EP0914584B1 - Verfahren und einrichtung zur herstellung eines luftgases mit variablen mengen - Google Patents

Verfahren und einrichtung zur herstellung eines luftgases mit variablen mengen Download PDF

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EP0914584B1
EP0914584B1 EP97935636A EP97935636A EP0914584B1 EP 0914584 B1 EP0914584 B1 EP 0914584B1 EP 97935636 A EP97935636 A EP 97935636A EP 97935636 A EP97935636 A EP 97935636A EP 0914584 B1 EP0914584 B1 EP 0914584B1
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Prior art keywords
flow
liquid
auxiliary
gas
pressure
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French (fr)
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EP0914584A1 (de
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Bernard Darredeau
Alain Guillard
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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
    • 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
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • F25J3/04515—Simultaneously changing air feed and products output
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04763—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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the present invention relates to a method for producing an air gas, in particular oxygen, at variable flow by air distillation, of the type described in the preamble of claim 1.
  • the invention applies in particular to the production of oxygen under pressure with variable flow.
  • the pressures discussed here are absolute pressures, and flow rates are flow rates molars.
  • EP-A-0 422 974 in the name of the Applicant describes a process of this type, called a "rocking process", intended for the production of gaseous oxygen with variable flow.
  • the second fluid in question is air to be distilled, which is condensed at a variable rate.
  • the compressor, and possibly the booster are significantly oversized compared to the flow nominal oxygen to be produced.
  • they work for the majority of the time at high flows reduced compared to their capacities, and therefore with a degraded yield.
  • the invention aims to allow the production of air gas with variable flow in particularly effective and economical conditions.
  • This process can include one or more of Features of claims 2 to 11.
  • the subject of the invention is also a installation intended for the implementation of such process. This installation is described in the claim 12.
  • This installation may include one or more several of the features of claims 13 to 16.
  • the installation shown in Figure 1 basically includes a main air compressor 1 with variable flow, for example of the centrifugal type with blades mobile, an adsorption purification device 2, a heat exchange line 3, a turbine 4 for maintaining cold, an air distillation apparatus 5 consisting of a double column including itself a column medium pressure 6 surmounted by a low pressure column 7 and a vaporizer-condenser 8, a reservoir liquid oxygen 10, a liquefied air tank 11, two pumps 12 and 13, an air booster 14 and a capacity auxiliary or "buffer" 15.
  • This installation is intended to produce a variable flow of gaseous oxygen via a production line 16, at a pressure of around 15 bars.
  • a first flow is cooled in passages 19 of exchange line 3; some came out of this exchange line after partial cooling, expanded to around 1 bar in turbine 4 and blown into the low pressure column 7 near its point of dew via line 20; the rest continues cooling to the vicinity of its dew point under 6 bars, then is injected at the bottom of the middle column pressure 6 via line 21.
  • a second flow is boosted at 14 to a high condensing pressure defined below, then is cooled and liquefied in passages 22 of the line then stored in liquid form in the tank 11 after expansion to 6 bars in a valve trigger 23.
  • a constant flow of liquefied air is drawn off from the bottom of this tank and is divided into a first flow constant at 6 bars sent in the middle column pressure via line 24, and in a second flow constant relaxed towards 1 bar in an expansion valve 25 then injected into the low pressure column 7.
  • the vaporizer-condenser 8 vaporizes a flow liquid oxygen constant in bottom column tank pressure 7 by condensation of an approximately equal flow nitrogen at the top of the medium pressure column 6.
  • Du "rich liquid” (oxygen-enriched air) taken from tank of the medium pressure column and relaxed to 1 bar in an expansion valve 26 is injected at a level intermediate of the low pressure column, and of the “liquid poor "(almost pure nitrogen), taken at the head of the medium pressure column and relaxed to 1 bar in one expansion valve 27, is injected at the top of the column low pressure.
  • Capacity 15 is connected to the conduct of production 16 via a line 33 fitted with a valve trigger and flow control 34, and a constant flow equal to that of the aforementioned second stream is relaxed in this valve 34 and sent from capacity 15 to line 16.
  • the installation includes a single blower 14, so that the condensation of pressurized air is used, in passages 22 of the exchange line, to vaporize both the oxygen under 15 bars and oxygen under 30 bars.
  • the pressure of the supercharged air is chosen as being the pressure known as "concomitant" with the vaporization of oxygen under 15 bars.
  • This pressure is that for which the knee G of air liquefaction is close to the stage P of vaporization of oxygen under 15 bars, as shown in FIG. 2, on which the quantities of heat exchanged Q are plotted on the ordinate and temperatures t on the abscissa.
  • point A represents the inlet temperature of turbine 4, and this inlet temperature is chosen so as to obtain a minimum temperature difference, of the order of a few degrees, at the warm end of the exchange line.
  • oxygen is produced under 1 bar approximately, and the oxygen demand is still greater than a given minimum value.
  • a flow constant gaseous oxygen equal to this minimum value can then be drawn directly from the bottom of the column low pressure 7 via a pipe 35, as indicated in dashed line in Figure 1, then reheated in the line exchange.
  • This variant reduces the capacity tanks 10 and 11.
  • production constants of liquid oxygen and / or nitrogen gas and / or liquid nitrogen can be supplied simultaneously by the double column, via lines 36 and / or 37 and / or 38, also as shown in phantom in Figure 1.
  • the pump 13 is deleted.
  • the auxiliary oxygen flow is withdrawn in gaseous form from the tank of column 7, via a pipe 39, is heated at 30 below the low pressure and then is compressed at high pressure by a auxiliary compressor 40 before being introduced into the capacity 15.
  • the vaporizing fluid at least one of the two oxygen flow rates is nitrogen.
  • the main flow is sprayed using the vaporizer 8 of the double column. This main flow is then withdrawn in gaseous form from the column tank 7, via a pipe 41, and heated at 29.
  • the discharge pump 12 is then connected to the column tank, which feeds the tank 10 by gravity.
  • line 38 is connected to a nitrogen tank 42, and the bottom of this tank is connected to a pump 43 for returning a constant flow of nitrogen liquid at the top of column 6.
  • the rocker is, in this variant, a rocker oxygen / nitrogen, and the reservoir 11, at constant level, can be deleted.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Respiratory Apparatuses And Protective Means (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)

Claims (16)

  1. Verfahren zur Produktion eines Luftgases, insbesondere von Sauerstoff, mit variabler Durchflußmenge durch Luftdestillation, bei dem man zumindest einen Teil des zu produzierenden Gases in Form einer ersten Flüssigkeit in einem ersten Vorratstank (10) speichert; aus diesem Vorratstank eine variable Durchflußmenge der ersten Flüssigkeit abzieht und (bei 12, 29; 12, 8, 29) in Gasform und auf den Produktionsdruck bringt, wobei die variable Durchflußmenge (bei 29; 8) durch Kondensieren einer entsprechenden variablen Durchflußmenge eines zweiten Fluids, insbesondere zu destillierender Luft, verdampft wird; dieses kondensierte zweite Fluid in Form einer zweiten Flüssigkeit in einem zweiten Vorratstank (11) speichert und der Destillationsapparatur eine gesteuerte Durchflußmenge dieser zweiten Flüssigkeit zuführt, dadurch gekennzeichnet, daß man eine zusätzliche Durchflußmenge des zu produzierenden Gases in Gasform und auf einen über dem Produktionsdruck liegenden hohen Druck bringt, danach unter diesem hohen Druck in einem zusätzlichen Behälter (15) speichert und bei bestimmten Gasverbrauchsspitzen zumindest einen Teil des in diesem zusätzlichen Behälter enthaltenen überschüssigen Gases (bei 34) auf den Produktionsdruck bringt und danach entnimmt.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß man die zusätzliche Durchflußmenge in flüssiger Form (bei 13) auf den hohen Druck verdichtet und die verdichtete zusätzliche Durchflußmenge vor dem Eintragen in den zusätzlichen Behälter (15) unter diesem hohen Druck verdampft.
  3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß man die verdichtete zusätzliche Durchflußmenge durch Wärmeaustausch mit dem zweiten Fluid verdampft.
  4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß man die variable Durchflußmenge und die zusätzliche Durchflußmenge durch Wärmeaustausch mit dem zweiten Fluid unter einem einzigen Kondensationsdruck verdampft.
  5. Verfahren nach Anspruch 3 oder 4, dadurch gekennzeichnet, daß man den einzigen Kondensationsdruck so wählt, daß die Kondensationstemperatur des zweiten Fluids kleiner ist als die Verdampfungstemperatur des Gases, zumindest unter dem hohen Druck.
  6. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß die Kondensationstemperatur des zweiten Fluids unter dem Kondensationsdruck zur Verdampfungstemperatur des Gases unter dem Produktionsdruck konkomitant ist.
  7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß man aus der Destillationsapparatur (5) eine konstante Durchflußmenge der ersten Flüssigkeit abzieht und eine konstante Durchflußmenge der zweiten Flüssigkeit aus dem zweiten Vorratstank (11) zur Destillationsapparatur leitet.
  8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß es sich bei der zusätzlichen Durchflußmenge um eine untergeordnete Fraktion der Durchflußmenge der ersten Flüssigkeit, insbesondere etwa 25% davon bei Nominalbetrieb, handelt.
  9. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß die zusätzliche Durchflußmenge konstant ist.
  10. Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, daß es sich bei den Verbrauchsspitzen um Spitzen mit einer über einem vorgegebenen Wert liegenden Amplitude handelt.
  11. Verfahren nach einem der Ansprüche 1 bis 10, dadurch gekennzeichnet, daß man die überschüssige Durchflußmenge des Gases bis zu einer vorgegebenen überschüssigen Durchflußmenge des Gases durch Erhöhung der variablen Durchflußmenge bereitstellt.
  12. Anlage zur Produktion eines Luftgases, insbesondere von Sauerstoff, mit variabler Durchflußmenge, enthaltend: eine Luftdestillationsapparatur (5); eine Wärmeaustauschleitung (3) zum Abkühlen der zu destillierenden Luft durch Wärmeaustausch mit Produkten, die von der Destillationsapparatur kommen; einen ersten Vorratstank (10) zum Speichern des Gases in Form einer ersten Flüssigkeit; erste Einrichtungen (12, 29; 12, 8, 29) zum Abziehen einer variablen Durchflußmenge der ersten Flüssigkeit aus dem ersten Vorratstank und zum Bringen der ersten Flüssigkeit in Gasform und auf den Produktionsdruck, wobei diese ersten Einrichtungen zweite Einrichtungen (29; 8) zum Verdampfen der variablen Durchflußmenge durch Kondensieren einer entsprechenden variablen Durchflußmenge eines zweiten Fluids, insbesondere zu destillierender Luft, in Form einer zweiten Flüssigkeit aufweisen; und einen zweiten Vorratstank (11) zum Speichern der zweiten Flüssigkeit, dadurch gekennzeichnet, daß sie dritte Einrichtungen (13, 30) zum Bringen einer zusätzlichen Durchflußmenge des zu produzierenden Gases in Gasform und auf einen über dem Produktionsdruck liegenden hohen Druck und anschließenden Einleiten in einen zusätzlichen Behälter (15) und eine mit einem Entspannungs- und Durchflußregelventil (34) versehene Leitung (33), die diesen zusätzlichen Behälter mit der Produktionsleitung (16) der Anlage verbindet, enthält.
  13. Anlage nach Anspruch 12, dadurch gekennzeichnet, daß die dritten Einrichtungen (13, 30) eine Pumpe (13) zum Verdichten der zusätzlichen Durchflußmenge in flüssiger Form und Einrichtungen (30) zum Verdampfen der verdichteten zusätzlichen Durchflußmenge enthalten.
  14. Anlage nach Anspruch 13, dadurch gekennzeichnet, daß die Pumpe (13) mit dem ersten Vorratstank (10) verbunden ist.
  15. Anlage nach Anspruch 13 oder 14, dadurch gekennzeichnet, daß sie einen einzigen Nachverdichter (14) enthält, der das zweite Fluid durch Wärmeaustausch mit der variablen Durchflußmenge und mit der zusätzlichen Durchflußmenge auf einen einzigen Kondensationsdruck bringt.
  16. Anlage nach einem der Ansprüche 12 bis 15, dadurch gekennzeichnet, daß sie Abzieheinrichtungen (28), die auf das Abziehen einer konstanten Durchflußmenge der ersten Flüssigkeit aus der Destillationsapparatur (5) ausgelegt sind, und Einrichtungen zum Leiten einer konstanten Durchflußmenge der zweiten Flüssigkeit aus dem zweiten Vorratstank (11) zur Destillationsapparatur enthält.
EP97935636A 1996-07-25 1997-07-25 Verfahren und einrichtung zur herstellung eines luftgases mit variablen mengen Expired - Lifetime EP0914584B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR9609376 1996-07-25
FR9609376A FR2751737B1 (fr) 1996-07-25 1996-07-25 Procede et installation de production d'un gaz de l'air a debit variable
PCT/FR1997/001401 WO1998004877A1 (fr) 1996-07-25 1997-07-25 Procede et installation de production d'un gaz de l'air a debit variable

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EP0914584B1 true EP0914584B1 (de) 2002-05-02

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JP (1) JP2000515236A (de)
KR (1) KR100488029B1 (de)
CN (1) CN1145004C (de)
AR (1) AR013064A1 (de)
AT (1) ATE217071T1 (de)
BR (1) BR9710525A (de)
CA (1) CA2261097A1 (de)
DE (1) DE69712340T2 (de)
ES (1) ES2175446T3 (de)
FR (1) FR2751737B1 (de)
PL (1) PL331280A1 (de)
WO (1) WO1998004877A1 (de)
ZA (2) ZA976197B (de)

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US6182471B1 (en) * 1999-06-28 2001-02-06 Praxair Technology, Inc. Cryogenic rectification system for producing oxygen product at a non-constant rate
US6354105B1 (en) * 1999-12-03 2002-03-12 Ipsi L.L.C. Split feed compression process for high recovery of ethane and heavier components
EP1318368A1 (de) * 2001-12-10 2003-06-11 The Boc Group, Inc. Luftzerlegungsverfahren zur Produktion von gasförmigem Produkt mit variabeler Durchflussmenge
GB0219415D0 (en) * 2002-08-20 2002-09-25 Air Prod & Chem Process and apparatus for cryogenic separation process
US7228715B2 (en) * 2003-12-23 2007-06-12 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
US7272954B2 (en) * 2004-07-14 2007-09-25 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Proceded Georges Claude Low temperature air separation process for producing pressurized gaseous product
US7553419B2 (en) * 2006-05-03 2009-06-30 Organix, Inc. Method of material processing to produce a fiber product
FR2949845B1 (fr) * 2009-09-09 2011-12-02 Air Liquide Procede d'operation d'au moins un appareil de separation d'air et d'une unite de combustion de combustibles carbones
US9400135B2 (en) * 2010-07-05 2016-07-26 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Process and apparatus for the separation of air by cryogenic distillation
CN103282732B (zh) * 2010-07-05 2016-08-03 乔治洛德方法研究和开发液化空气有限公司 通过低温蒸馏分离空气的装置和方法
US10359231B2 (en) * 2017-04-12 2019-07-23 Praxair Technology, Inc. Method for controlling production of high pressure gaseous oxygen in an air separation unit

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FR2652887B1 (fr) * 1989-10-09 1993-12-24 Air Liquide Procede et installation de production d'oxygene gazeux a debit variable par distillation d'air.
FR2670278B1 (fr) * 1990-12-06 1993-01-22 Air Liquide Procede et installation de distillation d'air en regime variable de production d'oxygene gazeux.
FR2723184B1 (fr) * 1994-07-29 1996-09-06 Grenier Maurice Procede et installation de production d'oxygene gazeux sous pression a debit variable
FR2757282B1 (fr) * 1996-12-12 2006-06-23 Air Liquide Procede et installation de fourniture d'un debit variable d'un gaz de l'air

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ZA976620B (en) 1999-01-25
EP0914584A1 (de) 1999-05-12
FR2751737B1 (fr) 1998-09-11
ZA976197B (en) 1999-02-17
CN1145004C (zh) 2004-04-07
DE69712340D1 (de) 2002-06-06
FR2751737A1 (fr) 1998-01-30
US6062044A (en) 2000-05-16
KR100488029B1 (ko) 2005-05-09
ES2175446T3 (es) 2002-11-16
ATE217071T1 (de) 2002-05-15
CN1226312A (zh) 1999-08-18
JP2000515236A (ja) 2000-11-14
DE69712340T2 (de) 2002-11-14
BR9710525A (pt) 1999-08-17
PL331280A1 (en) 1999-07-05
CA2261097A1 (fr) 1998-02-05
KR20000023846A (ko) 2000-04-25
AR013064A1 (es) 2000-12-13
WO1998004877A1 (fr) 1998-02-05

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