maurice Grenier
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Air Liquide SA
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
    • F25J3/04151—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
    • F25J3/04006—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
    • F25J3/04151—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
    • 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
    • F25J3/04193—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
    • 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
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods
    • 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 production process gaseous oxygen under pressure by air distillation in an installation comprising a heat exchange line and a double column of distillation which itself has a first column, called a column medium pressure, operating under medium pressure, and a second column, called low pressure column, operating under a low pressure, pumping of liquid oxygen withdrawn from the bottom column tank pressure, and vaporization of compressed oxygen by heat exchange with compressed air at high air pressure, all of the air to be treated being compressed at a first pressure P1 significantly greater than the medium pressure, the air at pressure P1 is divided into only two parts, the first being cooled and the second part being overpressed to a second high pressure P2 and cooled, most of at least the separated oxygen being withdrawn in the liquid state from the low pressure column, compressed by a pump at least a first pressure of vaporization to which it vaporizes by condensation of air at one of said high pressures P1, P2, and vaporized by condensation of air at one of these pressures.
  • the object of the invention is to provide a method using a unique air compressor with high thermodynamic efficiency overall.
  • the invention also relates to an installation for producing gaseous oxygen under pressure for the implementation of the process described above, of the type comprising a double air distillation column comprising a column, called a low pressure column, operating under low pressure, and a column, called medium pressure column operating under medium pressure, a liquid oxygen compression pump drawn from the bottom of the low pressure column, compression means for bringing the air to be distilled to a high air pressure significantly higher than the medium pressure, and a heat exchange line for bringing the high pressure air and compressed liquid oxygen into heat exchange relationship, the compression means comprising a compressor for supplying all of the air to be distilled at a first high pressure P1 significantly higher than the medium pressure, and means for overpressuring a fraction of the air under this p first high pressure to a second high pressure P2, characterized in that these overpressure means comprise at least two blowers in series each coupled to an expansion turbine, one blower being coupled to an air expansion turbine under the first high pressure P1 and another blower being coupled to a second turbine for expanding part of the compressed air, and in that
  • the installation shown in Figure 1 is intended to produce gaseous oxygen at two different pressures, nitrogen gas under two different pressures, liquid oxygen and liquid nitrogen.
  • the installation essentially comprises a double column of distillation 1, a heat exchange line 2, an air compressor main 3, two blowers in series 4 and 5 provided with an outlet refrigerant 6, a "hot” turbine 7, a “cold” turbine 8, two pumps liquid oxygen 9, 10 and a liquid nitrogen pump 11.
  • Double column 1 includes a column medium pressure operating at 5 to 6 bar, one low pressure column 13 of the "minaret" type operating a little above atmospheric pressure, a vaporizer-condenser 14 which puts the overhead vapor (nitrogen) from column 12 in heat exchange relationship with the tank liquid (oxygen) from column 13, and an auxiliary column 15 for the production of impure argon coupled to column 13.
  • the fan wheel 4 is rigidly coupled to that of turbine 8, and, similarly, the wheel of fan 5 is rigidly coupled to that of the turbine 7.
  • the air to be distilled is fully compressed by compressor 3 at one pressure P1 of the order of 25 to 35 bars and purified in water and carbon dioxide in an adsorber 21, then divided in two streams.
  • the first current, at pressure P1, is cooled to an intermediate temperature T1 between 0 ° C and - 60 ° C. Part of this first current continues to cool, is liquefied, then is relieved at medium pressure in a valve trigger and sent to column 12 via a pipe 22. The rest of the first stream is out of the line exchange at temperature T1, relaxed to the average pressure in turbine 7, reintroduced into the line exchange, cooled and liquefied, then sent to the column 12 via a line 23.
  • the rest of the air leaving the adsorber 21 is blown up in two stages by blowers 4 and 5, up to a pressure P2 of the order of 35 to 50 bars, precooled in 6 then cooled in the exchange line up to a second intermediate temperature T2 clearly less than T1 and between -80 ° C and -130 ° C. Part of this air continues to cool, is liquefied and then relaxed at medium pressure in an expansion valve and introduced into column 12 via line 22 above. The rest of the air under pressure P2 has left the exchange line at temperature T2, expanded at medium pressure in turbine 8 and introduced into column 12 via line 23 above.
  • the exchange diagram includes a curve C1 corresponding to all of the heated fluids, and a curve C2 corresponding to the air treated during cooling.
  • the installation may include a third turbine 30, for example braked by a alternator 31, adapted to relax at low pressure part of the medium pressure air from the turbine 7.
  • the exhaust of the turbine 30 is connected to an intermediate point in column 13 or to the pipe carrying residual impure nitrogen. Admission of turbine 30 is at a temperature of -100 ° C to -150 ° C about.
  • Such a low pressure turbine is interesting in two cases: on the one hand, to enhance the low separation energy when oxygen is product with a purity between 85% and 98%, in increasing fluid production without decreasing notable of the oxygen extraction yield; else hand, to increase the production of liquid at the expense that of oxygen. If, as shown, the installation argon product, it is better to send low pressure air in impure nitrogen to maintain a good argon extraction yield. In the case reverse, this low pressure air can be blown into column 13.
  • the diagram in Figure 4 does not differ from that in Figure 1 only by mounting turbines 7 and 8. Indeed, it is the "hot” turbine 7 which is supplied by air at the highest pressure P2, while the “cold” turbine 8 is supplied with air at the pressure P1. In addition, the turbine 7 escapes a pressure P3 higher than medium pressure and, in practice, between this average pressure and the pressure P1.
  • the air at pressure P3 is cooled and liquefied in the exchange line, by oxygen spraying, then expanded at medium pressure in an expansion valve 34 before to be sent in column 12. This provision is particularly interesting for oxygen pressure between 3 bars and 8 bars.
  • the exchange line 2 of the installation includes three pressure air cooling passages different.
  • One or more of these pressures can be used to condense air by vaporization to against the current, with a small temperature difference of around 2 ° C, at least most of the oxygen separated, compressed in the liquid state to a corresponding pressure and vaporized under this pressure, oxygen additional to another pressure and / or nitrogen which may also be compressed in liquid form and vaporized in exchange line 2.
  • the installation produces a fraction of oxygen and nitrogen in liquid form with excellent specific energy due to the use two temperature expansion turbines very different admission.

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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 (14)

  1. Verfahren zur Herstellung gasförmigen Sauerstoffs unter Druck durch Destillation von Luft in einer Vorrichtung mit einer Wärmeaustauschleitung (2) und einer Destillationsdoppelkolonne (1), die selbst wiederum eine als Mitteldruckkolonne bezeichnete und unter einem mittleren Druck arbeitende erste Kolonne (12) und eine als Niederdruckkolonne bezeichnete und unter einem niedrigen Druck arbeitende zweite Kolonne (13) umfaßt, Pumpen (bei 9, 10) flüssigen, am Sumpf der Niederdruckkolonne entnommenen Sauerstoffs und Verdampfen des verdichteten Sauerstoffs durch Austausch von Wärme gegen auf einen hohen Luftdruck verdichtete Luft, wobei die gesamte, zu verarbeitende Luft auf einen ersten Druck P1 deutlich größer als der mittlere Druck verdichtet wird, die Luft mit dem Druck P1 in nur zwei Teile aufgeteilt wird, von welchen der erste Teil abgekühlt und der zweite Teil auf einen zweiten hohen Druck P2 nachverdichtet und abgekühlt wird, der Großteil zumindest des abgetrennten Sauerstoffs in flüssiger Form der Niederdruckkolonne (13) entnommen, durch eine Pumpe (9, 10) auf wenigstens einen ersten Verdampfungsdruck, bei dem er durch Kondensation von Luft verdampft, komprimiert und durch Kondensation von Luft verdampft wird,
    dadurch gekennzeichnet, daß:
    der erste Teil dieser Luft bis auf eine erste Zwischentemperatur T1 abgekühlt wird, auf der eine erste Fraktion in einer ersten Turbine (8) entspannt wird, während der Rest dieses ersten Teils abgekühlt, verflüssigt, entspannt und in die Mitteldruckkolonne (12) eingeleitet wird;
    der zweite Teil bis auf eine zweite Zwischentemperatur T2 abgekühlt wird, auf der eine erste Menge in einer zweiten Turbine (8) entspannt wird, während der Rest dieses ersten Teils abgekühlt, verflüssigt, entspannt und in die Mitteldruckkolonne (12) eingeleitet wird;
    gegebenenfalls der Verdichtungsdruck einer der Turbinen (7, 8) auf einen Druck P3 zwischen dem ersten, hohen Druck und dem mittleren Druck geregelt wird,
    und der verdichtete Sauerstoff durch Kondensation von Luft bei einem oder mehreren der Drücke P1, P2, P3 verdampft.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß eine der Zwischentemperaturen T1 und T2 aus dem Bereich zwischen etwa 0°C und -60°C und die andere aus dem Bereich zwischen etwa -80°C und -130°C gewählt wird.
  3. Verfahren nach einem der Ansprüche 1 oder 2, dadurch gekennzeichnet, daß etwa 20 bis 30% der verarbeiteten Luftmenge die erste Turbine (7) speisen.
  4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß am Sumpf der Niederdruckkolonne (13) entnommener zusätzlicher, flüssiger Sauerstoff durch Pumpen auf zumindest einen zweiten Verdampfungsdruck verdichtet und bei diesem oder diesen Drücken in der Wärmeaustauschleitung (2) verdampft wird.
  5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß flüssiger Stickstoff der Doppelkolonne (1) entnommen, durch Pumpen (10, 11) auf zumindest einen Stickstoffverdampfungsdruck verdichtet und bei diesem oder diesen Drücken in der Wärmeaustauschleitung (2) verdampft wird.
  6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß zumindest ein Teil der aus der ersten (7) oder der zweiten (8) Turbine ausgetretenen Luft in einer dritten Turbine (30) auf den niedrigen Druck entspannt und die aus der dritten Turbine ausgetretene Luft in die Niederdruckkolonne (13) oder in das aus dem oberen Teil dieser Kolonne ausgeleitete Restgas eingeleitet wird.
  7. Verfahren nach Anspruch 6, dadurch gekennzeichnet, daß in der dritten Turbine (30) die gesamte aus der ersten (7) oder zweiten (8) Turbine ausgetretene Luft, wobei diese sich im wesentlichen auf dem mittleren Druck befindet, sowie eine am Sumpf der Mitteldruckkolonne (12) entnommene Zusatzluftmenge entspannt werden.
  8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß die Luft mittels zumindest zwei aufeinanderfolgend angeordneten Verdichtern (4, 5, 32) nachverdichtet wird, die jeweils mit einer der Turbinen (7, 8, 30) gekuppelt sind.
  9. Zur Herstellung gasförmigen Sauerstoffs unter Druck dienende Vorrichtung zur Anwendung eines Verfahrens gemäß einem der Ansprüche 1 bis 8, umfassend eine Doppelkolonne (1) zur Destillation von Luft mit einer als Niederdruckkolonne (13) bezeichneten, unter einem ersten Druck arbeitenden Kolonne und einer als Mitteldruckkolonne (12) bezeichneten, unter einem mittleren Druck arbeitenden Kolonne, eine Pumpe (9, 10) zum Verdichten flüssigen, am Sumpf der Niederdruckkolonne (13) entnommenen Sauerstoffs, Verdichtermittel (3, 4, 5, 32) zum Bringen der zu destillierenden Luft auf einen hohen Luftdruck deutlich größer als der mittlere Druck, und eine Wärmeaustauschleitung (2) zum Herstellen einer Wärmeaustauschbeziehung zwischen der Luft auf dem hohen Druck und dem verdichteten, flüssigen Sauerstoff, wobei die Verdichtermittel einen Verdichter (3) zum Bringen der gesamten, zu destillierenden Luft auf einen ersten hohen Druck P1 deutlich größer als der mittlere Druck und Mittel (4, 5, 32) zum Nachverdichten eines Teils der Luft unter diesem ersten hohen Druck bis auf einen zweiten hohen Druck umfassen,
    dadurch gekennzeichnet, daß diese Nachverdichtermittel zumindest zwei aufeinanderfolgend angeordnete, jeweils mit einer Entspannungsturbine (7, 8, 30) gekuppelte Verdichter umfassen, wobei ein Verdichter (4, 5) mit einer ersten Turbine (7) zur Entspannung von Luft unter dem ersten hohen Druck P1 und ein weiterer Verdichter (5; 4) mit einer zweiten Turbine (8) zur Entspannung eines Teils der nachverdichteten Luft gekuppelt sind, und dadurch, daß die Wärmeaustauschleitung (2) Abschnitte zur Kühlung der aus der ersten, die höhere Einlaßtemperatur besitzenden Turbine (7) ausgetretenen Luft aufweist und/oder die Einlaßtemperatur T1 der einen (7) der beiden Turbinen zwischen etwa 0°C und -60°C liegt, während die Einlaßtemperatur T2 der zweiten Turbine (8) zwischen etwa -80°C und -130°C beträgt.
  10. Vorrichtung nach Anspruch 9, gekennzeichnet durch eine zweite Pumpe (10) für flüssigen Sauerstoff oder flüssigen Stickstoff und eventuell eine dritte Pumpe (11) für flüssigen Sauerstoff oder flüssigen Stickstoff, und dadurch, daß die Wärmeaustauschleitung (2) entsprechende Verdampfer-Erwärmer-Abschnitte umfaßt.
  11. Vorrichtung nach einem der Ansprüche 9 oder 10, gekennzeichnet durch eine dritte Turbine (30) zur Entspannung zumindest eines Teils der aus der Turbine (7) mit der höheren Einlaßtemperatur ausgetretenen Luft auf den niedrigen Druck, und Mittel zum Einleiten der aus der dritten Turbine ausgetretenen Luft in die Niederdruckkolonne (13) oder in eine Leitung mit aus dieser Kolonne stammendem Restgas.
  12. Vorrichtung nach Anspruch 11, gekennzeichnet durch Mittel (33), die die Speisegasversorgung der dritten Turbine (30) durch am Sumpf der Mitteldruckkolonne (12) entnommene Luft vervollständigen, wobei die aus der Turbine (7) mit der höheren Einlaßtemperatur ausgetretene Luft im wesentlichen den mittleren Druck hat.
  13. Vorrichtung nach einem der Ansprüche 11 und 12, dadurch gekennzeichnet, daß die dritte Turbine (30) durch einen Generator (31) oder durch einen Luftverdichter (32) gebremst wird.
  14. Vorrichtung nach Anspruch 13, dadurch gekennzeichnet, daß der mit der dritten Turbine (30) gekuppelte Verdichter (32) in Reihe mit den anderen Verdichtern (4, 5) angeordnet ist.
EP93401395A 1992-06-23 1993-06-02 Verfahren und Apparat zur Herstelling von gasförmigem Sauerstoff unter Druck Expired - Lifetime EP0576314B2 (de)

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FR9207662 1992-06-23
FR9207662A FR2692664A1 (fr) 1992-06-23 1992-06-23 Procédé et installation de production d'oxygène gazeux sous pression.

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DE10024708B4 (de) * 1999-05-21 2007-10-25 Kabushiki Kaisha Kobe Seiko Sho, Kobe Verfahren zur Herstellung von Sauerstoffgas
DE10106480B4 (de) * 2000-02-23 2008-01-31 Kabushiki Kaisha Kobe Seiko Sho, Kobe Verfahren zur Herstellung von Sauerstoff

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CA2098895A1 (fr) 1993-12-24
FR2692664A1 (fr) 1993-12-24
US5400600A (en) 1995-03-28
DE69305246T2 (de) 1997-05-07
EP0576314A1 (de) 1993-12-29
JPH0658662A (ja) 1994-03-04
CN1080390A (zh) 1994-01-05
DE69305246D1 (de) 1996-11-14
AU660260B2 (en) 1995-06-15
CN1077275C (zh) 2002-01-02
ZA934204B (en) 1994-01-10
DE69305246T3 (de) 2001-03-08
AU4135793A (en) 1994-01-06
EP0576314B1 (de) 1996-10-09

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