EP0531182A1 - Process and plant for distilling air and application in the feeding of gas to steel plants - Google Patents

Process and plant for distilling air and application in the feeding of gas to steel plants Download PDF

Info

Publication number
EP0531182A1
EP0531182A1 EP92402246A EP92402246A EP0531182A1 EP 0531182 A1 EP0531182 A1 EP 0531182A1 EP 92402246 A EP92402246 A EP 92402246A EP 92402246 A EP92402246 A EP 92402246A EP 0531182 A1 EP0531182 A1 EP 0531182A1
Authority
EP
European Patent Office
Prior art keywords
column
oxygen
liquid
low pressure
gas
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.)
Granted
Application number
EP92402246A
Other languages
German (de)
French (fr)
Other versions
EP0531182B1 (en
EP0531182B2 (en
Inventor
François Camberlein
Jean-Louis Girault
Philippe Mazieres
Jean-Pierre Tranier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=9415988&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0531182(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0531182A1 publication Critical patent/EP0531182A1/en
Publication of EP0531182B1 publication Critical patent/EP0531182B1/en
Application granted granted Critical
Publication of EP0531182B2 publication Critical patent/EP0531182B2/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04551—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the metal production
    • F25J3/04557—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the metal production for pig iron or steel making, e.g. blast furnace, Corex
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/0446—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 the heat generated by mixing two different phases
    • F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid 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
    • F25J3/04642—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/915—Combustion
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the present invention relates to the air distillation technique.
  • coal gasification gasification of petroleum residues, direct reduction-smelting of iron ore, injection of coal into blast furnaces, metallurgy of non-ferrous metals, etc.
  • the object of the invention is to satisfy such needs economically, that is to say to allow, with a relatively low investment and energy consumption, the production of impure oxygen at a selected purity and pressure. at will and, if necessary, the production of practically pure oxygen.
  • the subject of the invention is a process for the distillation of air by means of a double distillation column coupled to a mixing column, in which the mixing column is supplied to the tank with an auxiliary gas consisting of a mixture of air gases, and at the top with a liquid richer in oxygen than the auxiliary gas, taken from the lower part of the low pressure column, and impure oxygen is drawn off at the top of the mixing column constituting a production gas, where the auxiliary gas and the liquid supplying the mixing column are compressed at the same pressure different from that of the medium pressure column, typically higher than the latter, advantageously at least 2 ⁇ 105 Pa.
  • Said liquid can be the bottom liquid of the low pressure column, in particular oxygen practically without nitrogen, or else it can be drawn off a few trays above the bottom of the low pressure column.
  • the invention also relates to an air distillation installation intended for the implementation of the process defined above, of the type comprising a double distillation column, a mixing column, a heat exchange line, a source an auxiliary gas consisting of a mixture of air gases, means for introducing the auxiliary gas at the base of the mixing column, means for withdrawing a liquid richer in oxygen than the auxiliary gas in the part bottom of the low pressure column, means for pumping this liquid and for introducing it at the top of the mixing column, and means for withdrawing impure oxygen at the head of the mixing column as gas for producing the installation, characterized in that it comprises means for compressing the auxiliary gas to a determined pressure different from that of the medium pressure column, passages for this compressed auxiliary gas provided in the line heat exchange and in that the pumping means bring the liquid to said determined pressure.
  • the invention also relates to the application of the process defined above to the supply of gas to a steelworks, said impure oxygen being produced under the pressure of the blast furnace and being sent to the latter.
  • said liquid is oxygen practically without nitrogen
  • said oxygen is sent practically without nitrogen to the converters of the steelworks.
  • FIGS. 1 to 3 schematically represent three embodiments of the air distillation installation according to the invention.
  • the air distillation installation shown in FIG. 1 is intended to produce impure oxygen, for example having a purity of 80 to 97% and preferably 85 to 95%, under a determined pressure P clearly different from 6 x 105 Pa abs., Per example under 2 to 5 x 105 Pa or advantageously under a pressure higher by at least 2 x 105 Pa and possibly up to around 30 x 105 Pa, preferably between 8 x 105 Pa and 15 x 105 Pa.
  • the installation essentially comprises a heat exchange line 1, a double distillation column 2 itself comprising a medium pressure column 3, a low pressure column 4 and a main condenser-vaporizer 5, and a mixing column 6. Columns 3 and 4 typically operate at approximately 6 x 105 Pa and approximately 1 x 105 Pa, respectively.
  • a mixing column is a column which has the same structure as a distillation column but which is used to mix in a manner close to reversibility a relatively volatile gas, introduced at its base, and a less volatile liquid, introduced at its top.
  • Such a mixture produces refrigerating energy and therefore makes it possible to reduce the energy consumption linked to the distillation.
  • this mixture is used, moreover, to directly produce impure oxygen under the pressure P, as will be described below.
  • the air to be separated by distillation, compressed to 6 x 105 Pa and suitably purified, is conveyed to the base of the medium pressure column 3 by a pipe 7. Most of this air is cooled in the exchange line 1 and introduced at the base of the medium pressure column 3, and the rest, boosted at 8 then cooled, is expanded at low pressure in a turbine 9 coupled to the booster 8, then blown at an intermediate point of the low pressure column 4. From “rich liquid” (oxygen-enriched air), taken from the tank of column 3 is, after expansion in an expansion valve 10, introduced into column 4, approximately at the point of air blowing.
  • Liquid oxygen is withdrawn from the tank of column 4, carried by a pump 13 at a pressure P1, slightly higher than the above-mentioned pressure P to take account of the losses load (P1-P less than 1 x 105 Pa), and introduced at the top of column 6.
  • P1 is therefore advantageously between 8 x 105 Pa and 30 x 105 Pa, preferably between 8 x 105 Pa and 16 x 105 Pa.
  • Auxiliary air, compressed at the same pressure P1 by an auxiliary compressor 14 and cooled in the exchange line 1, is introduced at the base of the mixing column 6.
  • FIG. 1 also shows auxiliary heat exchangers 19, 20, 21 ensuring the recovery of the cold available in the fluids circulating in the installation.
  • the pressure P of the impure oxygen produced can be chosen as desired.
  • the adjustment of the double column makes it possible to obtain various degrees of purity for this gas.
  • Another way of determining this degree of purity consists, as shown in FIG. 2, of choosing the level of sampling, in the low pressure column 4, of the liquid feeding the column 6, for example by leaving a few trays of distillation between the point and the column 4 tank.
  • the installation can produce, simultaneously with the impure oxygen of column 6, oxygen at a different purity and at a pressure, in particular oxygen roughly pure, by drawing off at the bottom of column 4.
  • This oxygen can be supplied in gaseous form, via a line 22 crossing the exchange line 1, under the low pressure of the low pressure column 4 or under pressure, in particular by pumping the liquid at 23 before it warms up in the exchange line; it can also be liquefied and sent to storage 24.
  • FIG. 3 differs from that of FIG. 2 in that it further comprises a column 25 for producing impure argon coupled, in a conventional manner, to the low pressure column 4.
  • the fact that the impure oxygen is produced not by the low pressure column 4 but by the mixing column 6 makes it possible to produce impure oxygen containing very little argon, which leaves the possibility of producing, in addition to argon, provided of course that the liquid oxygen withdrawn and pumped at 13 has sufficient purity, in particular at least equal to 98%.
  • the air auxiliary to the pressure P1 may be suitably purified atmospheric air, but also come from an annex process comprising an air compressor. It may for example be air taken from the inlet of a gas turbine and the pressure of which may be adjusted by means of a booster or an expansion turbine. More generally, it is possible to use, to feed the base of the mixing column 6, a mixture of air gases less rich in oxygen than the liquid taken from the lower part of the low pressure column, in particular impure nitrogen originating possibly from the installation itself.
  • the invention makes it possible to simultaneously produce, under particularly economical conditions of investment and energy consumption, pure or nearly pure oxygen, impure oxygen and argon.
  • the oxygen produced by column 4 is practically devoid of nitrogen and can therefore be used in the converters of a steelworks.
  • the installation in the form of FIG. 2, thus makes it possible to supply both these converters with pure oxygen and the blast furnace of the steelworks with impure oxygen at the pressure of the blast furnace; in its form in FIG. 3, the installation can also supply the steelworks with argon.

Abstract

L'installation est du type à double colonne (2) et à colonne de mélange (6). Cette dernière est alimentée en cuve par de l'air auxiliaire comprimé à une pression différente de celle de la colonne moyenne pression (3), et en tête par du liquide soutiré au bas de la colonne basse pression (4) et pompé à la même pression que l'air auxiliaire. De l'oxygène impur est soutiré en tête de la colonne de mélange en tant que gaz de production, et de l'oxygène à peu près pur est produit en cuve de la colonne basse pression. <IMAGE>The installation is of the double column (2) and mixing column (6) type. The latter is supplied to the tank by auxiliary air compressed to a pressure different from that of the medium pressure column (3), and at the head by liquid withdrawn from the bottom of the low pressure column (4) and pumped at the same pressure than auxiliary air. Impure oxygen is drawn off at the head of the mixing column as production gas, and approximately pure oxygen is produced in the bottom of the low pressure column. <IMAGE>

Description

La présente invention est relative à la technique de distillation de l'air.The present invention relates to the air distillation technique.

Certaines applications industrielles nécessitent des quantités importantes d'oxygène impur sous diverses pressions :Certain industrial applications require significant quantities of impure oxygen under various pressures:

gazéification du charbon, gazéification de résidus pétroliers, réduction-fusion directe du minerai de fer, injection de charbon dans les hauts fourneaux, métallurgie des métaux non ferreux, etc.coal gasification, gasification of petroleum residues, direct reduction-smelting of iron ore, injection of coal into blast furnaces, metallurgy of non-ferrous metals, etc.

Par ailleurs, certains contextes industriels nécessitent la fourniture simultanée, en grandes quantités, d'oxygène pratiquement pur et d'oxygène impur sous des pressions différentes. C'est notamment le cas des aciéries comportant des convertisseurs à l'oxygène et dans lesquelles le haut fourneau est alimenté en oxygène ou en air enrichi en oxygène.In addition, certain industrial contexts require the simultaneous supply, in large quantities, of practically pure oxygen and of impure oxygen under different pressures. This is particularly the case for steelworks with oxygen converters and in which the blast furnace is supplied with oxygen or oxygen-enriched air.

L'invention a pour but de satisfaire de tels besoins de façon économique, c'est-à-dire de permettre, avec un investissement et une consommation d'énergie relativement faibles, la production d'oxygène impur à une pureté et une pression choisies à volonté et, si nécessaire, la production d'oxygène pratiquement pur.The object of the invention is to satisfy such needs economically, that is to say to allow, with a relatively low investment and energy consumption, the production of impure oxygen at a selected purity and pressure. at will and, if necessary, the production of practically pure oxygen.

A cet effet, l'invention a pour objet un procédé de distillation d'air au moyen d'une double colonne de distillation couplée à une colonne de mélange, dans lequel on alimente la colonne de mélange en cuve par un gaz auxiliaire constitué d'un mélange de gaz de l'air, et en tête par un liquide plus riche en oxygène que le gaz auxiliaire, prélevé dans la partie inférieure de la colonne basse pression, et on soutire en tête de la colonne de mélange de l'oxygène impur constituant un gaz de production, où le gaz auxiliaire et le liquide alimentant la colonne de mélange sont comprimés à une même pression différente de celle de la colonne moyenne pression, typiquement supérieure à cette dernière, avantageusement d'au moins 2 x 10⁵ Pa.To this end, the subject of the invention is a process for the distillation of air by means of a double distillation column coupled to a mixing column, in which the mixing column is supplied to the tank with an auxiliary gas consisting of a mixture of air gases, and at the top with a liquid richer in oxygen than the auxiliary gas, taken from the lower part of the low pressure column, and impure oxygen is drawn off at the top of the mixing column constituting a production gas, where the auxiliary gas and the liquid supplying the mixing column are compressed at the same pressure different from that of the medium pressure column, typically higher than the latter, advantageously at least 2 × 10⁵ Pa.

Ledit liquide peut être le liquide de cuve de la colonne basse pression, notamment de l'oxygène pratiquement sans azote, ou bien être soutiré quelques plateaux au-dessus de la cuve de la colonne basse pression.Said liquid can be the bottom liquid of the low pressure column, in particular oxygen practically without nitrogen, or else it can be drawn off a few trays above the bottom of the low pressure column.

Dans le cadre d'un tel procédé, on peut en outre produire de l'argon au moyen d'une colonne de distillation additionnelle de production d'argon impur couplée à la colonne basse pression.In the context of such a process, it is also possible to produce argon by means of an additional distillation column for producing impure argon coupled to the low pressure column.

L'invention a également pour objet une installation de distillation d'air destinée à la mise en oeuvre du procédé défini ci-dessus, du type comprenant une double colonne de distillation, une colonne de mélange, une ligne d'échange thermique, une source d'un gaz auxiliaire constitué d'un mélange de gaz de l'air, des moyens pour introduire le gaz auxiliaire à la base de la colonne de mélange, des moyens pour soutirer un liquide plus riche en oxygène que le gaz auxiliaire dans la partie inférieure de la colonne basse pression, des moyens pour pomper ce liquide et pour l'introduire au sommet de la colonne de mélange, et des moyens pour soutirer de l'oxygène impur en tête de la colonne de mélange en tant que gaz de production de l'installation, caractérisée en ce qu'elle comprend des moyens pour comprimer le gaz auxiliaire à une pression déterminée différente de celle de la colonne moyenne pression, des passages pour ce gaz auxiliaire comprimé prévus dans la ligne d'échange thermique et en ce que les moyens de pompage portent le liquide à ladite pression déterminée.The invention also relates to an air distillation installation intended for the implementation of the process defined above, of the type comprising a double distillation column, a mixing column, a heat exchange line, a source an auxiliary gas consisting of a mixture of air gases, means for introducing the auxiliary gas at the base of the mixing column, means for withdrawing a liquid richer in oxygen than the auxiliary gas in the part bottom of the low pressure column, means for pumping this liquid and for introducing it at the top of the mixing column, and means for withdrawing impure oxygen at the head of the mixing column as gas for producing the installation, characterized in that it comprises means for compressing the auxiliary gas to a determined pressure different from that of the medium pressure column, passages for this compressed auxiliary gas provided in the line heat exchange and in that the pumping means bring the liquid to said determined pressure.

L'invention a encore pour objet l'application du procédé défini plus haut à l'alimentation en gaz d'une aciérie, ledit oxygène impur étant produit sous la pression du haut fourneau et étant envoyé à ce dernier.The invention also relates to the application of the process defined above to the supply of gas to a steelworks, said impure oxygen being produced under the pressure of the blast furnace and being sent to the latter.

Lorsque ledit liquide est de l'oxygène pratiquement sans azote, de façon avantageuse, on envoie ledit oxygène pratiquement sans azote aux convertisseurs de l'aciérie.When said liquid is oxygen practically without nitrogen, advantageously, said oxygen is sent practically without nitrogen to the converters of the steelworks.

Des exemples de mise en oeuvre de l'invention vont maintenant être décrits en regard des dessins annexés, sur lesquels les figures 1 à 3 représentent schématiquement trois modes de réalisation de l'installation de distillation d'air conforme à l'invention.Examples of implementation of the invention will now be described with reference to the accompanying drawings, in which FIGS. 1 to 3 schematically represent three embodiments of the air distillation installation according to the invention.

L'installation de distillation d'air représentée à la figure 1 est destinée à produire de l'oxygène impur, par exemple ayant une pureté de 80 à 97 % et de préférence de 85 à 95 %, sous une pression déterminée P nettement différente de 6 x 10⁵ Pa abs., par exemple sous 2 à 5 x 10⁵ Pa ou avantageusement sous une pression supérieure d'au moins 2 x 10⁵ Pa et pouvant aller jusqu'à 30 x 10⁵ Pa environ, de préférence entre 8 x 10⁵ Pa et 15 x 10⁵ Pa. L'installation comprend essentiellement une ligne d'échange thermique 1, une double colonne de distillation 2 comprenant elle-même une colonne moyenne pression 3, une colonne basse pression 4 et un condenseur-vaporiseur principal 5, et une colonne de mélange 6. Les colonnes 3 et 4 fonctionnent typiquement sous environ 6 x 10⁵ Pa et environ 1 x 10⁵ Pa, respectivement.The air distillation installation shown in FIG. 1 is intended to produce impure oxygen, for example having a purity of 80 to 97% and preferably 85 to 95%, under a determined pressure P clearly different from 6 x 10⁵ Pa abs., Per example under 2 to 5 x 10⁵ Pa or advantageously under a pressure higher by at least 2 x 10⁵ Pa and possibly up to around 30 x 10⁵ Pa, preferably between 8 x 10⁵ Pa and 15 x 10⁵ Pa. The installation essentially comprises a heat exchange line 1, a double distillation column 2 itself comprising a medium pressure column 3, a low pressure column 4 and a main condenser-vaporizer 5, and a mixing column 6. Columns 3 and 4 typically operate at approximately 6 x 10⁵ Pa and approximately 1 x 10⁵ Pa, respectively.

Comme expliqué en détail dans le document US-A-4.022.030, une colonne de mélange est une colonne qui a la même structure qu'une colonne de distillation mais qui est utilisée pour mélanger de façon proche de la réversibilité un gaz relativement volatil, introduit à sa base, et un liquide moins volatil, introduit à son sommet.As explained in detail in document US-A-4,022,030, a mixing column is a column which has the same structure as a distillation column but which is used to mix in a manner close to reversibility a relatively volatile gas, introduced at its base, and a less volatile liquid, introduced at its top.

Un tel mélange produit de l'énergie frigorifique et permet donc de réduire la consommation d'énergie liée à la distillation. Dans le cas présent, ce mélange est mis à profit, en outre, pour produire directement de l'oxygène impur sous la pression P, comme cela sera décrit ci-dessous.Such a mixture produces refrigerating energy and therefore makes it possible to reduce the energy consumption linked to the distillation. In the present case, this mixture is used, moreover, to directly produce impure oxygen under the pressure P, as will be described below.

L'air à séparer par distillation, comprimé à 6 x 10⁵ Pa et convenablement épuré, est acheminé vers la base de la colonne moyenne pression 3 par une conduite 7. La majeure partie de cet air est refroidie dans la ligne d'échange 1 et introduite à la base de la colonne moyenne pression 3, et le reste, surpressé en 8 puis refroidi, est détendu à la basse pression dans une turbine 9 couplée au surpresseur 8, puis insufflé en un point intermédiaire de la colonne basse pression 4. Du "liquide riche" (air enrichi en oxygène), prélevé en cuve de la colonne 3 est, après détente dans une vanne de détente 10, introduit dans la colonne 4, à peu près au point d'insufflation de l'air. Du "liquide pauvre" (azote impur) prélevé en un point intermédiaire 11 de la colonne 3 est, après détente dans une vanne de détente 12, introduit au sommet de la colonne 4, constituant le gaz résiduaire de l'installation, et l'azote gazeux pur sous la moyenne pression produit en tête de la colonne 3, sont réchauffés dans la ligne d'échange 1 et évacués de l'installation. Ces gaz sont indiqués respectivement par NI et NG sur la figure 1.The air to be separated by distillation, compressed to 6 x 10⁵ Pa and suitably purified, is conveyed to the base of the medium pressure column 3 by a pipe 7. Most of this air is cooled in the exchange line 1 and introduced at the base of the medium pressure column 3, and the rest, boosted at 8 then cooled, is expanded at low pressure in a turbine 9 coupled to the booster 8, then blown at an intermediate point of the low pressure column 4. From "rich liquid" (oxygen-enriched air), taken from the tank of column 3 is, after expansion in an expansion valve 10, introduced into column 4, approximately at the point of air blowing. "Lean liquid" (impure nitrogen) taken from an intermediate point 11 of column 3 is, after expansion in an expansion valve 12, introduced at the top of column 4, constituting the residual gas of the installation, and the pure nitrogen gas under the medium pressure produced at the top of column 3, are heated in the exchange line 1 and evacuated from the installation. These gases are indicated respectively by NI and NG in Figure 1.

De l'oxygène liquide, plus ou moins pur suivant le réglage de la double colonne 2, est soutiré en cuve de la colonne 4, porté par une pompe 13 à une pression P1, légèrement supérieure à la pression P précitée pour tenir compte des pertes de charge (P1-P inférieur à 1 x 10⁵ Pa), et introduit au sommet de la colonne 6. P1 est donc avantageusement comprise entre 8 x 10⁵ Pa et 30 x 10⁵ Pa, de préférence entre 8 x 10⁵ Pa et 16 x 10⁵ Pa. De l'air auxiliaire, comprimé à la même pression P1 par un compresseur auxiliaire 14 et refroidi dans la ligne d'échange 1, est introduit à la base de la colonne de mélange 6. De cette dernière sont soutirés trois courants de fluide : à sa base, du liquide voisin du liquide riche et réuni à ce dernier via une conduite 15 munie d'une vanne de détente 15A ; en un point intermédiaire, un mélange essentiellement constitué d'oxygène et d'azote, qui est renvoyé en un point intermédiaire de la colonne basse pression 4 via une conduite 16 munie d'une vanne de détente 17 ; et à son sommet de l'oxygène impur qui, après réchauffement dans la ligne d'échange thermique, est évacué, sensiblement à la pression P, de l'installation via une conduite 18 en tant que gaz de production 0I.Liquid oxygen, more or less pure depending on the setting of the double column 2, is withdrawn from the tank of column 4, carried by a pump 13 at a pressure P1, slightly higher than the above-mentioned pressure P to take account of the losses load (P1-P less than 1 x 10⁵ Pa), and introduced at the top of column 6. P1 is therefore advantageously between 8 x 10⁵ Pa and 30 x 10⁵ Pa, preferably between 8 x 10⁵ Pa and 16 x 10⁵ Pa. Auxiliary air, compressed at the same pressure P1 by an auxiliary compressor 14 and cooled in the exchange line 1, is introduced at the base of the mixing column 6. From this latter are drawn three streams of fluid : at its base, liquid close to the rich liquid and joined to the latter via a pipe 15 provided with an expansion valve 15A; at an intermediate point, a mixture essentially consisting of oxygen and nitrogen, which is returned to an intermediate point of the low pressure column 4 via a pipe 16 provided with an expansion valve 17; and at its top impure oxygen which, after heating in the heat exchange line, is evacuated, substantially at pressure P, from the installation via a pipe 18 as production gas OI.

On a également représenté sur la figure 1 des échangeurs de chaleur auxiliaires 19, 20, 21 assurant la récupération du froid disponible dans les fluides en circulation dans l'installation.FIG. 1 also shows auxiliary heat exchangers 19, 20, 21 ensuring the recovery of the cold available in the fluids circulating in the installation.

Comme on le comprend, grâce à la présence d'un circuit séparé pour l'air auxiliaire alimentant la colonne 6, on peut choisir à volonté la pression P de l'oxygène impur produit. De plus, comme indiqué plus haut, le réglage de la double colonne permet d'obtenir divers degrés de pureté pour ce gaz.As will be understood, thanks to the presence of a separate circuit for the auxiliary air supplying column 6, the pressure P of the impure oxygen produced can be chosen as desired. In addition, as indicated above, the adjustment of the double column makes it possible to obtain various degrees of purity for this gas.

Une autre manière de déterminer ce degré de pureté consiste, comme représenté à la figure 2, à choisir le niveau de prélèvement, dans la colonne basse pression 4, du liquide alimentant la colonne 6, par exemple en laissant quelques plateaux de distillation entre le point de prélèvement et la cuve de la colonne 4.Another way of determining this degree of purity consists, as shown in FIG. 2, of choosing the level of sampling, in the low pressure column 4, of the liquid feeding the column 6, for example by leaving a few trays of distillation between the point and the column 4 tank.

Comme on l'a également représenté sur la figure 2, l'installation peut produire, simultanément à l'oxygène impur de la colonne 6, de l'oxygène à une pureté et à une pression différentes, notamment de l'oxygène à peu près pur, par soutirage au bas de la colonne 4. Cet oxygène peut être fourni sous forme gazeuse, via une conduite 22 traversant la ligne d'échange 1, sous la basse pression de la colonne basse pression 4 ou sous pression, notamment par pompage du liquide en 23 avant son réchauffement dans la ligne d'échange ; il peut aussi être liquéfié et envoyé dans un stockage 24.As also shown in FIG. 2, the installation can produce, simultaneously with the impure oxygen of column 6, oxygen at a different purity and at a pressure, in particular oxygen roughly pure, by drawing off at the bottom of column 4. This oxygen can be supplied in gaseous form, via a line 22 crossing the exchange line 1, under the low pressure of the low pressure column 4 or under pressure, in particular by pumping the liquid at 23 before it warms up in the exchange line; it can also be liquefied and sent to storage 24.

L'installation de la figure 3 diffère de celle de la figure 2 par le fait qu'elle comprend en outre une colonne 25 de production d'argon impur couplée, de façon classique, à la colonne basse pression 4.The installation of FIG. 3 differs from that of FIG. 2 in that it further comprises a column 25 for producing impure argon coupled, in a conventional manner, to the low pressure column 4.

En effet, le fait que l'oxygène impur soit produit non pas par la colonne basse pression 4 mais par la colonne de mélange 6 permet de produire de l'oxygène impur contenant très peu d'argon, ce qui laisse la possibilité de produire, en plus de l'argon, à condition bien entendu que l'oxygène liquide soutiré et pompé en 13 ait une pureté suffisante, notamment au moins égale à 98 %.Indeed, the fact that the impure oxygen is produced not by the low pressure column 4 but by the mixing column 6 makes it possible to produce impure oxygen containing very little argon, which leaves the possibility of producing, in addition to argon, provided of course that the liquid oxygen withdrawn and pumped at 13 has sufficient purity, in particular at least equal to 98%.

L'air auxiliaire à la pression P1 peut être de l'air atmosphérique convenablement épuré, mais également provenir d'un procédé annexe comprenant un compresseur d'air. Il peut par exemple s'agir d'air prélevé à l'entrée d'une turbine à gaz et dont la pression est éventuellement ajustée au moyen d'un surpresseur ou d'une turbine de détente. Plus généralement, on peut utiliser pour alimenter la base de la colonne de mélange 6, un mélange de gaz de l'air moins riche en oxygène que le liquide prélevé dans la partie inférieure de la colonne basse pression, notamment de l'azote impur provenant éventuellement de l'installation elle-même.The air auxiliary to the pressure P1 may be suitably purified atmospheric air, but also come from an annex process comprising an air compressor. It may for example be air taken from the inlet of a gas turbine and the pressure of which may be adjusted by means of a booster or an expansion turbine. More generally, it is possible to use, to feed the base of the mixing column 6, a mixture of air gases less rich in oxygen than the liquid taken from the lower part of the low pressure column, in particular impure nitrogen originating possibly from the installation itself.

Ainsi, l'invention permet de produire simultanément, dans des conditions particulièrement économiques d'investissement et de consommation d'énergie, de l'oxygène pur ou à peu près pur, de l'oxygène impur et de l'argon.Thus, the invention makes it possible to simultaneously produce, under particularly economical conditions of investment and energy consumption, pure or nearly pure oxygen, impure oxygen and argon.

Il est à noter que l'oxygène produit par la colonne 4 est pratiquement dépourvu d'azote et peut donc être utilisé dans les convertisseurs d'une aciérie. L'installation, sous la forme de la figure 2, permet ainsi d'alimenter à la fois ces convertisseurs en oxygène pur et le haut fourneau de l'aciérie en oxygène impur à la pression du haut fourneau ; sous sa forme de la figure 3, l'installation peut alimenter en outre l'aciérie en argon.It should be noted that the oxygen produced by column 4 is practically devoid of nitrogen and can therefore be used in the converters of a steelworks. The installation, in the form of FIG. 2, thus makes it possible to supply both these converters with pure oxygen and the blast furnace of the steelworks with impure oxygen at the pressure of the blast furnace; in its form in FIG. 3, the installation can also supply the steelworks with argon.

Claims (15)

Procédé de distillation d'air au moyen d'une double colonne de distillation (2) couplée à une colonne de mélange (6), dans lequel on alimente la colonne de mélange en cuve par un gaz auxiliaire constitué d'un mélange de gaz de l'air, et en tête par un liquide plus riche en oxygène que le gaz auxiliaire, prélevé dans la partie inférieure de la colonne basse pression (4), et on soutire en tête de la colonne de mélange (6) de l'oxygène impur constituant un gaz de production, caractérisé en ce que le gaz auxiliaire et le liquide alimentant la colonne de mélange (6) sont comprimés sensiblement à une même première pression (P₁) différente de celle de la colonne moyenne pression (3).Air distillation process by means of a double distillation column (2) coupled to a mixing column (6), in which the mixing column is supplied to the tank with an auxiliary gas consisting of a mixture of air, and at the top with a liquid richer in oxygen than the auxiliary gas, taken from the lower part of the low pressure column (4), and oxygen is withdrawn at the top of the mixing column (6) impure constituting a production gas, characterized in that the auxiliary gas and the liquid supplying the mixing column (6) are compressed at substantially the same first pressure (P₁) different from that of the medium pressure column (3). Procédé suivant la revendication 1, caractérisé en ce que le liquide est le liquide de cuve de la colonne basse pression (4).Method according to claim 1, characterized in that the liquid is the bottom liquid of the low pressure column (4). Procédé suivant la revendication 2, caractérisé en ce que le liquide est de l'oxygène pratiquement sans azote.Method according to claim 2, characterized in that the liquid is oxygen which is practically nitrogen-free. Procédé suivant l'une quelconque des revendications 1 à 3, caractérisé en ce que ledit liquide est soutiré quelques plateaux au-dessus de la cuve de la colonne basse pression (4).Process according to any one of Claims 1 to 3, characterized in that the said liquid is drawn off a few trays above the tank of the low pressure column (4). Procédé suivant l'une quelconque des revendications 1 à 4, caractérisé en ce qu'on soutire de l'oxygène en cuve de la colonne basse pression (4) pour constituer un second gaz de production.Process according to any one of Claims 1 to 4, characterized in that oxygen is drawn off from the bottom of the low pressure column (4) to constitute a second production gas. Procédé suivant l'une quelconque des revendications 1 à 5, caractérisé en ce qu'on produit en outre de l'argon au moyen d'une colonne de distillation additionnelle de production d'argon impur (25) couplée à la colonne basse pression (4).Process according to any one of Claims 1 to 5, characterized in that argon is also produced by means of an additional distillation column for the production of impure argon (25) coupled to the low pressure column ( 4). Procédé selon l'une des revendications 1 à 6, caractérisé en ce que la première pression (P1) est supérieure d'au moins 2 x 10⁵ Pa à la pression dans la colonne moyenne pression.Method according to one of claims 1 to 6, characterized in that the first pressure (P1) is at least 2 x 10⁵ Pa higher than the pressure in the medium pressure column. Procédé selon la revendication 7, caractérisé en ce que la première pression est comprise entre 8 x 10⁵ Pa et 16 x 10⁵ Pa.Method according to claim 7, characterized in that the first pressure is between 8 x 10⁵ Pa and 16 x 10⁵ Pa. Installation de distillation d'air, du type comprenant une double colonne de distillation (2), une colonne de mélange (6), une ligne d'échange thermique (1), une source d'un gaz auxiliaire constitué d'un mélange de gaz de l'air, des moyens pour introduire le gaz auxiliaire à la base de la colonne de mélange (6), des moyens pour soutirer un liquide plus riche en oxygène que le gaz auxiliaire dans la partie inférieure de la colonne basse pression (4), des moyens (13) pour pomper ce liquide et pour l'introduire au sommet de la colonne de mélange, et des moyens pour soutirer de l'oxygène impur en tête de la colonne de mélange en tant que gaz de production de l'installation, caractérisée en ce qu'elle comprend des moyens (14) pour comprimer le gaz auxiliaire à une pression déterminée (P1) différente de celle de la colonne moyenne pression (3), et des passages pour ce gaz auxiliaire comprimé prévus dans la ligne d'échange thermique (1), et en ce que les moyens (13) de pompage portent le liquide à ladite pression déterminée (P₁).Air distillation installation, of the type comprising a double distillation column (2), a mixing column (6), a heat exchange line (1), a source of an auxiliary gas consisting of a mixture of air gas, means for introducing the auxiliary gas at the base of the mixing column (6), means for withdraw a liquid richer in oxygen than the auxiliary gas in the lower part of the low pressure column (4), means (13) for pumping this liquid and for introducing it at the top of the mixing column, and means for draw off impure oxygen at the top of the mixing column as production gas for the installation, characterized in that it comprises means (14) for compressing the auxiliary gas to a determined pressure (P1) different from that of the medium pressure column (3), and passages for this compressed auxiliary gas provided in the heat exchange line (1), and in that the pumping means (13) bring the liquid to said determined pressure (P₁ ). Installation suivant la revendication 9, caractérisée en ce que ledit liquide est soutiré en cuve de la colonne basse pression (4).Installation according to claim 9, characterized in that said liquid is withdrawn from the bottom of the low pressure column (4). Installation suivant la revendication 9, caractérisée en ce que ledit liquide est soutiré quelques plateaux au-dessus de la cuve de la colonne basse pression (4).Installation according to claim 9, characterized in that said liquid is drawn off a few trays above the tank of the low pressure column (4). Installation suivant l'une quelconque des revendications 9 à 11, caractérisée en ce qu'elle comprend des moyens pour soutirer de l'oxygène en cuve de la colonne basse pression (4) en tant que second gaz de producton de l'installation.Installation according to any one of claims 9 to 11, characterized in that it comprises means for withdrawing oxygen from the bottom of the low pressure column (4) as the second product gas of the installation. Installation suivant l'une quelconque des revendications 9 à 12, caractérisée en ce qu'elle comprend une colonne de production d'argon impur (25) couplée à la colonne basse pression (4).Installation according to any one of claims 9 to 12, characterized in that it comprises an impure argon production column (25) coupled to the low pressure column (4). Application d'un procédé suivant l'une quelconque des revendications 1 à 8 à l'alimentation en gaz d'une aciérie comprenant un haut fourneau, l'oxygène impur étant produit sous la pression du haut fourneau et étant envoyé à ce dernier.Application of a process according to any one of Claims 1 to 8 to the supply of gas to a steelworks comprising a blast furnace, the impure oxygen being produced under the pressure of the blast furnace and being sent to the latter. Application suivant la revendication 14, caractérisée en ce que, le procédé étant conforme à la revendication 3, on envoie l'oxygène pratiquement sans azote aux convertisseurs de l'aciérie.Application according to claim 14, characterized in that, the process being in accordance with claim 3, the oxygen, practically without nitrogen, is sent to the converters of the steelworks.
EP92402246A 1991-08-07 1992-08-06 Process and plant for distilling air and application in the feeding of gas to steel plants Expired - Lifetime EP0531182B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9110035 1991-08-07
FR9110035A FR2680114B1 (en) 1991-08-07 1991-08-07 METHOD AND INSTALLATION FOR AIR DISTILLATION, AND APPLICATION TO THE GAS SUPPLY OF A STEEL.

Publications (3)

Publication Number Publication Date
EP0531182A1 true EP0531182A1 (en) 1993-03-10
EP0531182B1 EP0531182B1 (en) 1996-02-21
EP0531182B2 EP0531182B2 (en) 2000-12-27

Family

ID=9415988

Family Applications (1)

Application Number Title Priority Date Filing Date
EP92402246A Expired - Lifetime EP0531182B2 (en) 1991-08-07 1992-08-06 Process and plant for distilling air and application in the feeding of gas to steel plants

Country Status (9)

Country Link
US (1) US5291737A (en)
EP (1) EP0531182B2 (en)
CN (1) CN1062656C (en)
AU (1) AU655485B2 (en)
BR (1) BR9203049A (en)
CA (1) CA2075420C (en)
DE (1) DE69208412T3 (en)
ES (1) ES2083709T5 (en)
FR (1) FR2680114B1 (en)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0636845A1 (en) * 1993-04-30 1995-02-01 The BOC Group plc Air separation
EP0697576A1 (en) * 1994-08-17 1996-02-21 The Boc Group, Inc. Air separation method and apparatus
EP0698772A1 (en) * 1994-08-25 1996-02-28 The Boc Group, Inc. Method and apparatus for producing oxygen
EP0932005A1 (en) * 1998-01-23 1999-07-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Combined oven and air separation plant and method of application
EP0932006A1 (en) * 1998-01-23 1999-07-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Combined oven and air separation plant and method of application
EP0982554A1 (en) * 1998-08-28 2000-03-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and plant for producing impure oxygen by distillation
FR2789162A1 (en) * 1999-02-01 2000-08-04 Air Liquide AIR SEPARATION PROCESS BY CRYOGENIC DISTILLATION
EP1387136A1 (en) * 2002-08-02 2004-02-04 Linde AG Process and device for producing impure oxygen by cryogenic air distillation
US6871513B2 (en) 2000-10-30 2005-03-29 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Process and installation for separation of air by cryogenic distillation integrated with an associated process
EP1666824A1 (en) * 2004-12-03 2006-06-07 Linde Aktiengesellschaft Process and device for the recovery of Argon by cryogenic separation of air
WO2007099246A2 (en) * 2006-03-03 2007-09-07 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method of integrating a blast furnace with an air gas separation unit
US7645319B2 (en) 2004-02-27 2010-01-12 L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for renovating a combined blast furnace and air/gas separation unit system
EP2703757A1 (en) 2012-09-04 2014-03-05 Linde Aktiengesellschaft Method and plant for creating liquid and gaseous oxygen products by cryogenic decomposition of air
DE102012017488A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements
DE102013009950A1 (en) 2013-06-13 2014-12-18 Linde Aktiengesellschaft Process and plant for the treatment and thermal gasification of hydrous organic feedstock
WO2014067662A3 (en) * 2012-11-02 2015-04-16 Linde Aktiengesellschaft Process for the low-temperature separation of air in an air separation plant and air separation plant

Families Citing this family (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5440884A (en) * 1994-07-14 1995-08-15 Praxair Technology, Inc. Cryogenic air separation system with liquid air stripping
FR2731781B1 (en) * 1995-03-15 1997-05-23 Air Liquide METHOD AND APPARATUS FOR VAPORIZING LIQUID FLOW
US5582036A (en) * 1995-08-30 1996-12-10 Praxair Technology, Inc. Cryogenic air separation blast furnace system
US5666823A (en) 1996-01-31 1997-09-16 Air Products And Chemicals, Inc. High pressure combustion turbine and air separation system integration
US5628207A (en) * 1996-04-05 1997-05-13 Praxair Technology, Inc. Cryogenic Rectification system for producing lower purity gaseous oxygen and high purity oxygen
US5596886A (en) * 1996-04-05 1997-01-28 Praxair Technology, Inc. Cryogenic rectification system for producing gaseous oxygen and high purity nitrogen
FR2753638B1 (en) * 1996-09-25 1998-10-30 PROCESS FOR SUPPLYING A GAS CONSUMER UNIT
FR2776057B1 (en) * 1998-03-11 2000-06-23 Air Liquide METHOD AND PLANT FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
US5865041A (en) * 1998-05-01 1999-02-02 Air Products And Chemicals, Inc. Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities
FR2801963B1 (en) 1999-12-02 2002-03-29 Air Liquide METHOD AND PLANT FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR2795496B1 (en) * 1999-06-22 2001-08-03 Air Liquide APPARATUS AND METHOD FOR SEPARATING AIR BY CRYOGENIC DISTILLATION
FR2814178B1 (en) * 2000-09-18 2002-10-18 Air Liquide SUPPLY OF OXYGEN-ENRICHED AIR TO A NON-FERROUS METAL PRODUCTION UNIT
DE10139727A1 (en) 2001-08-13 2003-02-27 Linde Ag Method and device for obtaining a printed product by low-temperature separation of air
FR2861841B1 (en) * 2003-11-04 2006-06-30 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR2862004B3 (en) * 2003-11-10 2005-12-23 Air Liquide METHOD AND INSTALLATION FOR ENRICHING A GASEOUS FLOW IN ONE OF ITS CONSTITUENTS
FR2862128B1 (en) * 2003-11-10 2006-01-06 Air Liquide PROCESS AND INSTALLATION FOR SUPPLYING HIGH-PURITY OXYGEN BY CRYOGENIC AIR DISTILLATION
FR2895068B1 (en) * 2005-12-15 2014-01-31 Air Liquide AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION
EP1845323A1 (en) * 2006-04-13 2007-10-17 Linde Aktiengesellschaft Process and device for producing a high pressure product by cryogenic separation of air
CN111271940A (en) * 2020-01-19 2020-06-12 浙江智海化工设备工程有限公司 Novel oxygen-enriched production method
EP4185824A1 (en) * 2020-07-22 2023-05-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Argon enhancing method and device

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1314605A (en) * 1961-01-26 1963-01-11 Lindes Eismaschinen Ag Process and plant for rectification for decomposition of gas at low temperature
FR2169561A6 (en) * 1971-02-01 1973-09-07 Air Liquide

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2125949B (en) * 1982-08-24 1985-09-11 Air Prod & Chem Plant for producing gaseous oxygen
US4595405A (en) * 1984-12-21 1986-06-17 Air Products And Chemicals, Inc. Process for the generation of gaseous and/or liquid nitrogen
DE3722746A1 (en) * 1987-07-09 1989-01-19 Linde Ag METHOD AND DEVICE FOR AIR DISASSEMBLY BY RECTIFICATION
FR2655137B1 (en) * 1989-11-28 1992-10-16 Air Liquide AIR DISTILLATION PROCESS AND INSTALLATION WITH ARGON PRODUCTION.
US5144808A (en) * 1991-02-12 1992-09-08 Liquid Air Engineering Corporation Cryogenic air separation process and apparatus
US5152149A (en) * 1991-07-23 1992-10-06 The Boc Group, Inc. Air separation method for supplying gaseous oxygen in accordance with a variable demand pattern

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1314605A (en) * 1961-01-26 1963-01-11 Lindes Eismaschinen Ag Process and plant for rectification for decomposition of gas at low temperature
FR2169561A6 (en) * 1971-02-01 1973-09-07 Air Liquide

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0636845A1 (en) * 1993-04-30 1995-02-01 The BOC Group plc Air separation
US5582035A (en) * 1993-04-30 1996-12-10 The Boc Group Plc Air separation
EP0697576A1 (en) * 1994-08-17 1996-02-21 The Boc Group, Inc. Air separation method and apparatus
EP0698772A1 (en) * 1994-08-25 1996-02-28 The Boc Group, Inc. Method and apparatus for producing oxygen
FR2774159A1 (en) * 1998-01-23 1999-07-30 Air Liquide COMBINED INSTALLATION OF AN OVEN AND AN AIR DISTILLATION APPARATUS AND METHOD OF IMPLEMENTING IT
EP0932006A1 (en) * 1998-01-23 1999-07-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Combined oven and air separation plant and method of application
FR2774157A1 (en) * 1998-01-23 1999-07-30 Air Liquide COMBINED INSTALLATION OF AN OVEN AND AN AIR DISTILLATION APPARATUS AND METHOD OF IMPLEMENTING IT
US6089040A (en) * 1998-01-23 2000-07-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Combined plant of a furnace and an air distillation device and implementation process
EP0932005A1 (en) * 1998-01-23 1999-07-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Combined oven and air separation plant and method of application
EP0982554A1 (en) * 1998-08-28 2000-03-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and plant for producing impure oxygen by distillation
US6247333B1 (en) 1998-08-28 2001-06-19 L'air Liquide, Societe Anonyme Pour L'etrude Et L'exploitation Des Procedes Georges Claude Process for supplying impure oxygen to a synthesis-gas production unit
FR2789162A1 (en) * 1999-02-01 2000-08-04 Air Liquide AIR SEPARATION PROCESS BY CRYOGENIC DISTILLATION
EP1026464A1 (en) * 1999-02-01 2000-08-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Air separation process by cryogenic distillation
US6295835B1 (en) 1999-02-01 2001-10-02 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for air separation by cryogenic distillation
US6871513B2 (en) 2000-10-30 2005-03-29 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Process and installation for separation of air by cryogenic distillation integrated with an associated process
EP1387136A1 (en) * 2002-08-02 2004-02-04 Linde AG Process and device for producing impure oxygen by cryogenic air distillation
US7645319B2 (en) 2004-02-27 2010-01-12 L'air Liquide Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for renovating a combined blast furnace and air/gas separation unit system
EP1666824A1 (en) * 2004-12-03 2006-06-07 Linde Aktiengesellschaft Process and device for the recovery of Argon by cryogenic separation of air
AU2007220388B2 (en) * 2006-03-03 2010-09-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method of integrating a blast furnace with an air gas separation unit
WO2007099246A3 (en) * 2006-03-03 2009-01-29 Air Liquide Method of integrating a blast furnace with an air gas separation unit
FR2898134A1 (en) * 2006-03-03 2007-09-07 Air Liquide METHOD FOR INTEGRATING A HIGH-FURNACE AND A GAS SEPARATION UNIT OF THE AIR
EA013661B1 (en) * 2006-03-03 2010-06-30 Л`Эр Ликид, Сосьете Аноним Пур Л`Этюд Э Л`Эксплуатасьон Де Проседе Жорж Клод Method of integrating a blast furnace with an air gas separation unit
WO2007099246A2 (en) * 2006-03-03 2007-09-07 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method of integrating a blast furnace with an air gas separation unit
AU2007220388B8 (en) * 2006-03-03 2011-01-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method of integrating a blast furnace with an air gas separation unit
EP2703757A1 (en) 2012-09-04 2014-03-05 Linde Aktiengesellschaft Method and plant for creating liquid and gaseous oxygen products by cryogenic decomposition of air
DE102012017484A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Process and plant for the production of liquid and gaseous oxygen products by cryogenic separation of air
DE102012017488A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements
WO2014037091A2 (en) 2012-09-04 2014-03-13 Linde Aktiengesellschaft Process and facility for generating liquid and gaseous oxygen products by low-temperature separation of air
WO2014067662A3 (en) * 2012-11-02 2015-04-16 Linde Aktiengesellschaft Process for the low-temperature separation of air in an air separation plant and air separation plant
DE102013009950A1 (en) 2013-06-13 2014-12-18 Linde Aktiengesellschaft Process and plant for the treatment and thermal gasification of hydrous organic feedstock

Also Published As

Publication number Publication date
DE69208412T3 (en) 2001-08-23
ES2083709T3 (en) 1996-04-16
US5291737A (en) 1994-03-08
EP0531182B1 (en) 1996-02-21
ES2083709T5 (en) 2001-03-16
CA2075420A1 (en) 1993-02-08
BR9203049A (en) 1993-05-04
EP0531182B2 (en) 2000-12-27
FR2680114B1 (en) 1994-08-05
DE69208412T2 (en) 1996-07-04
CN1071000A (en) 1993-04-14
AU655485B2 (en) 1994-12-22
CA2075420C (en) 2003-05-13
CN1062656C (en) 2001-02-28
AU2079892A (en) 1993-02-11
FR2680114A1 (en) 1993-02-12
DE69208412D1 (en) 1996-03-28

Similar Documents

Publication Publication Date Title
EP0531182B1 (en) Process and plant for distilling air and application in the feeding of gas to steel plants
EP0628778B2 (en) Process and high pressure gas supply unit for an air constituent consuming installation
EP0547946B2 (en) Process for the production of impure oxygen
EP0937679B1 (en) Process and apparatus for the production of carbon monoxide and hydrogen
EP0676373B1 (en) Process and installation for the production of carbon monoxide
WO2007068858A2 (en) Process for separating air by cryogenic distillation
EP1223395A1 (en) Integrated process for air separation and energy generation and plant for carrying out the process
LU88132A1 (en) METHOD FOR SUPPLYING AN OXYGEN-ENRICHED AIR STOVE, AND CORRESPONDING IRON ORE REDUCTION INSTALLATION
EP0937681B1 (en) Process and installation for the combined production of a ammoniac synthesis mixture and carbon monoxide
FR2584803A1 (en) METHOD AND INSTALLATION OF AIR DISTILLATION
FR2953004A1 (en) PROCESS FOR CRYOGENIC SEPARATION OF A NITROGEN MIXTURE AND CARBON MONOXIDE
EP1143216B1 (en) Process and apparatus for the production of oxygen enriched fluid by cryogenic distillation
EP0430803A1 (en) Process and installation for air distillation with argon production
FR2767317A1 (en) PROCESS FOR CONVERTING A FLOW CONTAINING HYDROCARBONS BY PARTIAL OXIDATION
FR2686405A1 (en) Air separation method and installation, and application of such an installation
WO2005045340A1 (en) Method and installation for supplying highly pure oxygen by cryogenic distillation of air
EP0595673A1 (en) Process and installation for the production of nitrogen and oxygen
WO2018020091A1 (en) Method and apparatus for scrubbing at cryogenic temperature in order to produce a mixture of hydrogen and nitrogen
FR2862004A1 (en) Enriching a flow of pressurised gas in one of its components by dividing the gas into two fractions, separating one fraction to obtain an enriched gas and mixing that gas with the other fraction
FR2860286A1 (en) Air separation comprises use of cryogenic distillation in installation with mixing column and double column, where vaporizer-condenser bath is used as storage to balance demand for oxygen-rich gas
FR2831250A1 (en) Air separation by cryogenic distillation using high, intermediate and low pressure columns where some of the compressed and purified feed air is sent to the intermediate pressure column
EP1690053A1 (en) Method and device for separating air by cryogenic distillation
FR2782787A1 (en) PROCESS AND PLANT FOR PRODUCING IMPURED OXYGEN BY AIR DISTILLATION
FR2825453A1 (en) Process for further purifying a nitrogen-rich feed involves adding a single column to a cryogenic distillation air separator producing a gas which is ninety percent or more nitrogen
FR2787562A1 (en) Air distillation process to produce argon

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19920814

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): BE DE ES FR IT NL SE

17Q First examination report despatched

Effective date: 19940509

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE ES FR IT NL SE

ITF It: translation for a ep patent filed

Owner name: ING. A. GIAMBROCONO & C. S.R.L.

REF Corresponds to:

Ref document number: 69208412

Country of ref document: DE

Date of ref document: 19960328

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2083709

Country of ref document: ES

Kind code of ref document: T3

PLAV Examination of admissibility of opposition

Free format text: ORIGINAL CODE: EPIDOS OPEX

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

PLBQ Unpublished change to opponent data

Free format text: ORIGINAL CODE: EPIDOS OPPO

PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

26 Opposition filed

Opponent name: LINDE AKTIENGESELLSCHAFT

Effective date: 19961121

Opponent name: THE BOC GROUP PLC

Effective date: 19961119

PLAV Examination of admissibility of opposition

Free format text: ORIGINAL CODE: EPIDOS OPEX

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

NLR1 Nl: opposition has been filed with the epo

Opponent name: LINDE AKTIENGESELLSCHAFT

Opponent name: THE BOC GROUP PLC

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

PLBF Reply of patent proprietor to notice(s) of opposition

Free format text: ORIGINAL CODE: EPIDOS OBSO

RDAH Patent revoked

Free format text: ORIGINAL CODE: EPIDOS REVO

APAC Appeal dossier modified

Free format text: ORIGINAL CODE: EPIDOS NOAPO

APAE Appeal reference modified

Free format text: ORIGINAL CODE: EPIDOS REFNO

APAC Appeal dossier modified

Free format text: ORIGINAL CODE: EPIDOS NOAPO

APAC Appeal dossier modified

Free format text: ORIGINAL CODE: EPIDOS NOAPO

PLAW Interlocutory decision in opposition

Free format text: ORIGINAL CODE: EPIDOS IDOP

PUAH Patent maintained in amended form

Free format text: ORIGINAL CODE: 0009272

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: PATENT MAINTAINED AS AMENDED

27A Patent maintained in amended form

Effective date: 20001227

AK Designated contracting states

Kind code of ref document: B2

Designated state(s): BE DE ES FR IT NL SE

ITF It: translation for a ep patent filed

Owner name: ING. A. GIAMBROCONO & C. S.R.L.

NLR2 Nl: decision of opposition
REG Reference to a national code

Ref country code: ES

Ref legal event code: DC2A

Kind code of ref document: T5

Effective date: 20010220

NLR3 Nl: receipt of modified translations in the netherlands language after an opposition procedure
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 20050719

Year of fee payment: 14

APAH Appeal reference modified

Free format text: ORIGINAL CODE: EPIDOSCREFNO

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20060807

EUG Se: european patent has lapsed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20080718

Year of fee payment: 17

Ref country code: ES

Payment date: 20080811

Year of fee payment: 17

Ref country code: DE

Payment date: 20080725

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20080726

Year of fee payment: 17

Ref country code: FR

Payment date: 20080714

Year of fee payment: 17

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20080801

Year of fee payment: 17

BERE Be: lapsed

Owner name: S.A. L'*AIR LIQUIDE POUR L'ETUDE ET L'EXPLOITATION

Effective date: 20090831

REG Reference to a national code

Ref country code: NL

Ref legal event code: V1

Effective date: 20100301

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090831

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20100301

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20100302

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20090807

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090806

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20110729

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090807

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20090831