FR2837564A1 - Distillation of air to produce oxygen, nitrogen and pure argon, extracts oxygen of specified purity and subjects argon to catalytic de-oxygenation - Google Patents

Distillation of air to produce oxygen, nitrogen and pure argon, extracts oxygen of specified purity and subjects argon to catalytic de-oxygenation Download PDF

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Publication number
FR2837564A1
FR2837564A1 FR0306513A FR0306513A FR2837564A1 FR 2837564 A1 FR2837564 A1 FR 2837564A1 FR 0306513 A FR0306513 A FR 0306513A FR 0306513 A FR0306513 A FR 0306513A FR 2837564 A1 FR2837564 A1 FR 2837564A1
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France
Prior art keywords
column
oxygen
argon
low pressure
distillation
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.)
Pending
Application number
FR0306513A
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French (fr)
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FR2837564A3 (en
Inventor
Frederic Staine
Jean Francois Ducholet
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Air Liquide SA
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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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to FR0306513A priority Critical patent/FR2837564A3/en
Publication of FR2837564A1 publication Critical patent/FR2837564A1/en
Publication of FR2837564A3 publication Critical patent/FR2837564A3/en
Pending legal-status Critical Current

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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
    • F25J3/04521—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
    • F25J3/04606—Partially integrated air feed compression, i.e. independent MAC for the air fractionation unit plus additional air feed from the air gas consuming unit
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04436—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—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]
    • 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
    • F25J3/04521—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
    • 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
    • F25J3/04521—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
    • 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
    • F25J3/04521—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
    • F25J3/046—Completely integrated air feed compression, i.e. common MAC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • 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
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04733—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction
    • F25J3/04739—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction in combination with an auxiliary pure argon column
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0046—Nitrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0051—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0062—Water
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0078—Noble gases
    • C01B2210/0082—Argon
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
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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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
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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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine

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  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Power Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

Oxygen is extracted from the low pressure column (13), preferably at 97.5%-98% purity. The argon is purified by reheating (20), catalytic de-oxygenation with hydrogen (22), dehydration (23, 24), cooling (20) and de-nitrogenation through distillation (25). Oxygen is extracted from the low pressure column (13), preferably at 97.5%-98% purity. The argon is purified by reheating (20), catalytic de-oxygenation with hydrogen (22), dehydration (23, 24), cooling (20) and de-nitrogenation through distillation (25). A further liquid oxygen stream (43) is extracted from the low pressure column (16). This is purified in an auxiliary distillation column (18) to a purity exceeding 99%. Impure argon is compressed before catalytic de-oxygenation, by less than two times. The low pressure column operates under a pressure of about 4 bars absolute. An Independent claim is also included for the corresponding plant for distillation of air.

Description

revendications 7 à 12.claims 7 to 12.

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La présente invention est relative à un procédé de productlon simultance par distillation d' air, d'oxygène et/ou d'azote sous pression d'une part, d' argon sensiblement pur d'autre part, du type dans lequel on distille de l' air dans une unité de distillation d' air qui comprend: une triple colonne comprenant une colonne moyenne pression, une colonne à pression intermédiaire et une colonne basse pression, la pression intermédiaire étant comprise entre la moyenne pression et la basse pression et cette dernière étant au moins égale à 2,5 bars; une colonne de production d' argon impur couplée à la colonne basse pression et fonctionnant à la même pression que celle-ci, et des moyens  The present invention relates to a simultaneous productlon process by distillation of air, oxygen and / or nitrogen under pressure on the one hand, substantially pure argon on the other hand, of the type in which distilled the air in an air distillation unit which comprises: a triple column comprising a medium pressure column, an intermediate pressure column and a low pressure column, the intermediate pressure being between medium pressure and low pressure and the latter being at least equal to 2.5 bars; an impure argon production column coupled to the low pressure column and operating at the same pressure as the latter, and means

de purification de l' argon impur.for the purification of impure argon.

L' invention s' applique notamment à l' alimentation en oxygène et en azote sous pression des unités de production d'énergie de type IGCC (Integrated Gasification Combined Cycle). Les pressions dont il est question ici sont des  The invention is particularly applicable to the supply of oxygen and nitrogen under pressure to IGCC (Integrated Gasification Combined Cycle) type energy production units. The pressures discussed here are

pressions absolues.absolute pressures.

Les unités IGCC consomment de très grandes quantités d'oxygène et d'azote sous pression, et demandent de l'oxygène à faible pureté, typiquement de 95%. Ceci conduit à faire appel à des triples colonnes de distillation d' air pour permettre à la colonne basse pression de produire de l'oxygène sous pression à faible pureté dans des conditions  IGCC units consume very large quantities of oxygen and nitrogen under pressure, and require low purity oxygen, typically 95%. This leads to the use of triple air distillation columns to allow the low pressure column to produce pressurized oxygen with low purity under conditions

de distillation satisfaisantes.satisfactory distillation.

De plus, du fait de la grande taille des unités de distillation d' air nécessaires, il est avantageux de les utiliser pour produire simultanément de l' argon et, éventuellement, de l'oxygène liquide et/ou de l'azote  In addition, due to the large size of the air distillation units required, it is advantageous to use them to simultaneously produce argon and, optionally, liquid oxygen and / or nitrogen.

liquide de plus grande pureté.higher purity liquid.

Cette production combinée pose cependant des problèmes complexes de conception de l'unité de distillation d' air, car d'une part les productions supplémentaires précitées doivent posséder une pureté élevée, typiquement 99,5% au moins pour l'oxygène, d'autre part la séparation  This combined production however poses complex design problems for the air distillation unit, because on the one hand the above-mentioned additional productions must have a high purity, typically 99.5% at least for oxygen, on the other hand apart the separation

argon/oxygène est difficile sous pression.  argon / oxygen is difficult under pressure.

L' invention a pour but de fournir un procédé qui permette d'obtenir une telle production combince dans des  The object of the invention is to provide a process which makes it possible to obtain such a combined production in

conditions économiquement satisfaisantes.  economically satisfactory conditions.

A cet effet, l' invention a pour objet un procédé du type précité, caractérisé en ce que: - on soutire de la cuve de la colonne basse pression de l'oxygène à une première pureté au moins égale à 97,5% environ mais inférieure à 99%, notamment inférieure à 98%; et - on purifie l' argon impur par des étapes successives de réchauffement, désoxygénation catalytique en présence d'hydrogène, déshydratation, refroidissement et  To this end, the subject of the invention is a process of the aforementioned type, characterized in that: - oxygen is withdrawn from the tank of the low pressure column at a first purity at least equal to approximately 97.5% but less than 99%, especially less than 98%; and - the impure argon is purified by successive stages of heating, catalytic deoxygenation in the presence of hydrogen, dehydration, cooling and

déazotation par distillation.denitrogenation by distillation.

Le procédé suivant l' invention peut comporter une ou plusieurs des caractéristiques suivantes: - on fournit l'oxygène soutiré de la cuve de la colonne basse pression à une unité industrielle, notamment à une unité de production d'énergie IGCC, qui accepte l'oxygène à une pureté au moins égale à une valeur nettement inférieure à 97,5%, notamment de 95% environ; - on soutire de la cuve de la colonne basse pression un courant auxiliaire d'oxygène liquide qui est purifié dans une colonne de distillation auxiliaire usqu'à une pureté supérieure à 99%; - on effectue une compression de l' argon impur avant l'étape de désoxygénation catalytique avec un taux de compression inférieur à 2; et - la colonne basse pression fonctionne sous environ 4 bars absolus, et on utilise une colonne de production  The process according to the invention may include one or more of the following characteristics: - the oxygen withdrawn from the tank of the low pressure column is supplied to an industrial unit, in particular to an IGCC energy production unit, which accepts the oxygen at a purity at least equal to a value much less than 97.5%, in particular approximately 95%; - an auxiliary stream of liquid oxygen is withdrawn from the tank of the low pressure column which is purified in an auxiliary distillation column until the purity is greater than 99%; - A compression of the impure argon is carried out before the catalytic deoxygenation step with a compression ratio of less than 2; and - the low pressure column operates at approximately 4 bar absolute, and a production column is used

d' argon impur qui contient 60 à 90 plateaux théoriques.  of impure argon which contains 60 to 90 theoretical plates.

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L' invention a également pour objet une installation  The invention also relates to an installation.

destinée à la mise en oeuvre du procédé défini ci-dessus.  intended for the implementation of the process defined above.

Cette installation, du type comprenant une unité de distillation d' air qui comprend: une triple colonne comprenant une colonne moyenne pression, une colonne à pression intermédiaire et une colonne basse pression, la pression intermédiaire étant comprise entre la moyenne pression et la basse pression et cette dernière étant au moins égale à 2,5 bars; une colonne de production d' argon impur couplée à la colonne basse pression et fonctionnant à la même pression que celle-ci; une ligne d'échange thermique principale adaptée pour refroidir l' air et réchauffer des fluides issus de la triple colonne; et des moyens de purification de l' argon impur, est caractérisée en ce que: - le nombre de plateaux théoriques de la triple colonne est choisi pour une production d'oxygène en cuve de la colonne basse pression à une première pureté au moins égale à 97,5% environ mais inférieure à 99% et notamment inférieure à 98%; et les moyens de purification de l' argon impur comprennent, en série: un échangeur de chaleur pour réchauffer l' argon impur de tête de la colonne de production d' argon impur; un réacteur de désoxygénation catalytique alimenté par l' argon impur issu de l'échangeur de chaleur et par de l'hydrogène; des moyens de déshydratation; et 30. une colonne de déazotation par distilla tion. Un exemple de mise en oeuvre de l' invention va maintenant étre décrit en regard du dessin annexé, dont la  This installation, of the type comprising an air distillation unit which comprises: a triple column comprising a medium pressure column, an intermediate pressure column and a low pressure column, the intermediate pressure being between medium pressure and low pressure and the latter being at least equal to 2.5 bars; an impure argon production column coupled to the low pressure column and operating at the same pressure as the latter; a main heat exchange line adapted to cool the air and heat fluids from the triple column; and means for purifying the impure argon, is characterized in that: - the number of theoretical plates of the triple column is chosen for oxygen production in the bottom of the column of the low pressure column at a first purity at least equal to 97.5% approximately but less than 99% and in particular less than 98%; and the means for purifying the impure argon comprise, in series: a heat exchanger for heating the impure argon at the head of the impure argon production column; a catalytic deoxygenation reactor supplied with impure argon from the heat exchanger and with hydrogen; means of dehydration; and 30. a denitrogenation column by distillation. An example of implementation of the invention will now be described with reference to the accompanying drawing, the

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Figure unique représente schématiquement une installation de  Single figure schematically represents an installation of

distillation d' air conforme à l'invention.  air distillation according to the invention.

L' installation représentée au dessin est constituée d'une unité 1 de production drénergie de type IGCC et d'une unité de distillation d' air 2. L'unité 1 est de tout type connu. La seule caractéristique de cette unité qui soit importante dans le cadre de la présente invention est le fait qu'elle comporte une turbine à gaz et qu'elle consomme de l'oxygène et de  The installation shown in the drawing consists of a unit 1 for producing energy of the IGCC type and an air distillation unit 2. The unit 1 is of any known type. The only characteristic of this unit which is important in the context of the present invention is the fact that it comprises a gas turbine and that it consumes oxygen and

l'azote sous pression.nitrogen under pressure.

- L'unité 2 est destinée à fournir à l'unité 1 l'oxygène sous pression via une conduite 3 et l'azote sous pression via une conduite 4. Elle produit en outre de l' argon liquide sensiblement pur, via une conduite 5, de l'oxygène liquide sensiblement pur, via une conduite 6, et de l'azote liquide sensiblement pur, via une conduite 7. Ces  - Unit 2 is intended to supply unit 1 with oxygen under pressure via a line 3 and nitrogen under pressure via a line 4. It also produces substantially pure liquid argon, via line 5 , substantially pure liquid oxygen, via a line 6, and substantially pure liquid nitrogen, via a line 7. These

trois fluides seront par la suite qualifiés de " purs ".  three fluids will subsequently be described as "pure".

L'unité 2 comprend essentiellement: des moyens d'alimentation en air moyenne pression, constitués par un compresseur d' air principal 7 et par une conduite 7A provenant de l'unité 1, le déLit de cette conduite représentant entre O et 100% du débit d' air traité dans l'unité 2; un appareil 107 de refroidissement et d'épuration en eau et en C02 de l' air moyenne pression; un surpresseur d' air 8; un ensemble turbine 9surpresseur (ou " booster ") couplés sur le même arbre 11 i une ligne d'échange thermique principale 12; une triple colonne de distillation d' air 13 constituée d'une colonne moyenne pression 14, d'une colonne à pression intermédiaire ou " colonne Etienne " 15, et d'une colonne basse pression 16 i une colonne 17 de production d' argon impur dont la cuve est couplée de façon classique à la colonne basse pression par une conduite d'alimentation en gaz 17A et par une conduite de retour de liquide 17B; une colonne 18 de production d'oxygène liquide  Unit 2 essentially comprises: means for supplying medium-pressure air, constituted by a main air compressor 7 and by a pipe 7A coming from unit 1, the delict of this pipe representing between 0 and 100% of the flow of treated air in unit 2; a device 107 for cooling and purifying medium pressure air and C02 air; an air booster 8; a turbine assembly 9 supercharger (or "booster") coupled on the same shaft 11 i a main heat exchange line 12; a triple air distillation column 13 consisting of a medium pressure column 14, an intermediate pressure column or "Etienne column" 15, and a low pressure column 16 i a column 17 for producing impure argon the tank of which is conventionally coupled to the low pressure column by a gas supply line 17A and by a liquid return line 17B; a column 18 for producing liquid oxygen

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pur à partir de l'oxygène liquide de cuve de la colonne basse pression 16; et des moyens 19 de purification d' argon. Ces moyens 19 comprennent euxmêmes un échangeur de chaleur 20, un compresseur d' argon impur 21, un réacteur 22 de désoxygénation catalytique, un réfrigérant 23, un appareil 24 de déshydratation par adsorption, et une colonne  pure from liquid oxygen in the tank of the low pressure column 16; and means 19 for purifying argon. These means 19 themselves include a heat exchanger 20, an impure argon compressor 21, a catalytic deoxygenation reactor 22, a refrigerant 23, an apparatus 24 for adsorption dehydration, and a column

de déazotation par distillation cryogénique.  denitrogenation by cryogenic distillation.

Les colonnes 14 et 16 sont couplées par un vaporiseur-condenseur 26 qui vaporise l'oxygène de cuve de la colonne 16 en condensant l'azote de tête de la colonne 14. La colonne 15 comporte un rebouilleur de cuve 27 dans lequel de l'azote moyenne pression soutiré en tête de la colonne 14 est condensé avant d'être renvoyé en reflux dans celle-ci, et un condenseur de tête 28 dans la calandre duquel du liquide de cuve de la colonne 15 est vaporisé,  Columns 14 and 16 are coupled by a vaporizer-condenser 26 which vaporizes the bottom oxygen of the column 16 by condensing the nitrogen at the top of the column 14. The column 15 includes a bottom reboiler 27 in which medium pressure nitrogen withdrawn at the top of column 14 is condensed before being returned to reflux therein, and an overhead condenser 28 in the shell from which liquid from the bottom of column 15 is vaporized,

après détente dans une vanne de détente 29.  after expansion in an expansion valve 29.

La colonne 17 comporte un condenseur de tête 30 dans la calandre duquel du liquide de cuve de la colonne 15 est  Column 17 has an overhead condenser 30 in the shell of which bottom liquid from column 15 is

vaporisé, après détente dans une vanne de détente 31.  vaporized, after expansion in an expansion valve 31.

Le gaz résultant des deux vaporisations précédentes, en 28 et 30, est envoyé à un niveau intermédiaire de la  The gas resulting from the two previous vaporizations, at 28 and 30, is sent to an intermediate level of the

colonne basse pression 16.low pressure column 16.

La colonne 18 comporte un reLouilleur de cuve 32 dans lequel de l' air moyenne pression est condensé, avant d'être renvoyé dans la partie inférieure de la colonne  Column 18 includes a tank re-reboiler 32 in which medium pressure air is condensed, before being returned to the lower part of the column

moyenne pression 14.medium pressure 14.

La colonne 25 comporte un rebouilleur de cuve 33 dans lequel de l' air moyenne pression est également condensé avant d'être renvoyé dans la partie inférieure de la colonne moyenne pression 14. La colonne 25 comporte également un condenseur de tête 34 dans lequel de l'azote liquide, préalablement détendu à la basse pression de la colonne 16 dans une vanne de détente 35, est vaporisé puis constitue une partie de la production d'azote gazeux sous pression de  Column 25 includes a tank reboiler 33 in which medium pressure air is also condensed before being returned to the lower part of the medium pressure column 14. Column 25 also includes a head condenser 34 in which l liquid nitrogen, previously expanded at low pressure in column 16 in an expansion valve 35, is vaporized and then forms part of the production of nitrogen gas under pressure of

l'unité 2.unit 2.

Les pressions de fonctionnement des colonnes sont les suivantes: 13 bars pour la colonne 14, 9 bars pour la colonne 15, et 4 bars pour les colonnes 16, 17, 18 et 25. En fonctionnement, l' air à traiter, comprimé à 13 bars en 7, est divisé en en trois flux: un flux moyenne pression à 13 bars (conduite 36), refroidi dans la ligne d'échange 12 jusqu'au voisinage de son point de rosée et introduit partiellement en cuve de la colonne 4 et partiellement dans chacun des condenseurs 32 et 33; un flux haute pression, surpressé en 8 à une haute pression suffisante pour permettre la vaporisation de l'oxygène sous pression, refroidi et liquéfié dans la ligne d'échange 12, puis détendu dans une vanne de détente 37 à la moyenne pression et introduit dans la partie inférieure de la colonne 14; et un flux surpressé en 10, refroidi jusqu'à une température intermédiaire dans la ligne d'échange 12 et détendu à la moyenne pression dans la turtine 9, puis réuni au premier flux d' air moyenne pression au bout froid de la  The operating pressures of the columns are as follows: 13 bars for column 14, 9 bars for column 15, and 4 bars for columns 16, 17, 18 and 25. In operation, the air to be treated, compressed to 13 bars in 7, is divided into three streams: a medium pressure stream at 13 bars (line 36), cooled in the exchange line 12 to the vicinity of its dew point and partially introduced into the tank of column 4 and partially in each of the condensers 32 and 33; a high pressure flow, overpressed at 8 to a high pressure sufficient to allow the vaporization of the oxygen under pressure, cooled and liquefied in the exchange line 12, then expanded in an expansion valve 37 at medium pressure and introduced into the lower part of column 14; and a flow pressurized at 10, cooled to an intermediate temperature in the exchange line 12 and expanded at medium pressure in the turtine 9, then joined to the first flow of medium pressure air at the cold end of the

ligne d'échange.exchange line.

Dans la triple colonne 13, comme connu en soi, le liquide riche de cuve de la colonne 14 est. après détente à la pression intermédiaire dans une vanne de détente 38, introduit en cuve de la colonne 15. Du liquide encore enrichi produit en cuve de cette colonne est. après une nouvelle détente dans les vannes 29 et 31, introduit dans la calandre des condenseurs 28 et 30. La fraction restante de ce même liquide est détendue dans une autre vanne de détente  In the triple column 13, as known per se, the rich bottom liquid of the column 14 is. after expansion to the intermediate pressure in an expansion valve 38, introduced into the bottom of the column 15. Liquid still enriched produced in the bottom of this column is. after a further expansion in the valves 29 and 31, introduced into the shell of the condensers 28 and 30. The remaining fraction of this same liquid is expanded in another expansion valve

39 et introduit à un niveau intermédiaire de la colonne 16.  39 and introduced at an intermediate level of column 16.

Une partie de l'azote liquide produit en tête de la colonne 15 est soutirée en tant que produit, via la conduite 7, et une autre partie, détendue dans une vanne de détente 40, est réunie à de l'azote liquide de tête de la colonne 14, détendu dans une vanne de détente 41. Le fluide résultant est. pour partie, introduit en reflux au sommet de la colonne 16 et, pour le reste, détendu dans la vanne de détente 35 pour alimenter le condenseur de tête 34 de la colonne 25. La colonne 16 produit en tête de l'azote gazeux sous pression qui, après mélange avec l'azote vaporisé dans le condenseur 34 et réchauffement dans la ligne d'échange 12, et éventuellement après une nouvelle compression par un compresseur 104, est envoyé à l'unité IGCC 1 via la conduite 4.  Part of the liquid nitrogen produced at the head of column 15 is drawn off as product, via line 7, and another part, expanded in an expansion valve 40, is combined with liquid nitrogen at the head of column 14, expanded in an expansion valve 41. The resulting fluid is. partly, introduced under reflux at the top of column 16 and, for the rest, expanded in the expansion valve 35 to supply the head condenser 34 of column 25. Column 16 produces nitrogen gas under pressure which, after mixing with the nitrogen vaporized in the condenser 34 and heating in the exchange line 12, and possibly after a new compression by a compressor 104, is sent to the IGCC unit 1 via the line 4.

La colonne 16 produit également, en cuve, c'est-à-  Column 16 also produces, in tanks, that is to say

dire au-dessous de tous les moyens d'échange de chaleur et de matière, tels que des garnissages, contenus dans celle ci, de l'oxygène liquide impur, à 97,5% de pureté. Une partie de cet oxygène, après pompage par une pompe 42 à la haute pression de production, est vaporisé puis réchauffé dans la ligne d'échange 12 en condensant l'air surpressé en 8, puis, éventuellement après une nouvelle compression par un compresseur 103, est envoyé à l'unité IGCC via la conduite 3. Une autre partie de cet oxygène liquide, introduit en tête de la colonne 18 via une conduite 43, est purifice dans cette colonne jusqu'à une pureté de 99,5%, puis soutirce à l'état liquide en cuve de la colonne 18, en tant que produit, via la conduite 6. La vapeur de tête de la colonne 18 est renvoyée en cuve de la colonne 16 via une  say below all the means of heat and material exchange, such as linings, contained therein, impure liquid oxygen, at 97.5% purity. Part of this oxygen, after pumping by a pump 42 at the high production pressure, is vaporized and then reheated in the exchange line 12 by condensing the compressed air at 8, then, possibly after a new compression by a compressor 103 , is sent to the IGCC unit via line 3. Another part of this liquid oxygen, introduced at the head of column 18 via line 43, is purified in this column to a purity of 99.5%, then withdrawal in the liquid state in the tank of column 18, as a product, via line 6. The overhead vapor of column 18 is returned to the tank of column 16 via a

conduite 44.driving 44.

L' argon impur produit en tête de la colonne 17 est soutiré sous forme gazeuse, réchauffé dans l'échangeur 20 et comprimé à environ 5,5 bars en 21. Un flux d'hydrogène y est ajouté via une conduite 45, et l' argon est désoxygéné dans le réacteur catalytique 22. L'eau formée par la réaction de l'oxygène et de l'hydrogène est éliminée par réfrigération  The impure argon produced at the head of column 17 is withdrawn in gaseous form, heated in the exchanger 20 and compressed to about 5.5 bars at 21. A stream of hydrogen is added thereto via a pipe 45, and the argon is deoxygenated in the catalytic reactor 22. The water formed by the reaction of oxygen and hydrogen is removed by refrigeration

en 23, puis par adsorption en 24.at 23, then by adsorption at 24.

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L' argon désoxygéné et déshydraté est ensuite refroidi du bout chaud au bout froid de l'échangeur 20, détendu à 4 bars dans une vanne de détente 46, et introduit dans la colonne 25. L' argon liquide pur est soutiré, en tant que produit, de la cuve de cette colonne via la conduite 5. Le gaz résiduaire W évacué en tête de la colonne 25 ne  The deoxygenated and dehydrated argon is then cooled from the hot end to the cold end of the exchanger 20, expanded to 4 bars in an expansion valve 46, and introduced into column 25. The pure liquid argon is withdrawn, as product, from the tank of this column via line 5. The waste gas W discharged at the head of column 25 does not

contient pratiquement pas d' argon.contains practically no argon.

L'ensemble de l' installation permet de fournir de facon particulièrement efficace l'ensemble des productions désirces: oxygène sous pression, azote sous pression,  The whole installation makes it possible to supply in a particularly efficient way all the desired productions: oxygen under pressure, nitrogen under pressure,

oxygène liquide pur, azote liquide pur, argon liquide pur.  pure liquid oxygen, pure liquid nitrogen, pure liquid argon.

La triple colonne permet à son tour, comme connu, de produire en cuve de la colonne 16 de l'oxygène sous pression à 97,5% de pureté, ce qui permet une séparation efficace de l' argon dans la colonne 17, et ce avec de bonnes performances de distillation. La limitation de la séparation argon/oxygène sous pression, dans la colonne 17, à une teneur en oxygène de l' argon de 2,5% environ, suivie d'une purification " chaude " de l' argon en 22, conduit à un rendement d' extraction élevé de l' argon avec un nombre de  The triple column in turn allows, as known, to produce in the bottom of column 16 oxygen under pressure at 97.5% purity, which allows efficient separation of the argon in column 17, and this with good distillation performance. Limiting the argon / oxygen separation under pressure, in column 17, to an oxygen content of argon of approximately 2.5%, followed by a "hot" purification of the argon at 22, leads to a high extraction efficiency of argon with a number of

plateaux théoriques relativement modéré.  relatively moderate theoretical platforms.

Par exemple, on obtient un rendement d' extraction de  For example, an extraction yield of

l' argon d' environ 33% avec 60 à 90 plateaux théoriques.  about 33% argon with 60 to 90 theoretical plates.

En même temps, la pression de la colonne 16, et donc de la colonne 17, est mise à profit d'une part par le fait que le taux de compression du compresseur 21 n'est que d' environ 1,4 (5,5/4), et d'autre part par le fait que la température en tête de la colonne 25 est environ - 182 C, et donc éloignée de la température de - 189 C à partir de laquelle la cristallisation de l' argon apparaît. Les pertes d' argon dans le gaz résiduaire W sont donc nulles, ce qui contribue à l'élévation du rendement d' extraction de  At the same time, the pressure of column 16, and therefore of column 17, is taken advantage of on the one hand by the fact that the compression ratio of compressor 21 is only about 1.4 (5, 5/4), and on the other hand by the fact that the temperature at the top of column 25 is approximately - 182 C, and therefore distant from the temperature of - 189 C from which the crystallization of argon appears. The losses of argon in the waste gas W are therefore zero, which contributes to the increase in the extraction yield of

l' argon.argon.

Claims (10)

REVENDICATIONS 1 - Procédé de production simultance par distillation d' air, d' oxygène et/ou d' azote sous pression d'une part, d' argon sensiblement pur d'autre part, du type dans lequel on distille de l'air dans une unité de distillation d' air (2) qui comprend: une triple colonne (13) comprenant une colonne moyenne pression (14), une colonne à pression intermédiaire (15) et une colonne basse pression (16), la pression intermédiaire étant comprise entre la moyenne pression et la basse pression et cette dernière étant au moins égale à 2,5 bars; une colonne de production d' argon impur (17) couplée à la colonne basse  1 - Process for the simultaneous production by distillation of air, oxygen and / or nitrogen under pressure on the one hand, substantially pure argon on the other hand, of the type in which air is distilled in a air distillation unit (2) which comprises: a triple column (13) comprising a medium pressure column (14), an intermediate pressure column (15) and a low pressure column (16), the intermediate pressure being between the medium pressure and the low pressure and the latter being at least equal to 2.5 bars; an impure argon production column (17) coupled to the lower column pression (16) et fonctionnant à la même pression que celle-  pressure (16) and operating at the same pressure as that ci, et des moyens (19) de purification de l'argon impur, caractérisé en ce que: - on soutire de la cuve de la colonne basse pression (13) de l'oxygène à une première pureté au moins égale à 97,5% environ mais inférieure à 99%, notamment inférieure à 98%; et - on purifie l' argon impur par des étapes successives de réchauffement (20), désoxygénation catalytique en présence d'hydrogène (22), déskydratation (23, 24), refroidissement (20) et déazotation par  ci, and means (19) for purifying impure argon, characterized in that: - oxygen is withdrawn from the tank of the low pressure column (13) at a first purity at least equal to 97.5 about% but less than 99%, especially less than 98%; and - the impure argon is purified by successive stages of heating (20), catalytic deoxygenation in the presence of hydrogen (22), de-hydration (23, 24), cooling (20) and denitrogenation by distillation (25).distillation (25). 2. Procédé suivant la revendication 1, caractérisé en ce qu' on fournit l'oxygène soutiré de la cuve de la colonne basse pression (13) à une unité industrielle (1), notamment à une unité de production d'énergie IGCC, qui accepte l'oxygène à une pureté au moins égale à une valeur  2. Method according to claim 1, characterized in that the oxygen withdrawn from the tank of the low pressure column (13) is supplied to an industrial unit (1), in particular to an IGCC energy production unit, which accepts oxygen at a purity at least equal to a value nettement inférieure à 97,5%, notamment de 95% environ.  significantly lower than 97.5%, especially around 95%. 3. Procédé suivant la revendication 1 ou 2, caractérisé en ce qu'on soutire de la cuve de la colonne basse pression (16) un courant auxiliaire d'oxygène liquide  3. Method according to claim 1 or 2, characterized in that an auxiliary stream of liquid oxygen is withdrawn from the tank of the low pressure column (16) 28375642837564 (43) qui est purifié dans une colonne de distillation  (43) which is purified in a distillation column auxiliaire (18) jusqu'à une pureté supérieure à 99%.  auxiliary (18) up to a purity greater than 99%. 4. Procédé suivant l'une queleonque des  4. Method according to any of the revendications 1 à 3, caractérisé en ce qu'on effectue une  Claims 1 to 3, characterized in that a compression (en 21) de l' argon impur avant l'étape de désoxygénation catalytique (22) avec un taux de compression  compression (at 21) of the impure argon before the catalytic deoxygenation step (22) with a compression ratio inférieur à 2.less than 2. 5. Procédé suivant l'une quelconque des  5. Method according to any one of revendications 1 à 4, caractérisé en ce que la colonne basse  Claims 1 to 4, characterized in that the lower column pression (16) fonctionne sous environ 4 bars absolus, et en ce qu'on utilise une colonne de production d' argon impur  pressure (16) operates at approximately 4 bar absolute, and in that an impure argon production column is used (17) qui contient 60 à 90 plateaux théoriques.  (17) which contains 60 to 90 theoretical plates. 6. Installation de production simultanée par distillation d' air, d'oxygène et/ou d'azote sous pression d'une part, d' argon sensiblement pur d'autre part, du type comprenant une unité de distillation d' air (2) qui comprend: une triple colonne (13) comprenant une colonne moyenne pression (14), une colonne à pression intermédiaire (15) et une colonne basse pression (16), la pression intermédiaire étant comprise entre la moyenne pression et la basse pression et cette dernière étant au moins égale à 2,5 bars; une colonne de production d' argon impur (17) couplée à la colonne basse pression (16) et fonctionnant à la même pression que celle-ci; une ligne d'échange thermique principale (12) adaptée pour refroidir l' air et réchauffer des fluides issus de la triple colonne (13) ; et des moyens (19) de purification de l' argon impur, caractérisoe en ce que: - le nombre de plateaux théoriques de la triple colonne (13) est choisi pour une production d'oxygène en cuve de la colonne basse pression (13) à une première pureté au moins égale à 97,5% environ mais inférieure à 99% et notamment inférieure à 98%; et - les moyens de purification de l' argon impur (19) comprennent, en série: un échangeur de chaleur (20) pour réchauffer l' argon impur de tête de la colonne de production d' argon impur (17); un réacteur de désoxygénation catalytique (22) alimenté par l' argon impur issu de l'échangeur de chaleur (20) et par de l'hydrogène; des moyens (23, 24) de déshydratation; et 10. une colonne de déazotation par  6. Installation for the simultaneous production by distillation of air, oxygen and / or nitrogen under pressure on the one hand, substantially pure argon on the other hand, of the type comprising an air distillation unit (2 ) which comprises: a triple column (13) comprising a medium pressure column (14), an intermediate pressure column (15) and a low pressure column (16), the intermediate pressure being between medium pressure and low pressure and the latter being at least equal to 2.5 bars; an impure argon production column (17) coupled to the low pressure column (16) and operating at the same pressure as the latter; a main heat exchange line (12) adapted to cool the air and heat fluids from the triple column (13); and means (19) for purifying the impure argon, characterized in that: - the number of theoretical plates of the triple column (13) is chosen for the production of oxygen in the bottom of the low pressure column (13) at a first purity at least equal to approximately 97.5% but less than 99% and in particular less than 98%; and - the means for purifying the impure argon (19) comprise, in series: a heat exchanger (20) for reheating the impure argon at the head of the impure argon production column (17); a catalytic deoxygenation reactor (22) supplied with impure argon from the heat exchanger (20) and with hydrogen; dehydration means (23, 24); and 10. a denitrogenation column by distillation (25).distillation (25). 7. Installation suivant la revendication 6, caractérisée en ce qu'elle comprend en outre une unité industrielle (1), notamment une unité de production d'énergie IGCC, qui accepte l'oxygène à une pureté au moins égale à une valeur nettement inférieure à 97,5% et notamment de 95% environ, et des moyens (3) pour alimenter cette unité industrielle (1) avec l'oxygène soutiré de la cuve de la  7. Installation according to claim 6, characterized in that it further comprises an industrial unit (1), in particular an IGCC energy production unit, which accepts oxygen at a purity at least equal to a significantly lower value at 97.5% and in particular around 95%, and means (3) for supplying this industrial unit (1) with oxygen drawn from the tank of the colonne basse pression (13).low pressure column (13). 8. Installation suivant la revendication 6 ou 7, caractérisée en ce qu'elle comprend en outre une colonne de purification d'oxygène (18) alimentée par de l'oxygène liquide soutiré de la cuve de la colonne basse pression (16) et adaptée pour produire en cuve de l'oxygène à une pureté  8. Installation according to claim 6 or 7, characterized in that it further comprises an oxygen purification column (18) supplied with liquid oxygen withdrawn from the tank of the low pressure column (16) and adapted to produce purity oxygen in tanks supérieure à 99%.greater than 99%. 9. Installation suivant l'une quelconque des  9. Installation according to any one of revendications 6 à 8, caractérisée en ce que les moyens de  Claims 6 to 8, characterized in that the means for purification d' argon impur (19) comprennent un compresseur (21), entre l'échangeur de chaleur (20) et le réacteur (22),  purification of impure argon (19) include a compressor (21), between the heat exchanger (20) and the reactor (22), ce compresseur ayant un taux de compression inférieur à 2.  this compressor having a compression ratio of less than 2. 10. Installation suivant l'une quelconque des  10. Installation according to any one of revendications 6 à 9, caractérisée en ce que la colonne  Claims 6 to 9, characterized in that the column basse pression (16) fonctionne sous environ 4 bars absolus, s  low pressure (16) operates at approximately 4 bar absolute, s 12 283756412 2837564 et en ce que la colonne de production d' argon impur (17)  and in that the impure argon production column (17)
FR0306513A 2003-05-28 2003-05-28 METHOD AND PLANT FOR PRODUCTION OF OXYGEN AND/OR NITROGEN UNDER PRESSURE AND PURE ARGON Pending FR2837564A3 (en)

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2968749A1 (en) * 2010-12-13 2012-06-15 Air Liquide Method for air separation by cryogenic distillation for integrated gasification combined cycle system, involves compressing vaporized oxygen without having to be heated more than specific degrees Celsius, and heating compressed oxygen
CN102721260A (en) * 2012-07-04 2012-10-10 开封空分集团有限公司 High-purity oxygen extracting device and method for extracting high-purity oxygen by utilizing same
CN111811213A (en) * 2020-06-10 2020-10-23 北京科技大学 Internal compression air separation process flow with energy storage and efficient recovery of material energy resources
WO2024026165A1 (en) * 2022-07-28 2024-02-01 Praxair Technology, Inc. System and method for cryogenic air separation using four distillation columns including an intermediate pressure column
WO2024026168A1 (en) * 2022-07-28 2024-02-01 Praxair Technology, Inc. Air separation unit and method for cryogenic separation of air using a distillation column system including an intermediate pressure kettle column
US11959701B2 (en) 2022-07-28 2024-04-16 Praxair Technology, Inc. Air separation unit and method for production of high purity nitrogen product using a distillation column system with an intermediate pressure kettle column
US12055345B2 (en) 2022-07-28 2024-08-06 Praxair Technology, Inc. Air separation unit and method for production of nitrogen and argon using a distillation column system with an intermediate pressure kettle column

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2968749A1 (en) * 2010-12-13 2012-06-15 Air Liquide Method for air separation by cryogenic distillation for integrated gasification combined cycle system, involves compressing vaporized oxygen without having to be heated more than specific degrees Celsius, and heating compressed oxygen
CN102721260A (en) * 2012-07-04 2012-10-10 开封空分集团有限公司 High-purity oxygen extracting device and method for extracting high-purity oxygen by utilizing same
CN111811213A (en) * 2020-06-10 2020-10-23 北京科技大学 Internal compression air separation process flow with energy storage and efficient recovery of material energy resources
WO2024026165A1 (en) * 2022-07-28 2024-02-01 Praxair Technology, Inc. System and method for cryogenic air separation using four distillation columns including an intermediate pressure column
WO2024026168A1 (en) * 2022-07-28 2024-02-01 Praxair Technology, Inc. Air separation unit and method for cryogenic separation of air using a distillation column system including an intermediate pressure kettle column
US11959701B2 (en) 2022-07-28 2024-04-16 Praxair Technology, Inc. Air separation unit and method for production of high purity nitrogen product using a distillation column system with an intermediate pressure kettle column
US12055345B2 (en) 2022-07-28 2024-08-06 Praxair Technology, Inc. Air separation unit and method for production of nitrogen and argon using a distillation column system with an intermediate pressure kettle column

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