EP1143216B1 - Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation - Google Patents

Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation Download PDF

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Publication number
EP1143216B1
EP1143216B1 EP01400749A EP01400749A EP1143216B1 EP 1143216 B1 EP1143216 B1 EP 1143216B1 EP 01400749 A EP01400749 A EP 01400749A EP 01400749 A EP01400749 A EP 01400749A EP 1143216 B1 EP1143216 B1 EP 1143216B1
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EP
European Patent Office
Prior art keywords
column
argon
flow
enriched
oxygen
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
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EP01400749A
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German (de)
French (fr)
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EP1143216A1 (en
Inventor
Benoît DAVIDIAN
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
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
    • F25J3/04248—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.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04006—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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04127—Gas turbine as the prime mechanical driver
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    • 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
    • F25J3/04309—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 nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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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    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
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    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
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    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
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    • 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
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    • 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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    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
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    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

Definitions

  • the present invention relates to a process and apparatus for producing an oxygen-enriched fluid by cryogenic distillation of a mixture containing nitrogen, oxygen and argon, according to the preambles of claims 1 and 12 respectively and as of document EP-A-0 795 728 .
  • it relates to a method and apparatus for separating air by cryogenic distillation allowing the production of pure oxygen, ie oxygen containing at least 95 mol%. oxygen, preferably at least 98 mol%. of oxygen or even 99.5 mol%. oxygen.
  • the patent application EP-A-0540900 discloses a process for producing impure oxygen in which a portion of the impure argon containing at least 90% argon of a mixture column is mixed with the residual nitrogen of a double column.
  • the mixture column operates at the same low pressure as the low pressure column, up to 1.75 bara.
  • EP-A-0384213 has a low pressure column operating at between 1.5 and 10 bara but the argon column operates at a lower pressure.
  • US Patent 4932212 describes the case in which the low pressure column and the argon column operate at pressures between 1 and 2 bars.
  • EP-A-0518491 discloses a process for producing nitrogen gas under pressure and incidentally liquid nitrogen, liquid argon and liquid oxygen in which the low pressure column and the argon column operate at a substantially identical pressure above 2.5 bara. No flow of argon gas is produced.
  • EP-A-0952415 describes an apparatus comprising a double column and an argon column operating with a yield lower than the optimal yield.
  • An object of the present invention is to increase the pure oxygen yield of an air separation apparatus.
  • Another object of the invention is to provide an air separation apparatus particularly well suited to the demands of large quantities of nitrogen under pressure (typically in the case of integration with a gas turbine of a IGCC).
  • the flow enriched in argon or optionally the flow enriched in argon mixed with a gas enriched in nitrogen is sent upstream of the expansion machine of a gas turbine.
  • the flow enriched with argon may contain between 10 and 95 mol%. argon (or between 40 and 95 mol% of argon), between 2 and 40 mol% of oxygen and between 2 and 40 mol%. nitrogen.
  • argon production for example by withdrawing a flow richer in argon from the auxiliary column which is the product.
  • the argon enriched flow that is sent upstream of the expansion machine of a gas turbine can constitute between 0.3 and 2% of the air, preferably between 0.5 and 1% of the air. For this reason, it is preferable to mix the argon-enriched flow with a nitrogen-enriched gas containing at least 90 mol%. nitrogen from eg the low pressure column of a double column and use the mixture in a gas turbine and currently relax the mixture in a turbine.
  • the mixture formed comprises less than 2 mol%. argon, preferably less than 1 mol%. argon.
  • the low pressure column can operate between 2 and 10 bara, preferably above 2.5 bara.
  • the apparatus may comprise an auxiliary flow separation column containing at least argon and oxygen and two other columns, including a high pressure column and a low pressure column thermally connected to each other, auxiliary column being fed from the low pressure column.
  • the apparatus may comprise an auxiliary flow separation column containing at least argon and oxygen and at least three other columns, including a high pressure column, an intermediate pressure column and a low pressure column connected. thermally between them, the auxiliary column being fed from the low pressure column or the intermediate pressure column.
  • an integrated air separation and energy production method comprising a method according to claim 1, in which a nitrogen-enriched gas is sent from the column preferably operating at the pressure a. lower to the gas turbine, after a possible compression step and optionally sends an oxygen-enriched fluid from a column of the apparatus to a gasifier.
  • the auxiliary column contains between 30 and 40 theoretical plates.
  • the separation of oxygen and argon in the bottom of the low pressure column is facilitated.
  • the fluid enriched with argon withdrawn from the auxiliary column is not necessarily an end product of the apparatus but can be used to cool the flow rates entering the columns or to provide frigories by expansion.
  • an air flow 1 of 1000 Nm 3 / h is purified by adsorbent beds 4 and is divided in two.
  • the flow 2 is supercharged at a higher pressure, sent into the heat exchanger 3 where it cools by vaporizing the liquid oxygen and then to a hydraulic turbine 5 from which it comes out in at least partially liquid form .
  • This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly to the low pressure column 11 operating between 4 and 6 bar (or even between 2 and 10 bar), or sending a portion of the liquid of a capacity upstream of the medium pressure column or by withdrawing a flow rate having a composition similar to that of the liquid air of the high pressure column 9, as shown in FIG. figure 1 .
  • the apparatus may include an insufflation turbine which serves during startup. It comprises a low pressure nitrogen turbine 55.
  • a rich liquid flow 15 is withdrawn from the high pressure column and sent to the subcooler 17, divided in two and sent partly to the low pressure column, after expansion in the valve 21 and in part to the top condenser 23 of the column after the expansion in the valve 27.
  • the rich liquid at least partially vaporized in the overhead condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the column. low pressure.
  • a nitrogen gas flow rate 19 may optionally be withdrawn from the top of the high pressure column 9.
  • the auxiliary column is fed with a gas flow 29 containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • the vessel liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.
  • the auxiliary column 25 may alternatively be fed with a liquid flow rate containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • column 25 will have a bottom reboiler heated by a gas flow such as air or nitrogen from the high pressure column 9.
  • a liquid air flow 33 and a low liquid flow rate 35 are sent from the high pressure column 9 to the low pressure column 11, after having been subcooled in the subcooler 17 and expanded in valves.
  • a flow of liquid oxygen 37 containing 99.5 mol%. oxygen is withdrawn in the bottom of the low pressure column, pressurized by a pump 39 and vaporized in the exchanger 3.
  • An argon-enriched gas 49 constituting between 0.5 and 1% of the air supplied to the apparatus and containing between 40 and 95 mol%.
  • Argon withdrawn from the head of the auxiliary column 25 is mixed with residual nitrogen 47 from the head of the low pressure column.
  • the mixture 54 heats up in the subcooler 17 and then warms up in the exchanger 3.
  • the mixture is then sent upstream of the expansion machine 51 of a gas turbine after a compression step.
  • the process of the Figure 1 can increase the oxygen yield from 78% to 90%.
  • a triple column is used instead of the double column of the Figure 1 .
  • An air flow 1 is purified by adsorbent beds 4 and is divided in two.
  • the flow 2 is supercharged at a higher pressure, sent into the heat exchanger 3 where it cools by vaporizing the liquid oxygen and then to a hydraulic turbine 5 from which it comes out in at least partially liquid form .
  • This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly to the low pressure column 11 operating between 4 and 6 bar and / or optionally to the intermediate pressure column 40 operating between 7 and 9 bar, either by sending a portion of the liquid of a capacity upstream of the medium pressure column or by withdrawing a flow rate having a composition similar to that of the liquid air of the high pressure column 9, as shown in FIG. figure 2 .
  • the apparatus may include an insufflation turbine which serves during startup. It comprises a low pressure nitrogen turbine 55.
  • a rich liquid flow 15 is withdrawn from the high pressure column and sent to the subcooler 17, divided in two and sent partly to the middle of the column operating at intermediate pressure 40, after expansion in the valve 21 and partly to the condenser of head 23 of the auxiliary column 25 after expansion in the valve 27.
  • the rich liquid at least partially vaporized in the head condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the low pressure column.
  • a nitrogen gas flow rate 19 may optionally be withdrawn from the top of the high pressure column 9.
  • the auxiliary column is fed with a portion of a gas flow 29 containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • the vessel liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.
  • the auxiliary column 25 may alternatively be fed with a liquid flow rate containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon.
  • column 25 will have a bottom reboiler heated by a gas flow such as air or nitrogen from the high pressure column 9.
  • the remainder of the gas flow 29 serves to heat the bottom reboiler 41 of the column 40 and after condensation is returned to the low pressure column with the flow 31.
  • the tank liquid 43 of the column 40 is sent partly directly to the low pressure column and partly to the top condenser of the column 40 where it is vaporizes at least partially before being sent to the low pressure column in turn.
  • the overhead liquid 47 of the column 40 is undercooled in the exchanger 17, expanded, mixed with the expanded flow 35 and sent to the top of the low pressure column.
  • a liquid air flow 33 and a low liquid flow rate 35 are sent from the high pressure column 9 to the low pressure column 11, after having been subcooled in the subcooler 17 and expanded in valves.
  • a flow of liquid oxygen 37 containing 99.5 mol%. oxygen is withdrawn in the bottom of the low pressure column, pressurized by a pump 39 and vaporized in the exchanger 3.
  • An argon-enriched gas 49 constituting between 0.5 and 1% of the air supplied to the apparatus and containing between 40 and 95 mol%.
  • Argon withdrawn from the head of the auxiliary column 25 is mixed with residual nitrogen 47 from the head of the low pressure column.
  • the mixture 54 heats up in the subcooler 17 and then warms up in the exchanger 3.
  • the mixture is then sent upstream of the expansion machine 51 of a gas turbine after a possible compression step.
  • the process according to the invention is of particular interest in the case in which the nitrogen of the low pressure column is upgraded, by sending it to an expansion machine 51 of a gas turbine.
  • at least part of the air 1 can come from the compressor 53 of the gas turbine and the oxygen produced by the distillation apparatus can be used for the gasification necessary to produce the fuel of the gas turbine.

Abstract

Cryogenic distillation enables pure oxygen (95% minimum) to be obtained from a mixture containing nitrogen, oxygen and argon. The production of an oxygen (O2)-enriched flow in a cryogenic distillation unit comprises the following stages: (a) cooling of a supply (1) containing O2, nitrogen (N2) and argon (Ar) and introduction in a distillation unit comprising an auxiliary column (25) for the separation of a flow (29) containing Ar and O2, the unit comprising two other columns (9,18); (b) separation of the flow to form fluids enriched in O2 and N2 (15,33); (c) conveyance of the flow containing Ar and O2 from one of the columns (18) to the auxiliary column, both operating at 2-10 bars; (d) withdrawal of an O2-enriched flow (37) containing at least 95% mol of O2; and (e) withdrawal of an Ar-enriched flow (49) from the auxiliary column. Part of the Ar-enriched flow is rejected to atmosphere and/or acts as an adsorbent bed (4) regenerator and/or part may be mixed with an N2-enriched gas (47) from the unit, or from another unit. An Independent claim is also included for the apparatus for the above process.

Description

La présente invention est relative à un procédé et à un appareil de production d'un fluide enrichi en oxygène par distillation cryogénique d'un mélange contenant de l'azote, de l'oxygène et de l'argon, conformément aux préambules des revendications 1 et 12 respectivement et comme du document EP-A-0 795 728 .The present invention relates to a process and apparatus for producing an oxygen-enriched fluid by cryogenic distillation of a mixture containing nitrogen, oxygen and argon, according to the preambles of claims 1 and 12 respectively and as of document EP-A-0 795 728 .

En particulier il concerne un procédé et à un appareil de séparation d'air par distillation cryogénique permettant la production d'oxygène pur, c'est à dire de l'oxygène contenant au moins 95% mol. oxygène, de préférence au moins 98% mol. d'oxygène ou même 99,5% mol. d'oxygène.In particular, it relates to a method and apparatus for separating air by cryogenic distillation allowing the production of pure oxygen, ie oxygen containing at least 95 mol%. oxygen, preferably at least 98 mol%. of oxygen or even 99.5 mol%. oxygen.

Lorsqu'on veut faire de l'oxygène pur, on doit nécessairement séparer l'oxygène de l'argon. Si les colonnes de l'appareil opèrent toutes à une pression au-dessus de 2 bar, la distillation est difficile.When one wants to make pure oxygen, one must necessarily separate oxygen from argon. If the columns of the apparatus all operate at a pressure above 2 bar, distillation is difficult.

La production d'argon pur nécessite une colonne ayant plus que 100 plateaux théoriques.Pure argon production requires a column with more than 100 theoretical plates.

La demande de brevet EP-A-0540900 décrit un procédé de production d'oxygène impur dans lequel une partie de l'argon impur contenant au moins 90% d'argon d'une colonne de mixture est mélangé avec l'azote résiduaire d'une double colonne. La colonne de mixture opère à la même pression basse que la colonne basse pression, jusqu'à 1,75 bara.The patent application EP-A-0540900 discloses a process for producing impure oxygen in which a portion of the impure argon containing at least 90% argon of a mixture column is mixed with the residual nitrogen of a double column. The mixture column operates at the same low pressure as the low pressure column, up to 1.75 bara.

EP-A-0384213 a une colonne basse pression opérant à entre 1,5 et 10 bara mais la colonne argon opère à une pression plus basse. EP-A-0384213 has a low pressure column operating at between 1.5 and 10 bara but the argon column operates at a lower pressure.

US-A-4932212 décrit le cas dans lequel la colonne basse pression et la colonne argon opèrent à des pressions entre 1 et 2 bars. US Patent 4932212 describes the case in which the low pressure column and the argon column operate at pressures between 1 and 2 bars.

EP-A-0518491 décrit un procédé de production d'azote gazeux sous pression et accessoirement de l'azote liquide, de l'argon liquide et de l'oxygène liquide dans lequel la colonne basse pression et la colonne argon opèrent à une pression substantiellement identique au-dessus de 2,5 bara. Aucun débit d'argon gazeux n'est produit. EP-A-0518491 discloses a process for producing nitrogen gas under pressure and incidentally liquid nitrogen, liquid argon and liquid oxygen in which the low pressure column and the argon column operate at a substantially identical pressure above 2.5 bara. No flow of argon gas is produced.

EP-A-0952415 décrit un appareil comprenant une double colonne et une colonne argon opérant avec un rendement inférieur au rendement optimal. EP-A-0952415 describes an apparatus comprising a double column and an argon column operating with a yield lower than the optimal yield.

Un but de la présente invention est d'augmenter le rendement en oxygène pur d'un appareil de séparation d'air.An object of the present invention is to increase the pure oxygen yield of an air separation apparatus.

Un autre but de l'invention est de fournir un appareil de séparation d'air particulièrement bien adapté aux demandes de grandes quantités d'azote sous pression (typiquement en cas d'intégration avec une turbine à gaz d'un IGCC).Another object of the invention is to provide an air separation apparatus particularly well suited to the demands of large quantities of nitrogen under pressure (typically in the case of integration with a gas turbine of a IGCC).

Selon un objet de l'invention, il est prévu un procédé selon la revendication 1.According to one object of the invention, there is provided a method according to claim 1.

Selon l'invention le débit enrichi en argon ou éventuellement le débit enrichi en argon mélangé avec un gaz enrichi en azote est envoyé en amont de la machine de détente d'une turbine à gaz.According to the invention, the flow enriched in argon or optionally the flow enriched in argon mixed with a gas enriched in nitrogen is sent upstream of the expansion machine of a gas turbine.

Le débit enrichi en argon peut contenir entre 10 et 95 % mol. d'argon (ou entre 40 et 95% mol. d'argon) ,entre 2 et 40% mol d'oxygène et entre 2 et 40 % mol. d'azote.The flow enriched with argon may contain between 10 and 95 mol%. argon (or between 40 and 95 mol% of argon), between 2 and 40 mol% of oxygen and between 2 and 40 mol%. nitrogen.

Dans ce cas, il peut tout de même y avoir une production d'argon, par exemple en soutirant un débit plus riche en argon de la colonne auxiliaire qui est le produit.In this case, there may still be an argon production, for example by withdrawing a flow richer in argon from the auxiliary column which is the product.

Le débit enrichi en argon qui est envoyé en amont de la machine de détente d'une turbine à gaz peut constituer entre 0,3 et 2% de l'air, de préférence entre 0,5 et 1% de l'air. Pour cette raison, il est préférable de mélanger le débit enrichi en argon avec un gaz enrichi en azote contenant au moins 90 %mol. d'azote provenant par exemple de la colonne basse pression d'une double colonne et d'utiliser le mélange dans une turbine à gaz et actuellement de détendre le mélange dans une turbine. Ainsi le mélange formé comprend moins de 2 % mol. d'argon, de préférence moins de 1% mol. d'argon.The argon enriched flow that is sent upstream of the expansion machine of a gas turbine can constitute between 0.3 and 2% of the air, preferably between 0.5 and 1% of the air. For this reason, it is preferable to mix the argon-enriched flow with a nitrogen-enriched gas containing at least 90 mol%. nitrogen from eg the low pressure column of a double column and use the mixture in a gas turbine and currently relax the mixture in a turbine. Thus the mixture formed comprises less than 2 mol%. argon, preferably less than 1 mol%. argon.

La colonne basse pression peut opérer entre 2 et 10 bara, de préférence au-dessus de 2,5 bara.The low pressure column can operate between 2 and 10 bara, preferably above 2.5 bara.

Par exemple, l'appareil peut comprendre une colonne auxiliaire de séparation d'un débit contenant au moins de l'argon et de l'oxygène et deux autres colonnes, dont une colonne haute pression et une colonne basse pression reliées thermiquement entre elles, la colonne auxiliaire étant alimentée à partir de la colonne basse pression.For example, the apparatus may comprise an auxiliary flow separation column containing at least argon and oxygen and two other columns, including a high pressure column and a low pressure column thermally connected to each other, auxiliary column being fed from the low pressure column.

Alternativement l'appareil peut comprendre une colonne auxiliaire de séparation d'un débit contenant au moins de l'argon et de l'oxygène et au moins trois autres colonnes, dont une colonne haute pression, une colonne pression intermédiaire et une colonne basse pression reliées thermiquement entre elles, la colonne auxiliaire étant alimentée à partir de la colonne basse pression ou la colonne pression intermédiaire.Alternatively the apparatus may comprise an auxiliary flow separation column containing at least argon and oxygen and at least three other columns, including a high pressure column, an intermediate pressure column and a low pressure column connected. thermally between them, the auxiliary column being fed from the low pressure column or the intermediate pressure column.

Selon un autre objet de l'invention, il est prévu un procédé intégré de séparation d'air et de production d'énergie comprenant un procédé la revendication 1 dans lequel on envoie un gaz enrichi en azote de la colonne opérant préférablement à la pression la plus basse à la turbine à gaz ,après une étape éventuelle de compression et, éventuellement on envoie un fluide enrichi en oxygène d'une colonne de l'appareil à un gazéifieur.According to another object of the invention, there is provided an integrated air separation and energy production method comprising a method according to claim 1, in which a nitrogen-enriched gas is sent from the column preferably operating at the pressure a. lower to the gas turbine, after a possible compression step and optionally sends an oxygen-enriched fluid from a column of the apparatus to a gasifier.

Selon un autre objet de l'invention, il est prévu un appareil selon la revendication.According to another object of the invention, there is provided an apparatus according to the claim.

De préférence il n'y a pas de moyen de détente entre la colonne alimentant la colonne auxiliaire et la colonne auxiliaire.Preferably there is no detent means between the column supplying the auxiliary column and the auxiliary column.

Optionnellement la colonne auxiliaire contient entre 30 et 40 plateaux théoriques.Optionally the auxiliary column contains between 30 and 40 theoretical plates.

Ainsi avec une colonne auxiliaire opérant à la même pression que la colonne basse pression, et de préférence opérant à une pression au-dessus de 2 bar, la séparation d'oxygène et argon en cuve de la colonne basse pression est facilitée. Dans ce cas le fluide enrichi en argon soutiré de la colonne auxiliaire n'est pas nécessairement un produit final de l'appareil mais peut servir à refroidir les débits rentrant dans les colonnes ou à fournir des frigories par détente.Thus with an auxiliary column operating at the same pressure as the low pressure column, and preferably operating at a pressure above 2 bar, the separation of oxygen and argon in the bottom of the low pressure column is facilitated. In this case, the fluid enriched with argon withdrawn from the auxiliary column is not necessarily an end product of the apparatus but can be used to cool the flow rates entering the columns or to provide frigories by expansion.

L'invention sera décrite en plus de détail en se référant aux figures.

  • La figure 1 est un schéma d'un appareil de production d'oxygène selon l'invention utilisant une double colonne.
  • La figure 2 est un schéma d'un appareil de production d'oxygène selon l'invention utilisant une triple colonne.
The invention will be described in more detail with reference to the figures.
  • The figure 1 is a diagram of an oxygen production apparatus according to the invention using a double column.
  • The figure 2 is a diagram of an oxygen production apparatus according to the invention using a triple column.

Dans la figure 1, un débit d'air 1 de 1000Nm3/h est épuré par des lits d'adsorbants 4 et est divisé en deux. Le débit 2 est surpressé à une pression plus élevée, envoyé dans l'échangeur de chaleur 3 où il se refroidit en assurant la vaporisation de l'oxygène liquide et ensuite à une turbine hydraulique 5 d'où il sort sous forme au moins partiellement liquide. Ce liquide (ou mélange diphasique) 7 est envoyé à la colonne haute pression 9 opérant entre 14 et 15 bar et éventuellement en partie à la colonne basse pression 11 opérant entre 4 et 6 bar (ou même entre 2 et 10 bar), soit en envoyant une partie du liquide d'une capacité en amont de la colonne moyenne pression soit en soutirant un débit ayant une composition similaire à celle de l'air liquide de la colonne haute pression 9, comme montré à la figure 1.In the figure 1 , an air flow 1 of 1000 Nm 3 / h is purified by adsorbent beds 4 and is divided in two. The flow 2 is supercharged at a higher pressure, sent into the heat exchanger 3 where it cools by vaporizing the liquid oxygen and then to a hydraulic turbine 5 from which it comes out in at least partially liquid form . This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly to the low pressure column 11 operating between 4 and 6 bar (or even between 2 and 10 bar), or sending a portion of the liquid of a capacity upstream of the medium pressure column or by withdrawing a flow rate having a composition similar to that of the liquid air of the high pressure column 9, as shown in FIG. figure 1 .

Le reste de l'air 13 à 14,4 bara est envoyé à la colonne haute pression 9.The remainder of the air 13 to 14.4 bara is sent to the high pressure column 9.

Eventuellement l'appareil peut comporter une turbine d'insufflation qui sert pendant le démarrage. Il comporte une turbine d'azote basse pression 55.Optionally the apparatus may include an insufflation turbine which serves during startup. It comprises a low pressure nitrogen turbine 55.

Un débit de liquide riche 15 est soutiré de la colonne haute pression et envoyé au sous refroidisseur 17, divisé en deux et envoyé en partie à la colonne basse pression, après détente dans la vanne 21 et en partie au condenseur de tête 23 de la colonne auxiliaire 25 après détente dans la vanne 27. Le liquide riche au moins partiellement vaporisé dans le condenseur de tête est envoyé à la colonne basse pression 11. Si la vaporisation est partielle, un débit liquide et un débit gazeux sont envoyés du condenseur à la colonne basse pression.A rich liquid flow 15 is withdrawn from the high pressure column and sent to the subcooler 17, divided in two and sent partly to the low pressure column, after expansion in the valve 21 and in part to the top condenser 23 of the column after the expansion in the valve 27. The rich liquid at least partially vaporized in the overhead condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the column. low pressure.

Un débit d'azote gazeux 19 peut éventuellement être soutiré de la tête de la colonne haute pression 9.A nitrogen gas flow rate 19 may optionally be withdrawn from the top of the high pressure column 9.

La colonne auxiliaire est alimentée par un débit gazeux 29 contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Le liquide de cuve 31 de la colonne auxiliaire est renvoyé à la colonne basse pression qui opère substantiellement à la même pression que la colonne auxiliaire.The auxiliary column is fed with a gas flow 29 containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon. The vessel liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.

Le colonne auxiliaire 25 peut alternativement être alimentée par un débit liquide contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Dans ce cas la colonne 25 aura un rebouilleur de cuve, chauffe par un débit gazeux tel que l'air ou de l'azote de la colonne haute pression 9.The auxiliary column 25 may alternatively be fed with a liquid flow rate containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon. In this case column 25 will have a bottom reboiler heated by a gas flow such as air or nitrogen from the high pressure column 9.

Un débit d'air liquide 33 et un débit de liquide pauvre 35 sont envoyés de la colonne haute pression 9 à la colonne basse pression 11, après avoir été sous-refroidis dans le sous refroidisseur 17 et détendus dans des vannes.A liquid air flow 33 and a low liquid flow rate 35 are sent from the high pressure column 9 to the low pressure column 11, after having been subcooled in the subcooler 17 and expanded in valves.

Un débit d'oxygène liquide 37 contenant 99,5% mol. d'oxygène est soutiré en cuve de la colonne basse pression, pressurisé par une pompe 39 et vaporisé dans l'échangeur 3.A flow of liquid oxygen 37 containing 99.5 mol%. oxygen is withdrawn in the bottom of the low pressure column, pressurized by a pump 39 and vaporized in the exchanger 3.

Un gaz enrichi en argon 49 constituant entre 0,5 et 1% de l'air envoyé à l'appareil et contenant entre 40 et 95 % mol. d'argon soutiré de la tête de la colonne auxiliaire 25 est mélangé avec de l'azote résiduaire 47 de la tête de la colonne basse pression. Le mélange 54 se réchauffe dans le sous refroidisseur 17 puis se réchauffe dans l'échangeur 3. Le mélange est ensuite envoyé en amont de la machine de détente 51 d'une turbine à gaz après une étape de compression.An argon-enriched gas 49 constituting between 0.5 and 1% of the air supplied to the apparatus and containing between 40 and 95 mol%. Argon withdrawn from the head of the auxiliary column 25 is mixed with residual nitrogen 47 from the head of the low pressure column. The mixture 54 heats up in the subcooler 17 and then warms up in the exchanger 3. The mixture is then sent upstream of the expansion machine 51 of a gas turbine after a compression step.

Auparavant une partie du mélange 54 est détendue dans une turbine 55 (en pointillés).Previously a portion of the mixture 54 is expanded in a turbine 55 (dashed).

Par rapport à un système classique avec une colonne haute pression à 14,3 bara et une colonne basse pression à 4,8 bara mais sans colonne auxiliaire, le procédé de la Figure 1 permet d'augmenter le rendement en oxygène de 78% à 90%.Compared to a conventional system with a high pressure column at 14.3 bara and a low pressure column at 4.8 bara but without an auxiliary column, the process of the Figure 1 can increase the oxygen yield from 78% to 90%.

Dans la Figure 2, une triple colonne est utilisée à la place de la double colonne de la Figure 1. Un débit d'air 1 est épuré par des lits d'adsorbants 4 et est divisé en deux. Le débit 2 est surpressé à une pression plus élevée, envoyé dans l'échangeur de chaleur 3 où il se refroidit en assurant la vaporisation de l'oxygène liquide et ensuite à une turbine hydraulique 5 d'où il sort sous forme au moins partiellement liquide. Ce liquide (ou mélange diphasique) 7 est envoyé à la colonne haute pression 9 opérant entre 14 et 15 bar et éventuellement en partie à la colonne basse pression 11 opérant entre 4 et 6 bar et/ou éventuellement à la colonne pression intermédiaire 40 opérant entre 7 et 9 bar, soit en envoyant une partie du liquide d'une capacité en amont de la colonne moyenne pression soit en soutirant un débit ayant une composition similaire à celle de l'air liquide de la colonne haute pression 9, comme montré à la figure 2.In the Figure 2 , a triple column is used instead of the double column of the Figure 1 . An air flow 1 is purified by adsorbent beds 4 and is divided in two. The flow 2 is supercharged at a higher pressure, sent into the heat exchanger 3 where it cools by vaporizing the liquid oxygen and then to a hydraulic turbine 5 from which it comes out in at least partially liquid form . This liquid (or two-phase mixture) 7 is sent to the high pressure column 9 operating between 14 and 15 bar and possibly partly to the low pressure column 11 operating between 4 and 6 bar and / or optionally to the intermediate pressure column 40 operating between 7 and 9 bar, either by sending a portion of the liquid of a capacity upstream of the medium pressure column or by withdrawing a flow rate having a composition similar to that of the liquid air of the high pressure column 9, as shown in FIG. figure 2 .

Le reste de l'air 13 à 14,4 bara est envoyé à la colonne haute pression 9.The remainder of the air 13 to 14.4 bara is sent to the high pressure column 9.

Eventuellement l'appareil peut comporter une turbine d'insufflation qui sert pendant le démarrage. Il comporte une turbine d'azote basse pression 55.Optionally the apparatus may include an insufflation turbine which serves during startup. It comprises a low pressure nitrogen turbine 55.

Un débit de liquide riche 15 est soutiré de la colonne haute pression et envoyé au sous refroidisseur 17, divisé en deux et envoyé en partie au milieu de la colonne opérant à pression intermédiaire 40, après détente dans la vanne 21 et en partie au condenseur de tête 23 de la colonne auxiliaire 25 après détente dans la vanne 27. Le liquide riche au moins partiellement vaporisé dans le condenseur de tête est envoyé à la colonne basse pression 11. Si la vaporisation est partielle, un débit liquide et un débit gazeux sont envoyés du condenseur à la colonne basse pression.A rich liquid flow 15 is withdrawn from the high pressure column and sent to the subcooler 17, divided in two and sent partly to the middle of the column operating at intermediate pressure 40, after expansion in the valve 21 and partly to the condenser of head 23 of the auxiliary column 25 after expansion in the valve 27. The rich liquid at least partially vaporized in the head condenser is sent to the low pressure column 11. If the vaporization is partial, a liquid flow and a gas flow are sent from the condenser to the low pressure column.

Un débit d'azote gazeux 19 peut éventuellement être soutiré de la tête de la colonne haute pression 9.A nitrogen gas flow rate 19 may optionally be withdrawn from the top of the high pressure column 9.

La colonne auxiliaire est alimentée par une partie d'un débit gazeux 29 contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Le liquide de cuve 31 de la colonne auxiliaire est renvoyé à la colonne basse pression qui opère substantiellement à la même pression que la colonne auxiliaire.The auxiliary column is fed with a portion of a gas flow 29 containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon. The vessel liquid 31 of the auxiliary column is returned to the low pressure column which operates substantially at the same pressure as the auxiliary column.

Le colonne auxiliaire 25 peut alternativement être alimentée par un débit liquide contenant entre 5 et 15 % mol. d'argon, de préférence vers 7 % mol. d'argon. Dans ce cas la colonne 25 aura un rebouilleur de cuve, chauffe par un débit gazeux tel que l'air ou de l'azote de la colonne haute pression 9.The auxiliary column 25 may alternatively be fed with a liquid flow rate containing between 5 and 15 mol%. argon, preferably to 7 mol%. argon. In this case column 25 will have a bottom reboiler heated by a gas flow such as air or nitrogen from the high pressure column 9.

Le reste du débit gazeux 29 sert à chauffer le rebouilleur de cuve 41 de la colonne 40 et après condensation est renvoyé à la colonne basse pression avec le débit 31.The remainder of the gas flow 29 serves to heat the bottom reboiler 41 of the column 40 and after condensation is returned to the low pressure column with the flow 31.

Le liquide de cuve 43 de la colonne 40 est envoyé en partie directement à la colonne basse pression et en partie au condenseur de tête de la colonne 40 où il se vaporise au moins partiellement avant d'être envoyé à la colonne basse pression à son tour.The tank liquid 43 of the column 40 is sent partly directly to the low pressure column and partly to the top condenser of the column 40 where it is vaporizes at least partially before being sent to the low pressure column in turn.

Le liquide de tête 47 de la colonne 40 est sousrefroidi dans l'échangeur 17, détendu, mélangé avec le débit détendu 35 et envoyé en tête de la colonne basse pression.The overhead liquid 47 of the column 40 is undercooled in the exchanger 17, expanded, mixed with the expanded flow 35 and sent to the top of the low pressure column.

Un débit d'air liquide 33 et un débit de liquide pauvre 35 sont envoyés de la colonne haute pression 9 à la colonne basse pression 11, après avoir été sous-refroidis dans le sous refroidisseur 17 et détendus dans des vannes.A liquid air flow 33 and a low liquid flow rate 35 are sent from the high pressure column 9 to the low pressure column 11, after having been subcooled in the subcooler 17 and expanded in valves.

Un débit d'oxygène liquide 37 contenant 99,5% mol. d'oxygène est soutiré en cuve de la colonne basse pression, pressurisé par une pompe 39 et vaporisé dans l'échangeur 3.A flow of liquid oxygen 37 containing 99.5 mol%. oxygen is withdrawn in the bottom of the low pressure column, pressurized by a pump 39 and vaporized in the exchanger 3.

Un gaz enrichi en argon 49 constituant entre 0,5 et 1% de l'air envoyé à l'appareil et contenant entre 40 et 95 % mol. d'argon soutiré de la tête de la colonne auxiliaire 25 est mélangé avec de l'azote résiduaire 47 de la tête de la colonne basse pression. Le mélange 54 se réchauffe dans le sous refroidisseur 17 puis se réchauffe dans l'échangeur 3. Le mélange est ensuite envoyé en amont de la machine de détente 51 d'une turbine à gaz après une étape de compression éventuelle.An argon-enriched gas 49 constituting between 0.5 and 1% of the air supplied to the apparatus and containing between 40 and 95 mol%. Argon withdrawn from the head of the auxiliary column 25 is mixed with residual nitrogen 47 from the head of the low pressure column. The mixture 54 heats up in the subcooler 17 and then warms up in the exchanger 3. The mixture is then sent upstream of the expansion machine 51 of a gas turbine after a possible compression step.

Auparavant une partie du mélange 54 est détendue dans une turbine 55 (en pointillés).Previously a portion of the mixture 54 is expanded in a turbine 55 (dashed).

Le procédé selon l'invention présente un intérêt particulier dans le cas dans lequel l'azote de la colonne basse pression est valorisé, en l'envoyant à une machine de détente 51 d'une turbine à gaz. Dans ce cas au moins une partie de l'air 1 peut provenir du compresseur 53 de la turbine à gaz et l'oxygène produit par l'appareil de distillation peut servir à la gazéification nécessaire pour produire le carburant de la turbine à gaz.The process according to the invention is of particular interest in the case in which the nitrogen of the low pressure column is upgraded, by sending it to an expansion machine 51 of a gas turbine. In this case at least part of the air 1 can come from the compressor 53 of the gas turbine and the oxygen produced by the distillation apparatus can be used for the gasification necessary to produce the fuel of the gas turbine.

Claims (14)

  1. Method for producing a flow enriched in oxygen in a cryogenic distillation unit, comprising the steps of:
    a) cooling a feed flow (1) comprising oxygen, nitrogen and argon and introducing this flow into a distillation unit comprising an auxiliary column (25) for separating a flow (29) containing at least argon and oxygen, and at least two other columns (9, 18);
    b) separating this flow by cryogenic distillation in the unit, in order to form fluids enriched in oxygen and in nitrogen (15, 33, 35);
    c) sending the flow containing at least argon and oxygen from one of the other columns to the auxiliary column, the auxiliary column operating substantially at the same pressure as the column (18) from which the flow containing at least argon and oxygen originates, this pressure being between 2 and 10 bar absolute;
    d) drawing off a flow enriched in oxygen (37), comprising at least 95 mol % of oxygen, from a column of the unit;
    e) drawing off a flow enriched in argon (49) from the auxiliary column;
    characterised in that at least a portion of the flow enriched in argon (49) is sent upstream of the expansion engine (51) of a gas turbine, optionally after having mixed it with a gas enriched in nitrogen from the unit, and in that a gas (54) is drawn off from the column (18) operating at the lowest pressure, apart from the auxiliary column, and sent to an expansion turbine (55) without being compressed between the column from which it is drawn off and the expansion turbine.
  2. Process according to claim 1, wherein the flow enriched in argon (49) contains between 10 and 95 mol % of argon.
  3. Process according to claim 2, wherein the flow enriched in argon (49) contains between 40 and 95 mol % of argon.
  4. Process according to either claim 1 or claim 2, wherein the flow enriched in argon (49) contains between 2 and 40 mol % of oxygen.
  5. Process according to any one of the preceding claims, wherein at least a portion of the flow enriched in argon (49) is discharged to the atmosphere, optionally after having mixed it with a gas enriched in nitrogen from the unit.
  6. Process according to any one of the preceding claims, wherein at least a portion of the flow enriched in argon (49) is used to regenerate reversible exchangers or adsorbent beds (4), optionally after having mixed it with a gas enriched in nitrogen from the unit.
  7. Process according to any one of claims 1 to 6, wherein a fluid enriched in argon is produced as final product.
  8. Process according to any one of the preceding claims, wherein at least a portion of the flow (49) enriched in argon is sent to the expansion turbine (55) or an expansion valve, optionally after having been mixed with a gas flow enriched in nitrogen.
  9. Process according to any one of the preceding claims, wherein the at least two other columns comprise a high pressure column (9) and a low pressure column (18) connected thermally to one another and the auxiliary column is fed from the low pressure column.
  10. Process according to any one of claims 1 to 8, wherein the unit comprises at least three other columns, including a high pressure column (9), an intermediate pressure column (40) and a low pressure column (18) connected thermally to one another, and the auxiliary column is fed from the low pressure column or the intermediate pressure column.
  11. Integrated process for separating air and producing energy, comprising a process according to claim 1, wherein a fluid enriched in oxygen is sent from a column of the unit to a gasifier or at least a portion of the air intended for the distillation unit originates from a compressor (53) of the gas turbine.
  12. Unit for producing oxygen by cryogenic distillation, comprising:
    a) an auxiliary column (25) and at least two other columns (9, 18);
    b) means for sending a flow (1) containing oxygen, nitrogen and argon to one of the other columns;
    c) means for drawing off a flow enriched in oxygen (37) from one of the other columns;
    d) means for drawing off a flow (29) containing at least argon and oxygen from one of the other columns and means for sending this flow as feed to the auxiliary column (25);
    e) means for drawing off a fluid enriched in argon from the auxiliary column; and
    f) an expansion turbine (55);
    characterised in that the auxiliary column contains between 1 and 99 theoretical plates and there are means for conveying a gas (54) from the column operating at the lowest pressure (18), apart from the auxiliary column, to the expansion turbine, these means not comprising compression means, and means for sending at least a portion of the fluid enriched in argon to an expansion engine of a gas turbine (51).
  13. Unit according to claim 12, wherein there is no expansion means between the column (18) feeding the auxiliary column and the auxiliary column (25).
  14. Unit according to claim 12, comprising means for sending at least a portion of the flow enriched in argon to the atmosphere and/or means for sending at least a portion of the fluid enriched in argon to reversible exchangers or adsorbent beds to regenerate them and/or means for mixing at least a portion of the fluid enriched in argon with a gas enriched in nitrogen (47) from the unit or from another unit.
EP01400749A 2000-04-04 2001-03-22 Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation Expired - Lifetime EP1143216B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0004284 2000-04-04
FR0004284A FR2807150B1 (en) 2000-04-04 2000-04-04 PROCESS AND APPARATUS FOR PRODUCING OXYGEN ENRICHED FLUID BY CRYOGENIC DISTILLATION

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EP1143216B1 true EP1143216B1 (en) 2012-03-07

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US (1) US6434973B2 (en)
EP (1) EP1143216B1 (en)
JP (1) JP2001349669A (en)
AT (1) ATE548619T1 (en)
ES (1) ES2382453T3 (en)
FR (1) FR2807150B1 (en)

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EP1143216A1 (en) 2001-10-10
US6434973B2 (en) 2002-08-20
ATE548619T1 (en) 2012-03-15
JP2001349669A (en) 2001-12-21
US20010052243A1 (en) 2001-12-20
ES2382453T3 (en) 2012-06-08
FR2807150B1 (en) 2002-10-18
FR2807150A1 (en) 2001-10-05

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