EP0576314B2 - Procédé et installation de production d'oxygène gazeux sous pression - Google Patents
Procédé et installation de production d'oxygène gazeux sous pression Download PDFInfo
- 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
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- Prior art keywords
- air
- pressure
- turbine
- column
- oxygen
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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
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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
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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
- F25J3/0409—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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- 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
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- 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
- 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
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- 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
- 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
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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
- F25J3/04248—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
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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
- F25J3/04248—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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- 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
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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
- F25J3/04406—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
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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
- F25J3/04642—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
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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
- 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
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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
- 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
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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
- 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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- 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.
Description
- la première partie de cet air est refroidie jusqu'à une première température intermédiaire T1, où une première fraction est détendue dans une première turbine, tandis que le reste est refroidi et liquéfié, détendu et introduit dans la colonne moyenne pression ;
- la deuxième partie est refroidie jusqu'à une seconde
température intermédiaire T2, où un premier débit est détendu dans une
seconde turbine, tandis que le reste de cette deuxième partie est refroidi et
liquéfié, détendu et introduit dans la colonne moyenne pression ;
- éventuellement la pression d'échappement de l'une des turbines est réglée à une pression P3 comprise entre ladite première haute pression P1 et la moyenne pression,
- et l'oxygène comprimé se vaporise par condensation d'air à une ou plusieurs des pressions P1, P2, P3.
- les températures intermédiaires T1 et T2 sont choisies l'une entre 0°C et -60°C environ et l'autre entre -80°C et -130°C environ ;
- le débit d'air alimentant la turbine chaude est de l'ordre de 20 à 30 % du débit d'air traité ;
- l'oxygène liquide additionnel soutiré de la colonne basse pression est comprimé par pompe à au moins une seconde pression de vaporisation et vaporisé à cette ou à ces pressions dans la ligne d'échange thermique ;
- l'azote liquide est soutiré de la double colonne, comprimé par pompe à au moins une pression de vaporisation d'azote, et vaporisé à cette ou à ces pressions dans la ligne d'échange thermique ;
- on détend à la basse pression dans une troisième turbine une partie au moins de l'air issu de la première ou de la seconde turbine, l'air issu de la troisième turbine étant introduit dans la colonne basse pression ou dans le gaz résiduaire évacué de la partie supérieure de cette colonne ;
- on détend dans la troisième turbine la totalité dudit air issu de la première ou de la deuxième turbine, cet air se trouvant sensiblement à la moyenne pression, ainsi qu'un débit complémentaire d'air soutiré en cuve de la colonne moyenne pression ;
- la surpression de l'air est réalisée au moyen d'au moins deux soufflantes en série couplées chacune à l'une des turbines.
caractérisée en ce que ces moyens de surpression comprennent au moins deux soufflantes en série couplées chacune à une turbine de détente, une soufflante étant couplée à une turbine de détente d'air sous la première haute pression P1 et une autre soufflante étant couplée à une seconde turbine de détente d'une partie de l'air surpressé, et en ce que la ligne d'échange thermique comprend des passages de refroidissement de l'air issu de la turbine ayant la plus haute température d'admission et/ou la température T1 d'admission de l'une des deux turbines est comprise entre 0°C et 60°C environ, tandis que celle T2 de l'autre turbine est comprise entre -80°C et -130°C.
- la figure 1 représente schématiquement une installation de production d'oxygène gazeux conforme à l'invention ;
- la figure 2 est un diagramme d'échange thermique, obtenu par calcul, correspondant à cette installation ; et
- les figures 3 et 4 représentent schématiquement deux autres modes de réalisation de l'installation suivant l'invention.
- l'azote gazeux basse pression issu du sommet de la colonne 13, et l'azote impur ou "waste" produit par cette même colonne, ces deux gaz parcourant la ligne d'échange de son bout froid à son bout chaud, puis étant évacués via des conduites respectives 24 et 25.
- la majeure partie de l'oxygène séparé est soutirée en cuve de la colonne 13 sous forme liquide, amenée à une première pression PO1, relativement basse, par la pompe 9, vaporisée en condensant de l'air soit à la pression P1, ce qui correspond à PO1 = 11 à 17 bars, soit à la pression P2, ce qui correspond à PO1 = 17 à 22 bars, réchauffée à la température ambiante puis évacuée en tant que produit via une conduite 26;
- une autre partie de l'oxygène séparé, que l'on désire, dans cet exemple, produire sous forme gazeuse à une seconde pression PO2, relativement élevée, typiquement comprise entre 11 et 60 bars, soutirée en cuve de la colonne 13 sous forme liquide, amenée à cette seconde pression PO2, vaporisée dans la ligne d'échange par prélèvement de chaleur sur l'air, sans que cette vaporisation soit nécessairement concomitante à la condensation de cet air, puis réchauffée à la température ambiante et évacuée en tant que produit via une conduite 27; et
- de l'azote, que l'on désire, dans cet exemple, produire sous forme gazeuse sous une pression de l'ordre de 5 à 60 bars et de préférence de 25 à 35 bars, soutiré sous forme liquide en tête de la colonne 12, amené par la pompe 11 à cette pression de production, vaporisé dans la ligne d'échange par prélèvement de chaleur sur l'air sans que cette vaporisation soit nécessairement concomitante à la condensation de cet air, réchauffé à la température ambiante, et évacué en tant que produit via une conduite 28.
- débit d'air traité : 26.000 Nm2/h
- P1 = 27,5 bars, P2 = 39,5 bars
- T1 = - 35°C, T2 = - 122°C
- la production d'oxygène gazeux est répartie en deux tiers à 12 bars (conduite 26) et un tiers à 42 bars (conduite 27)
- l'installation produit également 1.600 Nm2/h d'azote gazeux pur sous 42 bars (conduite 28), et 1.900 Nm2/h de liquide.
- la turbine basse pression 30 est freinée par une troisième soufflante 32, dont la roue est rigidement accouplée à celle de cette turbine et qui est montée en série avec les soufflantes 4 et 5, en amont de celles-ci;
- le débit à détendre dans la turbine 30 est supérieur à celui détendu dans la turbine 7. Par suite, la turbine 30 est alimentée d'une part par la totalité de l'air moyenne pression issu de la turbine 7, d'autre part par un complément d'air moyenne pression provenant de la colonne 12 via une conduite 33 et réchauffé dans la ligne d'échange jusqu'à la température convenable;
- seule la pompe 9 est affectée à l'oxygène, qui est donc produit sous une seule pression et vaporisé en totalité par condensation d'air à l'une des trois pressions disponibles (P1, P2 et la moyenne pression), tandis que les pompes 10 et 11 sont affectées à l'azote, qui est ainsi produit sous deux pressions différentes et, également, vaporisé par condensation d'air.
Claims (14)
- Procédé de production d'oxygène gazeux sous pression par distillation d'air dans une installation comprenant une ligne d'échange thermique (2) et une double colonne de distillation (1) qui comporte elle-même une première colonne (12), dite colonne moyenne pression, fonctionnant sous une moyenne pression, et une seconde colonne (13), dite colonne basse pression, fonctionnant sous une basse pression, pompage (en 9, 10) d'oxygène liquide soutiré en cuve de la colonne basse pression, et vaporisation de l'oxygène comprimé par échange de chaleur avec de l'air comprimé à une haute pression d'air, la totalité de l'air à traiter étant comprimée à une première pression P1 nettement supérieure à la moyenne pression, l'air à la pression P1 est divisé en seulement deux parties, la première étant refroidie et la deuxième partie étant surpressée à une seconde haute pression P2 et refroidie, la majeure partie au moins de l'oxygène séparé étant soutirée à l'état liquide de la colonne basse pression (13), comprimée par une pompe (9, 10) à au moins une première pression de vaporisation à laquelle il se vaporise par condensation d'air et vaporisée par condensation d'air,
caractérisé en ce que :la première partie de cet air est refroidie jusqu'à une première température intermédiaire T1, où une première fraction est détendue dans une première turbine (7), tandis que le reste de cette deuxième partie est refroidi et liquéfié, détendu et introduit dans la colonne moyenne pression (12) ;la deuxième partie est refroidie jusqu'à une seconde température intermédiaire T2, où un premier débit est détendu dans une seconde turbine (8), tandis que le reste de cette première partie est refroidi et liquéfié, détendu et introduit dans la colonne moyenne pression (12) ;éventuellement la pression d'échappement de l'une des turbines (7, 8) est réglée à une pression P3 comprise entre ladite première haute pression P1 et la moyenne pression,et l'oxygène comprimé se vaporise par condensation d'air à une ou plusieurs des pressions P1, P2, P3. - Procédé selon la revendication 1, caractérisé en ce que les températures intermédiaires T1 et T2 sont choisies l'une entre 0°C et -60°C environ et l'autre entre -80°C et -130°C environ.
- Procédé selon l'une des revendications 1 ou 2, caractérisé en ce que le débit d'air alimentant la première turbine (7) est de l'ordre de 20 à 30 % du débit d'air traité.
- Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que de l'oxygène liquide additionnel soutiré de la colonne basse pression (13) est comprimé par pompe à au moins une seconde pression de vaporisation et vaporisé à cette ou à ces pressions dans la ligne d'échange thermique (2).
- Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que de l'azote liquide est soutiré de la double colonne (1), comprimé par pompe (10, 11) à au moins une pression de vaporisation d'azote, et vaporisé à cette ou à ces pressions dans la ligne d'échange thermique (2).
- Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'on détend à la basse pression dans une troisième turbine (30) une partie au moins de l'air issu de la première ou de la seconde turbine (7, 8), l'air issu de la troisième turbine étant introduit dans la colonne basse pression (13) ou dans le gaz résiduaire évacué de la partie supérieure de cette colonne.
- Procédé selon la revendication 6, caractérisé en ce qu'on détend dans la troisième turbine (30) la totalité dudit air issu de la première ou de la deuxième turbine (7, 8), cet air se trouvant sensiblement à la moyenne pression, ainsi qu'un débit complémentaire d'air soutiré en cuve de la colonne moyenne pression (12).
- Procédé selon l'une quelconque des revendications 1 à 7, caractérisé en ce que la surpression de l'air est réalisée au moyen d'au moins deux soufflantes (4, 5, 32) en série couplées chacune à l'une des turbines (7, 8, 30).
- Installation de production d'oxygène gazeux sous pression pour la mise en oeuvre d'un procédé selon l'une quelconque des revendications 1 à 8, du type comprenant une double colonne de distillation d'air (1) comprenant une colonne, dite colonne basse pression (13), fonctionnant sous une basse pression, et une colonne, dite colonne moyenne pression (12) fonctionnant sous une moyenne pression, une pompe (9, 10) de compression d'oxygène liquide soutiré en cuve de la colonne basse pression (13), des moyens de compression (3, 4, 5, 32) pour amener de l'air à distiller à une haute pression d'air nettement supérieure à la moyenne pression, et une ligne d'échange thermique (2) pour mettre en relation d'échange thermique l'air à la haute pression et l'oxygène liquide comprimé, les moyens de compression comprenant un compresseur (3) pour amener la totalité de l'air à distiller à une première haute pression P1 nettement supérieure à la moyenne pression, et des moyens (4, 5, 32) de surpression d'une fraction de l'air sous cette première haute pression jusqu'à une seconde haute pression P2,
caractérisée en ce que ces moyens de surpression comprennent au moins deux soufflantes en série couplées chacune à une turbine de détente (7, 8, 30), une soufflante (4, 5) étant couplée à une première turbine (7) de détente d'air sous la première haute pression P1 et une autre soufflante (5 ; 4) étant couplée à une seconde turbine (8) de détente d'une partie de l'air surpressé, et en ce que la ligne d'échange thermique (2) comprend des passages de refroidissement de l'air issu de la première turbine (7) ayant la plus haute température d'admission et/ou la température T1 d'admission de l'une (7) des deux turbines est comprise entre 0°C et -60°C environ, tandis que celle T2 de la deuxième turbine (8) est comprise entre -80°C et -130°C environ. - Installation selon la revendication 9, caractérisée en ce qu'elle comprend une deuxième pompe (10) d'oxygène liquide ou d'azote liquide, et éventuellement une troisième pompe (11) d'oxygène liquide ou d'azote liquide, et en ce que la ligne d'échange thermique (2) comporte des passages de vaporisation-réchauffement correspondants.
- Installation selon l'une des revendications 9 ou 10, caractérisée en ce qu'elle comprend une troisième turbine (30) de détente à la basse pression d'une partie au moins de l'air issu de la turbine (7) ayant la plus haute température d'admission, et des moyens pour introduire l'air issu de la troisième turbine dans la colonne basse pression (13) ou dans une conduite de gaz résiduaire de cette colonne.
- Installation selon la revendication 11, caractérisée en ce qu'elle comprend des moyens (33) pour compléter l'alimentation de la troisième turbine (30) avec de l'air soutiré en cuve de la colonne moyenne pression (12), ledit air issu de la turbine (7) ayant la plus haute température d'admission étant sensiblement à la moyenne pression.
- Installation selon l'une des revendications 11 et 12 dans laquelle la troisième turbine (30) est freinée par un alternateur (31) ou par une soufflante (32) d'air.
- Installation selon la revendication 13, dans laquelle la soufflante (32) couplée à la troisième turbine (30) est montée en série avec les autres soufflantes (4, 5).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9207662A FR2692664A1 (fr) | 1992-06-23 | 1992-06-23 | Procédé et installation de production d'oxygène gazeux sous pression. |
FR9207662 | 1992-06-23 |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0576314A1 EP0576314A1 (fr) | 1993-12-29 |
EP0576314B1 EP0576314B1 (fr) | 1996-10-09 |
EP0576314B2 true EP0576314B2 (fr) | 2000-03-29 |
Family
ID=9431071
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP93401395A Expired - Lifetime EP0576314B2 (fr) | 1992-06-23 | 1993-06-02 | Procédé et installation de production d'oxygène gazeux sous pression |
Country Status (9)
Country | Link |
---|---|
US (1) | US5400600A (fr) |
EP (1) | EP0576314B2 (fr) |
JP (1) | JPH0658662A (fr) |
CN (1) | CN1077275C (fr) |
AU (1) | AU660260B2 (fr) |
CA (1) | CA2098895A1 (fr) |
DE (1) | DE69305246T3 (fr) |
FR (1) | FR2692664A1 (fr) |
ZA (1) | ZA934204B (fr) |
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US6321566B1 (en) | 1999-05-21 | 2001-11-27 | Kabushiki Kaisha Kobe Seiko Sho. | Method for producing oxygen gas |
DE10106480B4 (de) * | 2000-02-23 | 2008-01-31 | Kabushiki Kaisha Kobe Seiko Sho, Kobe | Verfahren zur Herstellung von Sauerstoff |
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FR2723184B1 (fr) | 1994-07-29 | 1996-09-06 | Grenier Maurice | Procede et installation de production d'oxygene gazeux sous pression a debit variable |
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GB9521782D0 (en) * | 1995-10-24 | 1996-01-03 | Boc Group Plc | Air separation |
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GB9810587D0 (en) * | 1998-05-15 | 1998-07-15 | Cryostar France Sa | Pump |
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FR2831249A1 (fr) * | 2002-01-21 | 2003-04-25 | Air Liquide | Procede et installation de separation d'air par distillation cryogenique |
FR2853407B1 (fr) * | 2003-04-02 | 2012-12-14 | Air Liquide | Procede et installation de fourniture de gaz sous pression |
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EP1726900A1 (fr) * | 2005-05-20 | 2006-11-29 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et installation pour la séparation cryogénique d'air |
US7437890B2 (en) * | 2006-01-12 | 2008-10-21 | Praxair Technology, Inc. | Cryogenic air separation system with multi-pressure air liquefaction |
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FR2913759B1 (fr) * | 2007-03-13 | 2013-08-16 | Air Liquide | Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique. |
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FR2948184B1 (fr) * | 2009-07-20 | 2016-04-15 | Air Liquide | Procede et appareil de separation d'air par distillation cryogenique |
EP2963367A1 (fr) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable |
TR201808162T4 (tr) | 2014-07-05 | 2018-07-23 | Linde Ag | Havanın düşük sıcaklıkta ayrıştırılması vasıtasıyla bir basınçlı gaz ürününün kazanılmasına yönelik yöntem ve cihaz. |
US20160025408A1 (en) * | 2014-07-28 | 2016-01-28 | Zhengrong Xu | Air separation method and apparatus |
US20160245585A1 (en) | 2015-02-24 | 2016-08-25 | Henry E. Howard | System and method for integrated air separation and liquefaction |
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-
1992
- 1992-06-23 FR FR9207662A patent/FR2692664A1/fr not_active Withdrawn
-
1993
- 1993-06-02 DE DE69305246T patent/DE69305246T3/de not_active Expired - Fee Related
- 1993-06-02 EP EP93401395A patent/EP0576314B2/fr not_active Expired - Lifetime
- 1993-06-07 US US08/072,991 patent/US5400600A/en not_active Expired - Lifetime
- 1993-06-14 ZA ZA934204A patent/ZA934204B/xx unknown
- 1993-06-16 JP JP5144912A patent/JPH0658662A/ja active Pending
- 1993-06-18 AU AU41357/93A patent/AU660260B2/en not_active Ceased
- 1993-06-21 CA CA002098895A patent/CA2098895A1/fr not_active Abandoned
- 1993-06-22 CN CN93107602A patent/CN1077275C/zh not_active Expired - Fee Related
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6321566B1 (en) | 1999-05-21 | 2001-11-27 | Kabushiki Kaisha Kobe Seiko Sho. | Method for producing oxygen gas |
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 |
Also Published As
Publication number | Publication date |
---|---|
CN1080390A (zh) | 1994-01-05 |
ZA934204B (en) | 1994-01-10 |
CN1077275C (zh) | 2002-01-02 |
DE69305246D1 (de) | 1996-11-14 |
CA2098895A1 (fr) | 1993-12-24 |
EP0576314A1 (fr) | 1993-12-29 |
US5400600A (en) | 1995-03-28 |
EP0576314B1 (fr) | 1996-10-09 |
FR2692664A1 (fr) | 1993-12-24 |
JPH0658662A (ja) | 1994-03-04 |
AU4135793A (en) | 1994-01-06 |
AU660260B2 (en) | 1995-06-15 |
DE69305246T3 (de) | 2001-03-08 |
DE69305246T2 (de) | 1997-05-07 |
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