EP0562893B1 - Process for the production of high pressure nitrogen and oxygen - Google Patents

Process for the production of high pressure nitrogen and oxygen Download PDF

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Publication number
EP0562893B1
EP0562893B1 EP93400522A EP93400522A EP0562893B1 EP 0562893 B1 EP0562893 B1 EP 0562893B1 EP 93400522 A EP93400522 A EP 93400522A EP 93400522 A EP93400522 A EP 93400522A EP 0562893 B1 EP0562893 B1 EP 0562893B1
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EP
European Patent Office
Prior art keywords
pressure
nitrogen
oxygen
column
compressor
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EP93400522A
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German (de)
French (fr)
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EP0562893B2 (en
EP0562893A1 (en
Inventor
Yves Koeberle
Jean-Pierre Tranier
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04121—Steam turbine as the prime mechanical driver
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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
    • F25J3/04248—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
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—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
    • 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
    • F25J3/04539—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
    • F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
    • 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
    • F25J2200/20—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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the present invention relates to a process for the simultaneous production on the one hand of pure nitrogen under a high pressure of nitrogen and on the other hand of oxygen, by air distillation in a double distillation column comprising a medium column pressure and a low pressure column of the "minaret" type producing pure nitrogen at the head.
  • a particular application of the invention is the simultaneous production of a portion of high purity nitrogen, containing less than 10 ppm of oxygen, in large quantity (that is to say representing at least 20% and typically more 30% of the treated air flow), under 50 to 60 bar, for a unit for manufacturing ammonia, and on the other hand oxygen of medium to high purity, ie 95 to 99.5% in moles, at a pressure of the order of 65 bar with a high extraction yield, for the production of hydrogen by reaction of oxygen with heavy hydrocarbons, the hydrogen being intended to supply the same ammonia manufacturing unit .
  • low pressure column of the minaret type means a low pressure column forming part of a double air distillation column, the upper end part of which is supplied at the head with “upper lean liquid” (nitrogen practically pure) withdrawn at the head of the medium pressure column and relaxed, and produces pure nitrogen at the head at low pressure.
  • US-A-2,982,108 which discloses a process as defined in the preamble of claim 1, describes a process for the simultaneous production of pressurized nitrogen and oxygen in which a compressor is used to pressurize the nitrogen produced up to '' at a pressure which cannot exceed 40 bar, if it is assumed that the compressor has at most six wheels.
  • a process for the simultaneous production, on the one hand of pure nitrogen under a high nitrogen pressure, on the other hand of oxygen, by distillation of air in a double distillation column comprising a medium pressure column and a low pressure column of the "minaret" type producing pure nitrogen at the top, in which after heating the nitrogen from the low pressure column, it is compressed at high pressure by means of a single nitrogen compressor of the centrifugal type having at most six compression wheels, characterized in that the low pressure column is operated under a pressure of the order of P N / ⁇ N , where P N denotes the high nitrogen pressure and ⁇ N the rate of compression of said nitrogen compressor.
  • the nitrogen compressor and the air compressor can in particular be connected to a common power source.
  • the installation shown in the drawings is intended to produce on the one hand, under 55 bar, high purity nitrogen gas (typically containing less than 10 ppm of oxygen), in a flow rate at least equal to 20% of the flow rate treated air, and on the other hand, under 65 bar, oxygen having a purity of 95 to 99.5%, with a high extraction yield.
  • high purity nitrogen gas typically containing less than 10 ppm of oxygen
  • 65 bar oxygen having a purity of 95 to 99.5%
  • the installation essentially comprises an air compressor 1, an apparatus 2 for purifying the air by adsorption, a heat exchange line 3 of the counter-current type, a double distillation column 4, an expansion turbine. 5, a liquid oxygen pump 6, a nitrogen compressor 7, an oxygen compressor 8 and an energy source 9 constituted for example by a steam turbine.
  • the double column 4 comprises a medium pressure column 10 surmounted by a low pressure column 11 whose upper end part forms a minaret 11A for producing pure nitrogen under low pressure.
  • a condenser-vaporizer 12 puts the overhead vapor (practically pure nitrogen) from column 10 into heat exchange relationship with the tank liquid (oxygen from determined purity) of column 11.
  • a pipe fitted with an expansion valve 13 makes it possible to raise the "rich liquid” (oxygen-enriched air) from the tank of the column 10 to an intermediate point of the column 11;
  • a pipe fitted with an expansion valve 14 makes it possible to raise "lower lean liquid” (impure nitrogen) from an intermediate point of the column 10 at the base of the minaret 11A;
  • a pipe fitted with an expansion valve 15 makes it possible to raise the "upper lean liquid” (practically pure nitrogen) from the head of the column 10 to the top of the minaret.
  • the nitrogen compressor 7 consists of a single three-stage compressor.
  • the first two stages each include two compression wheels and have average compression ratios per wheel of 2 and 1.73 respectively, while the third stage comprises a single compression wheel having a compression ratio of 1.83.
  • the overall compression ratio of the compressor is therefore 22.
  • Each wheel has a coolant at its outlet.
  • the oxygen compressor 8 also consists of a single compressor. This compressor has six wheels with an average compression ratio per wheel of 1.37. The overall compression ratio is therefore 6.5.
  • the shaft 16 of the compressor 7 is coupled to the shaft 17 of the compressor 1 by a coupling 18, and the assembly is driven by the common energy source 9.
  • the shaft 16 can drive the different stages of the compressor 7 by means of speed multipliers suitable for each stage.
  • the compressor 8 is driven by a separate energy source 19.
  • the low pressure is chosen so that, multiplied by the compression ratio of the compressor 7, it provides the desired high production pressure for nitrogen.
  • the incoming air is compressed to 11 bars in the compressor 1, purified in 2, cooled from the hot end to the cold end of the exchange line 3, and introduced in the vicinity of its dew point in the tank of the column 10
  • the low pressure pure nitrogen leaving the gaseous top of the minaret 11A and warmed to room temperature from the cold end to the hot end of the exchange line is introduced at the suction of the first stage of the compressor 7, with the possible exception of a flow of nitrogen produced at low pressure via a pipe 20.
  • the high pressure nitrogen is produced at the discharge of the third stage of the compressor and discharged via a pipe 21.
  • Compressor 7 is also used as a nitrogen cycle compressor. Indeed, medium pressure nitrogen is drawn off at the top of the column 10, via a line 22, warmed to ambient temperature in the exchange line and introduced via a line 23 at the suction of the second stage of the compressor 7 Nitrogen at high cycle pressure is discharged from this second stage via a line 24, cooled, liquefied and sub-cooled in the exchange line, expanded to medium pressure in an expansion valve 25 and introduced at the top of column 10.
  • the flow of nitrogen flowing in line 24 is greater by a predetermined amount than the flow of nitrogen flowing in line 23.
  • the difference constitutes an additional flow of liquid nitrogen, said rectification support, introduced at reflux at the top of column 10. This flow rate is taken from the low pressure nitrogen stream drawn in by the first stage of the compressor 7.
  • Impure nitrogen constituting the residual gas of the installation, is drawn off at the base of the minaret 11A via a pipe 25, heated to an intermediate temperature in the exchange line, taken out of the latter, expanded to atmospheric pressure in a turbine 5 which keeps the installation cold, then reintroduced into the exchange line, warmed up to room temperature, and finally used to regenerate the adsorption bottles of the device 2 and evacuated from installation via a pipe 26.
  • Oxygen at 65 bar is produced as follows.
  • the desired liquid oxygen flow rate is withdrawn from the bottom of the column 11, brought by the pump 6 to an intermediate pressure of oxygen, vaporized and warmed to room temperature in the exchange line 3, then compressed to the pressure of compressor production 8.
  • the vaporization of the liquid oxygen under the intermediate oxygen pressure is carried out by condensation of the nitrogen under the high cycle pressure, with a subcritical value for this high pressure, for example 30 bars. This value corresponds to a vaporization of liquid oxygen at about 11 bars, which is therefore the pressure supplied by the pump 6.

Description

La présente invention est relative à un procédé de production simultanée d'une part d'azote pur sous une haute pression d'azote et d'autre part d'oxygène, par distillation d'air dans une double colonne de distillation comprenant une colonne moyenne pression et une colonne basse pression du type "à minaret" produisant l'azote pur en tête.The present invention relates to a process for the simultaneous production on the one hand of pure nitrogen under a high pressure of nitrogen and on the other hand of oxygen, by air distillation in a double distillation column comprising a medium column pressure and a low pressure column of the "minaret" type producing pure nitrogen at the head.

Une application particulière de l'invention est la production simultanée d'une part d'azote à haute pureté, contenant moins de 10 ppm d'oxygène, en grande quantité (c'est-à-dire représentant au moins 20 % et typiquement plus de 30 % du débit d'air traité), sous 50 à 60 bar, pour une unité de fabrication d'ammoniac, et d'autre part d'oxygène de pureté moyenne à haute, soit 95 à 99,5 % en moles, à une pression de l'ordre de 65 bar avec un rendement d'extraction élevé, pour la production d'hydrogène par réaction de l'oxygène sur des hydrocarbures lourds, l'hydrogène étant destiné à alimenter la même unité de fabrication d'ammoniac.A particular application of the invention is the simultaneous production of a portion of high purity nitrogen, containing less than 10 ppm of oxygen, in large quantity (that is to say representing at least 20% and typically more 30% of the treated air flow), under 50 to 60 bar, for a unit for manufacturing ammonia, and on the other hand oxygen of medium to high purity, ie 95 to 99.5% in moles, at a pressure of the order of 65 bar with a high extraction yield, for the production of hydrogen by reaction of oxygen with heavy hydrocarbons, the hydrogen being intended to supply the same ammonia manufacturing unit .

On entend par "colonne basse pression du type à minaret", une colonne basse pression faisant partie d'une double colonne de distillation d'air, dont la partie d'extrémité supérieure est alimentée en tête par du "liquide pauvre supérieur" (azote pratiquement pur) soutiré en tête de la colonne moyenne pression et détendu, et produit en tête de l'azote pur sous la basse pression.The term "low pressure column of the minaret type" means a low pressure column forming part of a double air distillation column, the upper end part of which is supplied at the head with "upper lean liquid" (nitrogen practically pure) withdrawn at the head of the medium pressure column and relaxed, and produces pure nitrogen at the head at low pressure.

Les pressions dont il est question ici sont des pressions absolues. De plus, on entend par "basse pression" et "moyenne pression" les pressions de fonctionnement de la colonne basse pression et de la colonne moyenne pression de la double colonne respectivement.The pressures we are talking about here are absolute pressures. In addition, "low pressure" and "medium pressure" are understood to mean the operating pressures of the low pressure column and of the medium pressure column of the double column respectively.

US-A-2.982.108, qui divulgue un procédé tel que défini dans le préambule de la revendication 1, décrit un procédé de production simultanée d'azote sous pression et d'oxygène dans lequel un compresseur sert à pressuriser l'azote produit jusqu'à une pression qui ne peut pas excéder 40 bar, si on suppose que le compresseur a au plus six roues.US-A-2,982,108, which discloses a process as defined in the preamble of claim 1, describes a process for the simultaneous production of pressurized nitrogen and oxygen in which a compressor is used to pressurize the nitrogen produced up to '' at a pressure which cannot exceed 40 bar, if it is assumed that the compressor has at most six wheels.

A cet effet, selon l'invention, il est prévu un procédé de production simultanée, d'une part d'azote pur sous une haute pression d'azote, d'autre part d'oxygène, par distillation d'air dans une double colonne de distillation comprenant une colonne moyenne pression et une colonne basse pression du type "à minaret" produisant l'azote pur en tête, dans lequel après réchauffement de l'azote issu de la colonne basse pression, on le comprime à la haute pression au moyen d'un unique compresseur d'azote de type centrifuge ayant au plus six roues de compression, caractérisé en ce que l'on fait fonctionner la colonne basse pression sous une pression de l'ordre de PN/ρN, où PN désigne la haute pression d'azote et ρN le taux de compression dudit compresseur d'azote.To this end, according to the invention, there is provided a process for the simultaneous production, on the one hand of pure nitrogen under a high nitrogen pressure, on the other hand of oxygen, by distillation of air in a double distillation column comprising a medium pressure column and a low pressure column of the "minaret" type producing pure nitrogen at the top, in which after heating the nitrogen from the low pressure column, it is compressed at high pressure by means of a single nitrogen compressor of the centrifugal type having at most six compression wheels, characterized in that the low pressure column is operated under a pressure of the order of P N / ρ N , where P N denotes the high nitrogen pressure and ρ N the rate of compression of said nitrogen compressor.

Les procédés dans lesquels la haute pression de l'azote produit n'est pas supérieure à 40 bar absolus ne sont pas couverts par la revendication 1.Processes in which the high pressure of the nitrogen produced is not more than 40 bar absolute are not covered by claim 1.

Suivant un mode particulier de réalisation de l'invention:

  • lorsque l'on produit l'oxygène sous une haute pression d'oxygène supérieure à 10 bar absolus environ, de façon avantageuse, on amène par pompe de l'oxygène liquide soutiré en cuve de la colonne basse pression à une pression intermédiaire d'oxygène et, après vaporisation et réchauffement de l'oxygène, on le comprime à la haute pression d'oxygène au moyen d'un unique compresseur d'oxygène de type centrifuge ayant au plus six roues de compression, la pression intermédiaire d'oxygène étant de l'ordre de Po/ρo, où Po désigne la haute pression d'oxygène et ρo le taux de compression dudit compresseur d'oxygène ;
  • dans ce cas, de préférence :
    • * on utilise un compresseur d'azote à trois étages ayant chacun au plus deux roues, et on utilise en outre le deuxième étage pour comprimer à une pression intermédiaire entre la moyenne pression et la haute pression un débit d'azote de cycle soutiré de la colonne moyenne pression et réchauffé, l'azote de cycle comprimé étant refroidi, liquéfié, détendu à la moyenne pression et introduit en tête de la colonne moyenne pression ;
    • * l'azote de cycle est comprimé à une pression subcritique pour laquelle la température de condensation de l'azote est légèrement supérieure à la température de vaporisation de l'oxygène sous ladite pression intermédiaire d'oxygène.
According to a particular embodiment of the invention:
  • when oxygen is produced under a high oxygen pressure greater than approximately 10 bar absolute, advantageously, liquid oxygen drawn off from the bottom of the low pressure column is pumped to an intermediate oxygen pressure and, after vaporization and heating of the oxygen, it is compressed to the high oxygen pressure by means of a single oxygen compressor of the centrifugal type having at most six compression wheels, the intermediate oxygen pressure being the order of P o / ρ o , where P o denotes the high oxygen pressure and ρ o the compression ratio of said oxygen compressor;
  • in this case, preferably:
    • * a three-stage nitrogen compressor is used, each having at most two wheels, and the second stage is also used to compress at a pressure intermediate between the medium pressure and the high pressure a cycle nitrogen flow withdrawn from the medium pressure column and reheated, the compressed cycle nitrogen being cooled, liquefied, expanded to medium pressure and introduced at the head of the medium pressure column;
    • * the cycle nitrogen is compressed to a subcritical pressure for which the nitrogen condensation temperature is slightly higher than the oxygen vaporization temperature under said intermediate oxygen pressure.

Suivant encore un autre mode particulier de réalisation de l'invention:

  • on utilise un compresseur d'azote à trois étages ayant chacun au plus deux roues, et on utilise en outre les deux premiers étages pour comprimer de la basse pression à une pression intermédiaire entre la moyenne pression et la haute pression un débit d'azote, dit de soutien de rectification, liquéfié, détendu à la moyenne pression et introduit en tête de la colonne moyenne pression ;
  • on assure le maintien en froid de l'installation de distillation d'air en détendant dans une turbine de l'azote impur soutiré de la colonne basse pression, cet azote impur, après détente et réchauffement, étant de préférence utilisé pour régénérer des bouteilles d'adsorbant servant à l'épuration de l'air traité.
According to yet another particular embodiment of the invention:
  • a three-stage nitrogen compressor is used, each having at most two wheels, and the first two stages are also used to compress from low pressure to an intermediate pressure between the medium pressure and high pressure a flow of nitrogen, known as rectification support, liquefied, expanded at medium pressure and introduced at the head of the medium pressure column;
  • the air distillation installation is kept cold by expelling impure nitrogen withdrawn from the low pressure column in a turbine, this impure nitrogen, after expansion and reheating, is preferably used to regenerate bottles of adsorbent used to purify the treated air.

Le compresseur d'azote et le compresseur d'air peuvent en particulier être reliés à une source motrice commune.The nitrogen compressor and the air compressor can in particular be connected to a common power source.

Un exemple de mise en oeuvre de l'invention va maintenant être décrit en regard du dessin annexé, dont la figure unique représente schématiquement une installation de production simultanée d'azote et d'oxygène sous haute pression pour réaliser un procédé conforme à l'invention.An example of implementation of the invention will now be described with reference to the accompanying drawing, the single figure of which schematically represents an installation for the simultaneous production of nitrogen and oxygen under high pressure to carry out a process in accordance with the invention .

L'installation représentée aux dessins est destinée à produire d'une part, sous 55 bar, de l'azote gazeux à haute pureté (contenant typiquement moins de 10 ppm d'oxygène), en un débit au moins égal à 20 % du débit d'air traité, et d'autre part, sous 65 bar, de l'oxygène ayant une pureté de 95 à 99,5 %, avec un rendement d'extraction élevé. Ces deux gaz sous haute pression seront utilisés sur un même site : on produira de l'hydrogène par réaction de l'oxygène sur des hydrocarbures lourds, et l'on fera réagir cet hydrogène et l'azote pour produire de l'ammoniac.The installation shown in the drawings is intended to produce on the one hand, under 55 bar, high purity nitrogen gas (typically containing less than 10 ppm of oxygen), in a flow rate at least equal to 20% of the flow rate treated air, and on the other hand, under 65 bar, oxygen having a purity of 95 to 99.5%, with a high extraction yield. These two gases under high pressure will be used on the same site: hydrogen will be produced by reacting oxygen with heavy hydrocarbons, and this hydrogen and nitrogen will be reacted to produce ammonia.

L'installation comprend essentiellement un compresseur d'air 1, un appareil 2 d'épuration de l'air par adsorption, une ligne d'échange thermique 3 du type à contre-courant, une double colonne de distillation 4, une turbine de détente 5, une pompe d'oxygène liquide 6, un compresseur d'azote 7, un compresseur d'oxygène 8 et une source d'énergie 9 constituée par exemple par une turbine à vapeur.The installation essentially comprises an air compressor 1, an apparatus 2 for purifying the air by adsorption, a heat exchange line 3 of the counter-current type, a double distillation column 4, an expansion turbine. 5, a liquid oxygen pump 6, a nitrogen compressor 7, an oxygen compressor 8 and an energy source 9 constituted for example by a steam turbine.

La double colonne 4 comprend une colonne moyenne pression 10 surmontée d'une colonne basse pression 11 dont la partie d'extrémité supérieure forme un minaret 11A de production d'azote pur sous la basse pression. Un condenseur-vaporiseur 12 met en relation d'échange thermique la vapeur de tête (azote pratiquement pur) de la colonne 10 et le liquide de cuve (oxygène de pureté déterminée) de la colonne 11.The double column 4 comprises a medium pressure column 10 surmounted by a low pressure column 11 whose upper end part forms a minaret 11A for producing pure nitrogen under low pressure. A condenser-vaporizer 12 puts the overhead vapor (practically pure nitrogen) from column 10 into heat exchange relationship with the tank liquid (oxygen from determined purity) of column 11.

Comme il est classique, une conduite équipée d'une vanne de détente 13 permet de remonter du "liquide riche" (air enrichi en oxygène) de la cuve de la colonne 10 à un point intermédiaire de la colonne 11; une conduite équipée d'une vanne de détente 14 permet de remonter du "liquide pauvre inférieur"(azote impur) d'un point intermédiaire de la colonne 10 à la base du minaret 11A; et une conduite équipée d'une vanne de détente 15 permet de remonter du "liquide pauvre supérieur" (azote pratiquement pur) de la tête de la colonne 10 au sommet du minaret.As is conventional, a pipe fitted with an expansion valve 13 makes it possible to raise the "rich liquid" (oxygen-enriched air) from the tank of the column 10 to an intermediate point of the column 11; a pipe fitted with an expansion valve 14 makes it possible to raise "lower lean liquid" (impure nitrogen) from an intermediate point of the column 10 at the base of the minaret 11A; and a pipe fitted with an expansion valve 15 makes it possible to raise the "upper lean liquid" (practically pure nitrogen) from the head of the column 10 to the top of the minaret.

Le compresseur d'azote 7 est constitué d'un compresseur unique à trois étages. Les deux premiers étages comprennent chacun deux roues de compression et ont des taux de compression moyens par roue de 2 et 1,73 respectivement, tandis que le troisième étage comprend une roue de compression unique ayant un taux de compression de 1,83. Le taux de compression global du compresseur est donc 22. Chaque roue comporte à sa sortie un réfrigérant.The nitrogen compressor 7 consists of a single three-stage compressor. The first two stages each include two compression wheels and have average compression ratios per wheel of 2 and 1.73 respectively, while the third stage comprises a single compression wheel having a compression ratio of 1.83. The overall compression ratio of the compressor is therefore 22. Each wheel has a coolant at its outlet.

Le compresseur d'oxygène 8 est également constitué d'un compresseur unique. Ce compresseur possède six roues ayant un taux de compression moyen par roue de 1,37. Le taux de compression global est donc 6,5.The oxygen compressor 8 also consists of a single compressor. This compressor has six wheels with an average compression ratio per wheel of 1.37. The overall compression ratio is therefore 6.5.

L'arbre 16 du compresseur 7 est couplé à l'arbre 17 du compresseur 1 par un accouplement 18, et l'ensemble est entraîné par la source d'énergie commune 9. Eventuellement, l'arbre 16 peut entraîner les différents étages du compresseur 7 par l'intermédiaire de multiplicateurs de vitesse appropriés à chaque étage. Le compresseur 8 est entraîné par une source d'énergie séparée 19.The shaft 16 of the compressor 7 is coupled to the shaft 17 of the compressor 1 by a coupling 18, and the assembly is driven by the common energy source 9. Optionally, the shaft 16 can drive the different stages of the compressor 7 by means of speed multipliers suitable for each stage. The compressor 8 is driven by a separate energy source 19.

La basse pression est choisie de manière que, multipliée par le taux de compression du compresseur 7, elle fournisse la haute pression de production désirée pour l'azote. Ainsi, en négligeant les pertes de charge, pour une haute pression d'azote de 55 bars, on choisit comme basse pression 55/22 = 2,5 bars. Pour un écart de température de 2°C dans le vaporiseur-condenseur 12, ceci correspond à une moyenne pression de l'ordre de 11 bars.The low pressure is chosen so that, multiplied by the compression ratio of the compressor 7, it provides the desired high production pressure for nitrogen. Thus, neglecting the pressure drops, for a high nitrogen pressure of 55 bars, the low pressure is chosen 55/22 = 2.5 bars. For a temperature difference of 2 ° C in the vaporizer-condenser 12, this corresponds to an average pressure of the order of 11 bars.

Ainsi, l'air entrant est comprimé à 11 bars dans le compresseur 1, épuré en 2, refroidi du bout chaud au bout froid de la ligne d'échange 3, et introduit au voisinage de son point de rosée en cuve de la colonne 10. L'azote basse pression pur sortant gazeux du sommet du minaret 11A et réchauffé à la température ambiante du bout froid au bout chaud de la ligne d'échange est introduit à l'aspiration du premier étage du compresseur 7, à l'exception éventuellement d'un débit d'azote produit en basse pression via une conduite 20. L'azote haute pression est produit au refoulement du troisième étage du compresseur et évacué via une conduite 21.Thus, the incoming air is compressed to 11 bars in the compressor 1, purified in 2, cooled from the hot end to the cold end of the exchange line 3, and introduced in the vicinity of its dew point in the tank of the column 10 The low pressure pure nitrogen leaving the gaseous top of the minaret 11A and warmed to room temperature from the cold end to the hot end of the exchange line is introduced at the suction of the first stage of the compressor 7, with the possible exception of a flow of nitrogen produced at low pressure via a pipe 20. The high pressure nitrogen is produced at the discharge of the third stage of the compressor and discharged via a pipe 21.

Le compresseur 7 est également utilisé comme compresseur de cycle à azote. En effet, de l'azote moyenne pression est soutiré en tête de la colonne 10, via une conduite 22, réchauffé à la température ambiante dans la ligne d'échange et introduit via une conduite 23 à l'aspiration du deuxième étage du compresseur 7. De l'azote à la haute pression de cycle est sorti au refoulement de ce deuxième étage via une conduite 24, refroidi, liquéfié et sous-refroidi dans la ligne d'échange, détendu à la moyenne pression dans une vanne de détente 25 et introduit en tête de la colonne 10.Compressor 7 is also used as a nitrogen cycle compressor. Indeed, medium pressure nitrogen is drawn off at the top of the column 10, via a line 22, warmed to ambient temperature in the exchange line and introduced via a line 23 at the suction of the second stage of the compressor 7 Nitrogen at high cycle pressure is discharged from this second stage via a line 24, cooled, liquefied and sub-cooled in the exchange line, expanded to medium pressure in an expansion valve 25 and introduced at the top of column 10.

Grâce à des moyens de réglage de débit non représentés, le débit d'azote circulant dans la conduite 24 est supérieur d'une quantité prédéterminée au débit d'azote circulant dans la conduite 23. La différence constitue un débit d'azote liquide additionnel, dit de soutien de rectification, introduit en reflux en tête de la colonne 10. Ce débit est prélevé sur le courant d'azote basse pression aspiré par le premier étage du compresseur 7.By means of flow adjustment means not shown, the flow of nitrogen flowing in line 24 is greater by a predetermined amount than the flow of nitrogen flowing in line 23. The difference constitutes an additional flow of liquid nitrogen, said rectification support, introduced at reflux at the top of column 10. This flow rate is taken from the low pressure nitrogen stream drawn in by the first stage of the compressor 7.

De l'azote impur, constituant le gaz résiduaire de l'installation, est soutiré à la base du minaret 11A via une conduite 25, réchauffé à une température intermédiaire dans la ligne d'échange, sorti de cette dernière, détendu à la pression atmosphérique dans une turbine 5 qui assure le maintien en froid de l'installation, puis réintroduit dans la ligne d'échange, réchauffé jusqu'à la température ambiante, et enfin utilisé pour régénérer les bouteilles d'adsorption de l'appareil 2 et évacué de l'installation via une conduite 26.Impure nitrogen, constituting the residual gas of the installation, is drawn off at the base of the minaret 11A via a pipe 25, heated to an intermediate temperature in the exchange line, taken out of the latter, expanded to atmospheric pressure in a turbine 5 which keeps the installation cold, then reintroduced into the exchange line, warmed up to room temperature, and finally used to regenerate the adsorption bottles of the device 2 and evacuated from installation via a pipe 26.

L'oxygène sous 65 bars est produit de la manière suivante.Oxygen at 65 bar is produced as follows.

Le débit d'oxygène liquide désiré est soutiré en cuve de la colonne 11, amené par la pompe 6 à une pression intermédiaire d'oxygène, vaporisé et réchauffé à la température ambiante dans la ligne d'échange 3, puis comprimé à la pression de production par le compresseur 8.The desired liquid oxygen flow rate is withdrawn from the bottom of the column 11, brought by the pump 6 to an intermediate pressure of oxygen, vaporized and warmed to room temperature in the exchange line 3, then compressed to the pressure of compressor production 8.

Pour limiter au maximum les irréversibilités thermodynamiques dans la ligne d'échange, on fait en sorte que la vaporisation de l'oxygène liquide sous la pression intermédiaire d'oxygène s'effectue par condensation de l'azote sous la haute pression de cycle, avec une valeur subcritique pour cette haute pression, soit par exemple 30 bars. Cette valeur correspond à une vaporisation d'oxygène liquide sous environ 11 bars, qui est donc la pression fournie par la pompe 6.To limit thermodynamic irreversibilities in the exchange line as much as possible, the vaporization of the liquid oxygen under the intermediate oxygen pressure is carried out by condensation of the nitrogen under the high cycle pressure, with a subcritical value for this high pressure, for example 30 bars. This value corresponds to a vaporization of liquid oxygen at about 11 bars, which is therefore the pressure supplied by the pump 6.

Les considérations ci-dessus donnent les pressions pour les différents étages du compresseur 7 : 2,5 bars à l'entrée du premier étage, 11 bars à l'entrée du deuxième étage, 30 bars à l'entrée du troisième étage et 55 bars à la sortie de ce troisième étage.The above considerations give the pressures for the different stages of the compressor 7: 2.5 bars at the entry of the first stage, 11 bars at the entry of the second stage, 30 bars at the entry of the third stage and 55 bars at the exit of this third floor.

On peut montrer que le procédé décrit ci-dessus apporte un gain en investissement, par rapport au procédé classique où la basse pression est choisie légèrement supérieure à 1 bar, dès que le débit d'azote produit est au moins égal à 20% du débit d'air traité. Lorsque la production d'azote est supérieure à environ 30% du débit d'air, il apporte en outre un gain en énergie. Par ailleurs, le fait d'épurer l'air entrant sous 11 bars est très avantageux du point de vue économique.It can be shown that the process described above brings a gain in investment, compared to the conventional process where the low pressure is chosen slightly greater than 1 bar, as soon as the flow of nitrogen produced is at least equal to 20% of the flow of treated air. When nitrogen production is greater than about 30% of the air flow, it also provides energy savings. Furthermore, the fact of purifying the incoming air under 11 bars is very advantageous from the economic point of view.

Claims (6)

  1. Process for simultaneously producing, on the one hand pure nitrogen at a high nitrogen pressure and on the other hand oxygen, by distilling air in a double distillation column (4) comprising a medium pressure column (10) and a low pressure column (11) of the "minaret" type producing pure nitrogen at the top, in which, after the nitrogen coming from the low pressure column (11) is reheated, it is compressed to the high pressure by means of a single nitrogen compressor (7) of the centrifuge type having at most six compression wheels, characterized in that the low pressure column (11) is operated at a pressure of the order of PN/ρN, where PN denotes the high nitrogen pressure and ρN denotes the compression ratio of the said nitrogen compressor;
       processes in which the high nitrogen pressure is no greater than 40 bar absolute are not covered by this claim.
  2. Process according to claim 1, in which oxygen is produced at a high oxygen pressure greater than about 10 bar absolute, characterized in that liquid oxygen withdrawn from the vessel of the low pressure column (11) is brought by a pump (6) to an intermediate oxygen pressure and, after the oxygen is vaporized and reheated, it is compressed to the high oxygen pressure by means of a single oxygen compressor (8) of the centrifuge type having at most six compression wheels, the intermediate oxygen pressure being of the order of Po/ρo, where Po denotes the high oxygen pressure and ρo denotes the compression ratio of the said oxygen compressor.
  3. Process according to claim 2, characterized in that a nitrogen compressor (7) is used having three stages, each of these having at most two wheels, and in addition the second stage is used to compress, to a pressure intermediate between the medium pressure and the high pressure, a flow of cycle nitrogen withdrawn from the medium pressure column (10) and reheated, the compressed cycle nitrogen being cooled, liquefied, expanded to the medium pressure and introduced at the top of the medium pressure column (10).
  4. Process according to claim 3, characterized in that the cycle nitrogen is compressed to a sub-critical pressure for which the condensation temperature of nitrogen is slightly greater than the vaporization temperature of oxygen at the said intermediate oxygen pressure.
  5. Process according to any one of claims 1 to 4, characterized in that a nitrogen compressor (7) is used having three stages, each having at most two wheels, and in addition the first two stages are used to compress, from the low pressure to an intermediate pressure between the medium pressure and the high pressure, a flow of nitrogen, the so-called rectification maintenance nitrogen, withdrawn from the top of the low pressure column (11) and reheated, this compressed nitrogen being cooled, liquefied, expanded to the medium pressure and introduced at the top of the medium pressure column (10).
  6. Process according to any one of claims 1 to 5, characterized in that the air distillation plant is kept cold by expanding impure nitrogen withdrawn from the low pressure column (11) in a turbine (5), this impure nitrogen, after expansion and reheating, being preferably used to regenerate adsorbent bottles (2) serving to purify the treated air.
EP93400522A 1992-03-24 1993-03-02 Process for the production of high pressure nitrogen and oxygen Expired - Lifetime EP0562893B2 (en)

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FR9203501 1992-03-24
FR9203501A FR2689224B1 (en) 1992-03-24 1992-03-24 PROCESS AND PLANT FOR THE PRODUCTION OF NITROGEN AT HIGH PRESSURE AND OXYGEN.

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EP0562893B2 (en) 2000-12-20
EP0562893A1 (en) 1993-09-29
DE69310429D1 (en) 1997-06-12
US5341647A (en) 1994-08-30
FR2689224B1 (en) 1994-05-06
CA2092140C (en) 1998-08-18
CA2092140A1 (en) 1993-09-25
ES2101256T3 (en) 1997-07-01
DE69310429T3 (en) 2001-08-23
ES2101256T5 (en) 2001-03-16
FR2689224A1 (en) 1993-10-01
ZA932796B (en) 1993-09-30
DE69310429T2 (en) 1997-12-11

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