EP0789208B1 - Verfahren und Einrichtung zur Herstellung von gasförmigem Sauerstoff unter hohem Druck - Google Patents

Verfahren und Einrichtung zur Herstellung von gasförmigem Sauerstoff unter hohem Druck Download PDF

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Publication number
EP0789208B1
EP0789208B1 EP97400222A EP97400222A EP0789208B1 EP 0789208 B1 EP0789208 B1 EP 0789208B1 EP 97400222 A EP97400222 A EP 97400222A EP 97400222 A EP97400222 A EP 97400222A EP 0789208 B1 EP0789208 B1 EP 0789208B1
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Prior art keywords
air
pressure
column
liquid
approximately
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French (fr)
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EP0789208A1 (de
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Maurice Grenier
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA a Directoire et Conseil de Surveillance 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04733—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction
    • F25J3/04739—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction in combination with an auxiliary pure argon column
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • 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
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude 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
    • Y10S62/939—Partial feed stream expansion, air
    • Y10S62/94—High pressure column

Definitions

  • the present invention relates to a process for producing gaseous oxygen under high pressure at least about 30 bars.
  • the invention applies in particular to the production of large quantities, typically of at least 500 tonnes per day of oxygen gas under high pressure.
  • the pressures in question are absolute pressures.
  • pump processes Many processes for pumping and vaporizing liquid oxygen, called “pump processes” have been proposed (see in particular EP-A-0672878), and the invention has intended to provide a process of the same type that is particularly advantageous from the point of view of spent specific energy.
  • This process can include one or more features of claims 2 to 7.
  • the invention also relates to a installation according to claim 8, intended for the implementation of a method as defined above.
  • the installation includes a heat exchanger additional heat to sub-cool the liquid withdrawn from the tank of the medium pressure column by vaporization of liquid oxygen withdrawn from the tank of the low pressure column.
  • the installation shown in Figure 1 is intended to produce gaseous oxygen under a pressure at least equal to approximately 30 bars.
  • She basically includes a double column of distillation 1, a heat exchange line main 2 consisting of at least one body of brazed clad type exchanger, a sub-cooler 3, an air compressor 4, a device 5 purification by adsorption of air into water and CO2, a first air booster 6, a second air booster 7, an expansion turbine 8 and a pump liquid oxygen 9.
  • the double column consists, conventionally, a medium pressure column 10 operating under approximately 5 to 6 bars and overcome a low pressure column 11 operating slightly above atmospheric pressure, with, in the tank of the latter, a vaporizer-condenser 12 which relates to heat exchange liquid oxygen from the low pressure column tank with the top nitrogen of the medium pressure column.
  • the air to be distilled, fully compressed by compressor 4 on average pressure and purified in 5, is divided into two streams.
  • the first stream is cooled under this medium pressure in passages 13 of the line 20 which extend from the hot end to the end cold of it.
  • This medium pressure air comes out of the exchange line near its dew point and is introduced at the base of the middle column pressure 10.
  • the rest of the air coming out of the appliance 5 is overpressed in 6 to an intermediate pressure and is divided in turn into two streams.
  • the first flow, at this pressure intermediate, is cooled in passages 14 of the exchange line up to an intermediate temperature T1. Part of this flow eventually continues cooling, and is liquefied, to the cold end of the trade line and then is relaxed to the mean pressure in an expansion valve 15 and distributed in two currents: a first current sent to the base of column 10, and a second sub-cooled stream in 3, relaxed at low pressure in a valve trigger 16 and sent to column 11. The rest of the first stream came off the exchange line at the intermediate temperature T1, expanded in the turbine 6 at medium pressure and introduced at the base of the column 10.
  • the second compressed air flow is at again pressurized, up to a second high pressure of the order of 60 to 80 bars, by the booster 7, then cooled and liquefied in passages 17 of the line exchange, until the cold end of it.
  • the liquid thus obtained is expanded in an expansion valve 18 and combined with the liquefied current from the valve trigger 15.
  • Liquid oxygen drawn from the tank of the column 11 is brought by pump 9 to the high desired production pressure, then vaporized and heated in passages 18 of the exchange line before being evacuated from the installation via a pipe of production 19.
  • This impure nitrogen is heated in the sub-cooler 3 then in passages 28 of the line before being evacuated via a pipe 29.
  • the liquid air coming from the valves 15 and 18, the lean liquid and the rich liquid are sub-cooled, about 2 ° C for the liquid rich.
  • the exchange diagram should be of the exchange line 2 is also tightened as possible, this in order to approach conditions reversible heat exchange.
  • the enthalpies H are plotted on the abscissa and the temperatures on the ordinate, that the deviations of temperature between air being cooled (curve C1) and the products being heated (curve C2) are as low as possible at the end hot and cold end of the exchange line as well at the start of the oxygen vaporization stage 30.
  • turbines cryogenic have an input distributor followed of a wheel.
  • the distributor produces a first relaxation or enthalpy fall, which is a characteristic of the turbine.
  • the third condition above therefore makes it easy to determine the intermediate pressure, which is the pressure at which air must enter the turbine to be at the near its dew point at the entrance of the wheel. This intermediate pressure is between 30 and 40 bars approximately.
  • this flow rate D L could be canceled out if it were possible to choose a high air pressure clearly greater than 80 bars and, according to the calculation, of the order of 100 bars.
  • the mechanical energy produced by the turbine 8 is recovered to contribute to the drive of the booster 7, but the latter also has an external source of drive energy. If one wants, as a variant, to couple the turbine 8 and this booster, to simplify the installation, it is necessary to increase the intermediate pressure as well as the temperature T1, and the calculation shows that this leads to an increase in the flow rate D L as well as specific energy.
  • the air flows at the intermediate pressure and high pressure can represent around 20% and around 25%, respectively, of the treated air flow.
  • the tank of the column 31 is connected to the "argon tapping" of column 11 via two pipes 32 feed and 33 back while his head is equipped with a condenser 34 in which liquid rich, relaxed in 35 until near pressure atmospheric, is vaporized and then returned to the column 11 via a pipe 36.
  • the impure gas gas withdrawn at the head of column 31 via a pipe 37 is purified in 31A then 31B, and the pure argon is withdrawn installation in liquid form via a pipe of production 37A.
  • the sub-cooling of the rich liquid before its trigger in 21 and possibly in 35 can be made in an additional heat exchanger 38 vaporizing liquid oxygen drawn from the tank of the column 11. This makes it possible to sub-cool from 4 to 5 ° C. the large quantities of rich liquid circulating during the implementation of a "pump" process and therefore improve the extraction yield oxygen and, if applicable, argon.
  • the installation can also produce nitrogen gaseous under pressure, this nitrogen being taken in the state liquid in line 22, pumped under pressure desired by a pump 39, vaporized and then reheated in passages 40 of the exchange line 2, and withdrawn via a production line 41.
  • all or part of the liquid withdrawn can also consist of liquid nitrogen (line 25).
  • the liquid vaporized after pumping can be oxygen, nitrogen or argon.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (9)

  1. Verfahren zur Herstellung von gasförmigem Sauerstoff unter einem hohen Druck von mindestens ungefähr 30 bar, bei dem man:
    die Luft in einer Einrichtung mit doppelter Destillationskolonne (1), umfassend eine Kolonne (11), die unter einem niedrigen Druck arbeitet, und eine Kolonne (10), die unter einem mittleren Druck arbeitet, destilliert;
    (in 9) den flüssigen Sauerstoff abpumpt, welcher der unter niedrigem Druck arbeitenden Kolonne der Einrichtung (11) entnommen wird;
    die komprimierte Flüssigkeit durch den Austausch von Wärme - in einem Wärmetauscher (2) des Typs mit aufgelöteten Platten - mit Luft, die gerade abgekühlt und / oder verflüssigt wird, zur Verdampfung bringt; und
    der Einrichtung (in 24, 25; 37A) mindestens ein flüssiges Produkt entnimmt, wobei die Durchflussmenge des entnommenen, flüssigen Produkts zwischen ungefähr 2 und 12 % der gesamten Durchflussmenge an hergestelltem Sauerstoff liegt und die zu destillierende Luft in folgende drei Ströme unterteilt wird, wobei die Summe der Durchflussmengen gleich der Durchflussmenge der eintretenden Luft ist:
    in einen ersten Luftstrom, der unter mittlerem Druck steht, bis in die Nähe seines Taupunkts abgekühlt und dann in die unter mittlerem Druck arbeitende Kolonne (10) eingeleitet wird;
    in einen zweiten Luftstrom, der unter hohem Druck steht, welcher größer als ungefähr 60 bar ist, wobei dieser zweite Luftstrom (in 17) vollständig abgekühlt und verflüssigt wird und anschließend nach der Entspannung in einem Druckminderventil (18) in die Doppelkolonne (1) eingeführt wird, wobei auf diesen zweiten Luftstrom ungefähr 20 bis 25 % der gesamten Durchflussmenge der zu destillierenden Luft entfallen; und
    in einen dritten Luftstrom, der unter einem dazwischenliegenden Druck steht, wobei auf diesen dritten Luftstrom ungefähr 10 bis 30 % der gesamten Durchflussmenge der zu destillierenden Luft entfallen, mindestens ein Teil dieses dritten Luftstroms bei einer dazwischenliegenden Abkühlungstemperatur in einer Turbine (8) auf den mittleren Druck entspannt wird, bevor er in die unter mittlerem Druck arbeitende Kolonne (10) einleitet wird, der dazwischenliegende Druck so gewählt wird, dass die Luft sich am Einlass des Turbinenrads in der Nähe ihres Taupunkts befindet, und der eventuell verbleibende Teil weiterhin abgekühlt und verflüssigt wird und anschließend in einem Druckminderventil (15) entspannt und in die Doppelkolonne einleitet wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass auf diesen ersten, zweiten und dritten Luftstrom ungefähr 55 %, ungefähr 20 % beziehungsweise ungefähr 25 % der Durchflussmenge der verarbeiteten Luft entfallen.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass dieses flüssige Produkt mindestens zum Teil flüssiges Argon ist, das von einer zusätzlichen Kolonne (31) zur Trennung von Sauerstoff und Argon, welche mit der Doppelkolonne (1) verbunden ist, hergestellt wird.
  4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, dass die Gesamtheit dieses flüssigen Produkts aus flüssigem Argon besteht.
  5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass man die Kompression des zweiten Luftstroms von dem dazwischenliegenden Druck auf den hohen Druck allein mit Hilfe der mechanischen, von der Turbine (8) gelieferten Energie gewährleistet.
  6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass die dazwischenliegende Temperatur nahe an der Verdampfungstemperatur der Flüssigkeit liegt, die unter dem hohen Druck steht.
  7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, dass der hohe Druck nahe bei 40 bar liegt und die Durchflussmenge des flüssigen Produkts, das der Einrichtung entnommen wird, im Wesentlichen bestimmt wird durch: DL = -0,22 P + 22 wobei DL in % das Verhältnis der Durchflussmenge des entnommenen, flüssigen Produkts zu der gesamten Durchflussmenge des hergestellten Sauerstoffs ist und wobei P der hohe Luftdruck in Bar bei absolutem Druck ist.
  8. Einrichtung zur Herstellung von gasförmigem Sauerstoff unter einem hohen Druck von mindestens ungefähr 30 bar, umfassend:
    eine Doppelkolonne (1) zur Destillation von Luft, umfassend eine Kolonne (11), die unter einem niedrigen Druck arbeitet, und eine Kolonne (10), die unter einem mittleren Druck arbeitet;
    eine Kolonne (31) zur Herstellung von flüssigem Argon, die mit der Doppelkolonne (1) verbunden ist;
    eine Pumpe (9) zur Kompression des flüssigen Sauerstoffs, welcher der unter niedrigem Druck arbeitenden Kolonne der Einrichtung (11) entnommen wird;
    Mittel zur Kompression (14, 30) der eintretenden Luft;
    einen Wärmetauscher (2) des Typs mit aufgelöteten Platten, um für den thermischen Austausch die zu destillierende Luft und den komprimierten, flüssigen Sauerstoff in Verbindung zu bringen; und
    eine Leitung (24, 25; 37A) zur Entnahme wenigstens eines flüssigen Produkts aus der Einrichtung;
    wobei die Mittel zur Kompression wiederum Mittel (4, 6, 7) umfassen, um drei Luftströme zu erzeugen, die unter dem mittlerem Druck, unter einem dazwischenliegenden Druck und unter einem hohen Luftdruck stehen, wobei die Summe der Durchflussmengen gleich der Durchflussmenge der eintretenden Luft ist;
    wobei der Wärmetauscher (2) erste Durchlassöffnungen (13) zur Abkühlung der unter mittlerem Druck stehenden Luft von seinem heißen Ende zu seinem kalten Ende, zweite Durchlassöffnungen (14) zur Abkühlung der unter dem dazwischenliegenden Druck stehenden Luft und dritte Durchlassöffnungen (17) zur Abkühlung der gesamten, unter hohem Druck stehenden Luft von seinem heißen Ende zu seinem kalten Ende umfasst;
    wobei die Einrichtung eine Turbine (8) zur Entspannung - auf den mittleren Druck - von wenigstens einem Teil der unter dem dazwischenliegenden Druck stehenden Luft, die teilweise in den zweiten Durchlassöffnungen (14) abgekühlt worden ist, Mittel zur Regelung dieser Luftströme, die unter dem dazwischenliegenden und unter dem hohen Druck stehen, auf ungefähr 10 bis 30 % beziehungsweise auf ungefähr 20 bis 25 % der gesamten Durchflussmenge der zu destillierenden Luft sowie Mittel zur Regelung der Durchflussmenge des entnommenen, flüssigen Produkts auf einen Wert zwischen ungefähr 2 und 12 % der gesamten Durchflussmenge des hergestellten Sauerstoffs umfasst.
  9. Einrichtung nach Anspruch 8, dadurch gekennzeichnet, dass sie einen zusätzlichen Wärmetauscher (38) umfasst, um die Flüssigkeit, die in der Wanne der unter mittlerem Druck arbeitenden Kolonne (10) entnommen wird, durch Verdampfung der Flüssigkeit, die der unter niedrigem Druck arbeitenden Kolonne (11) entnommen wird, zu unterkühlen.
EP97400222A 1996-02-12 1997-01-31 Verfahren und Einrichtung zur Herstellung von gasförmigem Sauerstoff unter hohem Druck Expired - Lifetime EP0789208B1 (de)

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FR9601698 1996-02-12
FR9601698A FR2744795B1 (fr) 1996-02-12 1996-02-12 Procede et installation de production d'oxygene gazeux sous haute pression

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WO2020169900A1 (fr) 2019-02-21 2020-08-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et procédé de séparation des gaz de l'air mettant en œuvre un adsorbeur de forme parallélépipédique

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WO2020169901A1 (fr) 2019-02-21 2020-08-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et procédé de séparation des gaz de l'air à basse pression
WO2020169900A1 (fr) 2019-02-21 2020-08-27 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et procédé de séparation des gaz de l'air mettant en œuvre un adsorbeur de forme parallélépipédique

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DE69719578D1 (de) 2003-04-17
FR2744795B1 (fr) 1998-06-05
ES2193336T3 (es) 2003-11-01
CN1097715C (zh) 2003-01-01
DE69719578T2 (de) 2003-12-11
KR970062629A (ko) 1997-09-12
CN1168463A (zh) 1997-12-24
CA2197156A1 (en) 1997-08-13
JPH09310970A (ja) 1997-12-02
US5735142A (en) 1998-04-07
FR2744795A1 (fr) 1997-08-14
ZA971031B (en) 1997-08-25
KR100466917B1 (ko) 2005-04-22

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