EP0848220A1 - Method and plant for supplying an air gas at variable quantities - Google Patents

Method and plant for supplying an air gas at variable quantities Download PDF

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Publication number
EP0848220A1
EP0848220A1 EP97402990A EP97402990A EP0848220A1 EP 0848220 A1 EP0848220 A1 EP 0848220A1 EP 97402990 A EP97402990 A EP 97402990A EP 97402990 A EP97402990 A EP 97402990A EP 0848220 A1 EP0848220 A1 EP 0848220A1
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EP
European Patent Office
Prior art keywords
flow
pressure
total flow
pump
brought
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP97402990A
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German (de)
French (fr)
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EP0848220B1 (en
Inventor
Alain Guillard
Patrick Le Bot
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0848220A1 publication Critical patent/EP0848220A1/en
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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
    • F25J3/04763—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
    • 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
    • F25J3/04012—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
    • F25J3/04036—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 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
    • F25J3/04006—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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • 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
    • F25J3/04284—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
    • F25J3/04248—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
    • 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.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work 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
    • F25J3/04406—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods
    • 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 process for supplying a consumer line, during a time interval, a variable demand flow of an air component, in particular of oxygen, produced by an air distillation apparatus. It applies in particular to the supply of pressurized oxygen with highly variable flow.
  • the pressures discussed here are absolute pressures, and the flows are flows molars.
  • oxygen is used in "batch", with significant variations in flow and at moderately high pressures (of the order of a few bars to about twenty bars).
  • moderately high pressures of the order of a few bars to about twenty bars.
  • Various solutions are conventionally used in order to follow these changes in debit.
  • EP-A-0 422 974 on behalf of the Applicant describes a "rocking" process intended for the production of gaseous oxygen at variable flow.
  • Oxygen requested is withdrawn from a tank, pumped to operating pressure, and vaporized by condensation with a variable flow of air to be distilled.
  • 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 different from their nominal flow, and therefore with a degraded yield.
  • the right operation of the scale assumes permanent presence a reserve of the two liquids.
  • the invention aims to allow the supply of variable-flow air gases in particularly effective and economical conditions.
  • the subject of the invention is also a air distillation installation intended for work of the process defined above.
  • This installation comprises, according to the invention, means for withdrawing from the distillation apparatus a constant total flow of said constituent; a buffer capacity; of the first means for bringing at least part of said total flow at operating pressure and in gaseous form, these first means being connected to the consumer line; second means for bringing a second flow of said constituting at a high pressure greater than the pressure of use and in gaseous form, these second means being connected to the buffer capacity; and a conduct auxiliary fitted with a controlled expansion valve, connecting the buffer capacity to the consumer line.
  • pressure P constant and equal to 16 bars, but it will be understood that this pressure P can also fluctuate around an average value.
  • DN the flow nominal of the oxygen production installation. This DN flow is equal to D1 in this example, but, in variant it could be greater than this value if the installation is also intended to provide oxygen to other consumers.
  • the flow d1 is sent directly to the user or consumer behavior, while the flow d2 is sent to a buffer or buffer.
  • the requested flow D is greater than D1
  • This flow d3 is represented by diagram (d).
  • FIGS 2, 3 and 5 to 11 show several different installations capable of implement such a method.
  • Figures 2 and 3 relate to a installation close to that shown in Figure 1 from US-A-5,329,776, and differ from it only by the addition of an additional racking line 35 of liquid oxygen, of an additional pump 36 adapted to bring this liquid oxygen to the aforementioned pressure P, additional passages 37 of the exchange line thermal, for vaporization and reheating up to the ambient temperature of this oxygen, from a high oxygen storage buffer 38 pressure from the 12-passage pump circuit 17, from a pressure regulator 138 disposed upstream of this buffer, and a line 39 provided with an expansion valve 40, connecting this buffer to the consumer line 15.
  • the air distillation installation shown in FIG. 3 essentially comprises: an air compressor 1; an apparatus 2 for purifying the compressed air into water and CO 2 by adsorption, this apparatus comprising two adsorption bottles 2A, 2B, one of which operates in adsorption while the other is being regenerated; a turbine-booster assembly 3 comprising an expansion turbine 4 and a booster 5 whose shafts are coupled; a heat exchanger 6 constituting the heat exchange line of the installation; a double distillation column 7 comprising a medium pressure column 8 surmounted by a low pressure column 9, with a vaporizer-condenser 10 putting the overhead vapor (nitrogen) from column 8 in heat exchange relation with the tank liquid (oxygen) from column 9; a liquid oxygen tank 11, the bottom of which is connected to a liquid oxygen pump 12; and a liquid nitrogen tank 13, the bottom of which is connected to a liquid nitrogen pump 14.
  • This facility is intended to provide, via a user line 15, gaseous oxygen under the operating pressure P.
  • liquid oxygen drawn from the column 9 tank via line 16 and stored in the reservoir 11 is brought to the high pressure P1 (30 bars) by the pump 12 in the liquid state, then vaporized and heated under this high pressure in passages 17 of the exchanger 6, under the conditions of FIG. 1 (c), and sent to buffer 38. Under the conditions of Figure 1 (d), this oxygen is expanded at 40 and sent to the line 15 via line 39.
  • the heat necessary for this vaporization and to this reheating, as well as to reheating and possibly vaporization of other fluids drawn from the double column, is supplied by the air to be distilled, in the following conditions.
  • All of the air to be distilled is compressed by compressor 1 at a first high pressure significantly higher than the average column pressure 8 of use. Then the air, precooled in 18 and cooled to around room temperature in 19, is purified in one, 2A for example, of the bottles adsorption, and fully boosted by the booster 5, which is driven by the turbine 4.
  • Air is then introduced at the hot end of exchanger 6 and completely cooled to a intermediate temperature. At this temperature, a fraction of the air continues to cool and is liquefied in passages 20 of the exchanger, then is relaxed at low pressure in an expansion valve 21 and introduced at an intermediate level in the column 9. The rest of the air is relaxed to average pressure in turbine 4 then sent directly, via a pipe 22, at the base of column 8.
  • Low pressure nitrogen is heated in passages 28 of exchanger 6 then evacuated via a pipe 29, while the waste gas, after heating in passages 30 of the exchanger, is used to regenerate an adsorption bottle, the 2B bottle in the example considered, before being evacuated via a pipe 31.
  • part medium pressure liquid nitrogen is, after expansion in an expansion valve 32, stored in the tank 13, and that a production of liquid nitrogen and / or oxygen liquid is supplied via line 33 (for nitrogen) and / or 34 (for oxygen).
  • the pressure of the compressed air at 5 is the air condensation pressure by heat exchange with oxygen being vaporized under pressure of use P, i.e. the pressure for which air liquefaction knee 100, on the diagram heat exchange is located slightly to the right of the vertical bearing 101 for vaporizing oxygen under the pressure P ( Figure 4).
  • the temperature difference at the end heat of the exchange line is adjusted by means of the turbine 4, the suction temperature of which is indicated in 102.
  • pumps 12 and 36 can be connected in series, the pump suction 12 being stitched on the delivery line of the pump 36.
  • Figure 5 shows a variant installation which differs from the previous one by the removal of pump 36 and of the vaporization-heating circuit corresponding.
  • Figures 7 and 8 show another variant of the installation which does not differ from that of Figures 2 and 3 only by the fact that the oxygen at 16 bars is withdrawn in gaseous form from the column tank low pressure 9, via a line 44, heated under the low pressure in passages 45 of the exchange line 6, and brought to 16 bars by an oxygen compressor 46.
  • Oxygen at 30 bar is drawn from the tank 11 by pump 12, which brings it to this high pressure in liquid form and then is vaporized and warmed in passages 17, and is sent directly to buffer 38.
  • Figures 9 and 10 illustrate the implementation work of the invention with a conventional apparatus of air distillation without pump, nitrogen cycle (turbine 47 releasing at low pressure medium pressure nitrogen) and an argon separation column (not shown) coupled to the low pressure column by two lines 48.
  • the oxygen flow D1 is withdrawn in gaseous form from the bottom column tank pressure and, after heating, is compressed to 16 bars and / or at 30 bars, under the conditions described above, by two respective oxygen compressors 49 and 50.
  • the compressor 49 discharges directly into line 15, while compressor 50 backs up in buffer 38.
  • Figures 11 and 12 does not differs from the previous one only in that the two oxygen compressors are connected in series instead to be mounted in parallel. So the compressor 49 compresses the entire flow D1 to 16 bars, and the compressor 50 carries from 16 to 30 bars the flow d2 described next to Figure 1 (c).
  • compressors 49 and 50 can be made up of two floors or groups stages of the same machine.
  • operating pressure means the pressure in line 15. However, this does not exclude a subsequent modification of this pressure, for example by expansion.
  • the pressure regulator 138 can be deleted.
  • the buffer pressure then changes between pressures P and P1 as a function of time.
  • the method of the invention can use multiple buffers at high pressures P1, P2, ... different, all significantly greater than the operating pressure P.
  • gas is then taken from one or the other of the buffers, according to the variations of this flow.

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Abstract

The method for supplying to a consumer pipe (15), during an interval of time, a variable demand flow of a component of air, in particular oxygen, produced by an air distillation device, by: a) sucking from the device a total flow of the component of constant value (D1); b) dividing the time interval into different periods, so that eventually there is at least a first period during which the flow required (D) is equal to the total flow (D1); c) at least a second period during which the flow is less than the total flow; and at least a third period during which the flow is greater than the total flow. During the first period(s) the total flow is brought to the user pressure (P) and sent to the consumer pipe. During the second period(s), the required flow is brought to the pressure (P) and sent to the consumer pipe and a storage flow (equal to the difference between the supply and the required flow) is brought to a higher pressure (P1) greater than the user pressure and stored in a balancing store. During the third period(s), the total flow is brought to the user pressure and sent to the consumer pipe and a complementary flow (equal to the difference between the required flow and the supply) is delivered from the balancing store and expanded to the user pressure.

Description

La présente invention est relative à un procédé pour fournir à une conduite consommatrice, pendant un intervalle de temps, un débit demandé variable d'un constituant de l'air, notamment d'oxygène, produit par un appareil de distillation d'air. Elle s'applique en particulier à la fourniture d'oxygène sous pression à débit fortement variable.The present invention relates to a process for supplying a consumer line, during a time interval, a variable demand flow of an air component, in particular of oxygen, produced by an air distillation apparatus. It applies in particular to the supply of pressurized oxygen with highly variable flow.

Les pressions dont il est question ici sont des pressions absolues, et les débits sont des débits molaires.The pressures discussed here are absolute pressures, and the flows are flows molars.

Dans certaines activités industrielles telles que la sidérurgie des fours à arc électrique ou l'affinage de cuivre, l'oxygène est utilisé en "batch", avec des variations importantes de débit et à des pressions moyennement élevées (de l'ordre de quelques bars à une vingtaine de bars). Diverses solutions sont classiquement utilisées afin de suivre ces évolutions de débit.In certain industrial activities such that the steel industry of electric arc furnaces or copper refining, oxygen is used in "batch", with significant variations in flow and at moderately high pressures (of the order of a few bars to about twenty bars). Various solutions are conventionally used in order to follow these changes in debit.

Par exemple, EP-A-0 422 974 au nom de la Demanderesse décrit un procédé "à bascule" destiné à la production d'oxygène gazeux à débit variable. L'oxygène demandé est soutiré d'un réservoir, porté par pompage à la pression d'utilisation, et vaporisé par condensation d'un débit variable d'air à distiller.For example, EP-A-0 422 974 on behalf of the Applicant describes a "rocking" process intended for the production of gaseous oxygen at variable flow. Oxygen requested is withdrawn from a tank, pumped to operating pressure, and vaporized by condensation with a variable flow of air to be distilled.

Dans ce procédé connu, il est facile de montrer que pour maintenir constants les débits d'alimentation et de soutirage de l'appareil de distillation, il est nécessaire de faire varier le débit d'air entrant dans le même sens que les variations de la consommation d'oxygène. Dans le cas où l'oxygène est produit sous pression, l'air que l'on condense pour vaporiser l'oxygène liquide est surpressé par un surpresseur additionnel, et, lorsque la demande en oxygène varie, il faut faire varier de façon importante à la fois le débit surpressé et le débit comprimé par le compresseur principal.In this known process, it is easy to show that to keep the flow rates constant supply and withdrawal of the distillation apparatus, it is necessary to vary the air flow going in the same direction as the variations of the oxygen consumption. In the event that oxygen is pressurized product, the air that is condensed for vaporize liquid oxygen is boosted by a booster additional, and when the oxygen demand varies, you have to vary significantly at a time the boosted flow and the compressed flow by the compressor main.

Par conséquent, dans ce procédé connu, le compresseur, et éventuellement le surpresseur, sont surdimensionnés de façon importante par rapport au débit nominal d'oxygène à produire. De plus, ils travaillent pendant la majorité du temps à des débits fortement différents de leur débit nominal, et donc avec un rendement dégradé. A ceci s'ajoute le fait que le bon fonctionnement de la bascule suppose la présence permanente d'une réserve des deux liquides.Therefore, in this known method, the compressor, and possibly the booster, are significantly oversized compared to the flow nominal oxygen to be produced. In addition, they work for the majority of the time at high flows different from their nominal flow, and therefore with a degraded yield. Added to this is the fact that the right operation of the scale assumes permanent presence a reserve of the two liquids.

Il a également été proposé de stocker du gaz à produire, sous forme gazeuse, dans une capacité auxiliaire ou "buffer", à une pression supérieure à la pression de production. Cependant, cette solution n'est pas satisfaisante, car elle nécessite la mise en place de buffers de très grande dimension pour faire face à des pointes de consommation de longue durée. De plus, la production de la totalité du gaz à la pression du buffer est coûteuse en énergie.It has also been proposed to store gas to produce, in gaseous form, in a capacity auxiliary or "buffer", at a pressure higher than the production pressure. However, this solution is not not satisfactory, because it requires the installation very large buffers to deal with long-term consumption peaks. In addition, the production of all gas at buffer pressure is costly in energy.

L'invention a pour but de permettre la fourniture de gaz de l'air à débit variable dans des conditions particulièrement efficaces et économiques.The invention aims to allow the supply of variable-flow air gases in particularly effective and economical conditions.

A cet effet, l'invention a pour objet un procédé pour fournir à une conduite consommatrice, pendant un intervalle de temps, un débit demandé variable d'un constituant de l'air, notamment d'oxygène, produit par un appareil de distillation d'air, caractérisé en ce que :

  • on soutire de l'appareil un débit total dudit constituant de valeur constante;
  • on divise l'intervalle de temps en plusieurs types de périodes, à savoir :
    • éventuellement, au moins une première période pendant laquelle le débit demandé est égal audit débit total;
    • au moins une deuxième période pendant laquelle le débit demandé est inférieur audit débit total; et
    • au moins une troisième période pendant laquelle le débit demandé est supérieur audit débit total;
  • pendant ladite ou lesdites premières périodes, on amène ledit débit total à la pression d'utilisation, et on l'envoie à la conduite consommatrice;
  • pendant ladite ou lesdites deuxièmes périodes :
    • on amène le débit demandé à la pression d'utilisation, et on l'envoie à la conduite consommatrice; et
    • on amène à une haute pression supérieure à la pression d'utilisation un débit de stockage dudit constituant égal à la différence entre ledit débit total et le débit demandé, et on stocke ce débit de stockage dans au moins une capacité- tampon; et
  • pendant ladite ou lesdites troisièmes périodes :
    • on amène ledit débit total à la pression d'utilisation, et on l'envoie à la conduite consommatrice; et
    • on envoie en outre dans la conduite consommatrice un débit complémentaire dudit constituant égal à la différence entre le débit demandé et ledit débit total, ce débit complémentaire étant prélevé dans au moins une capacité-tampon et détendu à la pression d'utilisation.
To this end, the subject of the invention is a method for supplying a consuming pipe, during a time interval, with a variable demand flow of an air component, in particular of oxygen, produced by a distillation apparatus of 'air, characterized in that:
  • a total flow of said constituent of constant value is withdrawn from the apparatus;
  • we divide the time interval into several types of periods, namely:
    • optionally, at least a first period during which the requested flow is equal to said total flow;
    • at least a second period during which the requested flow is lower than said total flow; and
    • at least a third period during which the requested flow is greater than said total flow;
  • during said one or more first periods, said total flow is brought to the operating pressure, and it is sent to the consuming line;
  • during said second period (s):
    • the requested flow rate is brought to the operating pressure, and it is sent to the consuming line; and
    • a storage flow rate of said constituent is brought to a high pressure higher than the operating pressure equal to the difference between said total flow rate and the requested flow rate, and this storage flow rate is stored in at least one buffer capacity; and
  • during said third period (s):
    • the said total flow is brought to the operating pressure, and it is sent to the consuming line; and
    • in addition, a complementary flow of said constituent is sent to the consuming line, equal to the difference between the requested flow and said total flow, this additional flow being taken from at least one buffer capacity and expanded to the operating pressure.

Le procédé suivant l'invention peut comporter une ou plusieurs des caractéristiques suivantes :

  • on soutire ledit débit total sous forme liquide de l'appareil de distillation, et on le comprime sous cette forme par pompage avant de le vaporiser;
  • on amène à la pression d'utilisation un premier débit de liquide au moyen d'une première pompe, on amène à la haute pression le débit destiné à la capacité-tampon au moyen d'une seconde pompe, et on vaporise chaque flux de liquide sous sa pression de pompage;
  • on amène ledit débit total à la pression d'utilisation au moyen d'une pompe unique, on vaporise ce liquide et on porte à la haute pression la fraction du gaz ainsi obtenu qui est destinée à la capacité-tampon;
  • on amène ledit débit total à la haute pression au moyen d'une pompe unique, on détend une fraction de ce débit total à la pression d'utilisation, et on vaporise les deux flux chacun sous sa pression;
  • on soutire sous forme liquide de l'appareil de distillation un premier débit, on le comprime par pompage, et on le vaporise sous cette pression; et on soutire sous forme gazeuse de l'appareil de distillation le reste dudit débit total, et on le comprime sous cette forme;
  • on soutire ledit débit total sous forme gazeuse de l'appareil de distillation, on comprime à la pression d'utilisation une fraction de ce gaz, et on comprime à la haute pression le débit complémentaire destiné à la capacité-tampon;
  • on comprime chaque débit indépendamment à partir de la pression de soutirage de l'appareil de distillation;
  • on comprime ledit débit total à la pression d'utilisation, et on comprime une fraction de ce premier débit de la pression d'utilisation à la haute pression.
The process according to the invention may include one or more of the following characteristics:
  • said total flow rate is drawn off in liquid form from the distillation apparatus, and it is compressed in this form by pumping before vaporizing it;
  • a first flow of liquid is brought to the operating pressure by means of a first pump, the flow intended for the buffer capacity is brought to high pressure by means of a second pump, and each flow of liquid is vaporized under its pumping pressure;
  • the said total flow is brought to the operating pressure by means of a single pump, this liquid is vaporized and the fraction of the gas thus obtained which is intended for the buffer capacity is brought to high pressure;
  • said total flow is brought to high pressure by means of a single pump, a fraction of this total flow is relaxed to the operating pressure, and the two flows are each vaporized under its pressure;
  • a first flow is drawn off in liquid form from the distillation apparatus, it is compressed by pumping, and it is vaporized under this pressure; and the remainder of said total flow rate is drawn off in gaseous form from the distillation apparatus, and it is compressed in this form;
  • said total flow is drawn off in gaseous form from the distillation apparatus, a fraction of this gas is compressed at the operating pressure, and the additional flow intended for the buffer capacity is compressed at high pressure;
  • each flow is compressed independently from the withdrawal pressure of the distillation apparatus;
  • said total flow is compressed at the operating pressure, and a fraction of this first flow is compressed from the operating pressure to the high pressure.

L'invention a également pour objet une installation de distillation d'air destinée à la mise en oeuvre du procédé défini ci-dessus. Cette installation comprend, suivant l'invention, des moyens pour soutirer de l'appareil de distillation un débit total constant dudit constituant; une capacité-tampon; des premiers moyens pour amener une partie au moins dudit débit total à la pression d'utilisation et sous forme gazeuse, ces premiers moyens étant reliés à la conduite consommatrice; des seconds moyens pour amener un second débit dudit constituant à une haute pression supérieure à la pression d'utilisation et sous forme gazeuse, ces seconds moyens étant reliés à la capacité-tampon; et une conduite auxiliaire munie d'une vanne de détente commandée, reliant la capacité-tampon à la conduite consommatrice.The subject of the invention is also a air distillation installation intended for work of the process defined above. This installation comprises, according to the invention, means for withdrawing from the distillation apparatus a constant total flow of said constituent; a buffer capacity; of the first means for bringing at least part of said total flow at operating pressure and in gaseous form, these first means being connected to the consumer line; second means for bringing a second flow of said constituting at a high pressure greater than the pressure of use and in gaseous form, these second means being connected to the buffer capacity; and a conduct auxiliary fitted with a controlled expansion valve, connecting the buffer capacity to the consumer line.

Suivant diverses caractéristiques optionnelles de cette installation :

  • les premiers moyens comprennent une première pompe et des premiers moyens de vaporisation, et les seconds moyens comprennent une seconde pompe et des seconds moyens de vaporisation;
  • les premiers moyens comprennent une pompe et des moyens de vaporisation, et les seconds moyens comprennent un compresseur dont l'aspiration est reliée à la sortie des moyens de vaporisation;
  • les premiers moyens comprennent une pompe, une vanne de détente et des premiers moyens de vaporisation, et les seconds moyens comprennent des seconds moyens de vaporisation reliés au refoulement de la pompe;
  • les premiers moyens comprennent un compresseur dont l'aspiration est reliée à un point de soutirage de gaz de l'appareil de distillation, et les seconds moyens comprennent une pompe et des moyens de vaporisation reliés au refoulement de cette pompe;
  • les premiers et les seconds moyens comprennent respectivement deux compresseurs dont les aspirations sont reliées en parallèle à un point de soutirage de l'appareil de distillation ;
  • les premiers moyens comprennent un premier compresseur dont l'aspiration est reliée à un point de soutirage de gaz de l'appareil de distillation, et les seconds moyens comprennent un second compresseur dont l'aspiration est reliée au refoulement du premier compresseur.
According to various optional features of this installation:
  • the first means comprise a first pump and first spray means, and the second means comprise a second pump and second spray means;
  • the first means comprise a pump and vaporization means, and the second means comprise a compressor whose suction is connected to the outlet of the vaporization means;
  • the first means comprise a pump, an expansion valve and first vaporization means, and the second means comprise second vaporization means connected to the discharge of the pump;
  • the first means comprise a compressor, the suction of which is connected to a gas withdrawal point of the distillation apparatus, and the second means comprise a pump and vaporization means connected to the discharge of this pump;
  • the first and second means respectively comprise two compressors, the aspirations of which are connected in parallel to a withdrawal point of the distillation apparatus;
  • the first means comprise a first compressor, the suction of which is connected to a gas withdrawal point of the distillation apparatus, and the second means comprise a second compressor, the suction of which is connected to the discharge of the first compressor.

Des exemples de mises en oeuvre de l'invention vont maintenant être décrits en regard des dessins annexés sur lesquels :

  • la Figure 1 illustre le procédé de l'invention au moyen de quatre diagrammes (a) à (d) ;
  • la Figure 2 représente très schématiquement une installation suivant l'invention;
  • la Figure 3 représente la même installation de manière plus détaillée;
  • la Figure 4 est un diagramme d'échange thermique correspondant à cette installation, avec en abscisses les températures (en °C) et en ordonnées les quantités de chaleur échangées;
  • les Figures 5 et 6 sont des vues analogues à la Figure 2, relatives respectivement à deux variantes de l'installation;
  • la Figure 7 est une vue analogue à la Figure 2 d'une autre variante de l'installation;
  • la Figure 8 est une vue analogue à la Figure 3 correspondant à l'installation de la Figure 7;
  • les Figures 9 et 10 d'une part, 11 et 12 d'autre part, représentent deux autres modes de réalisation de l'installation, de manière analogue aux Figures 2 et 3 respectivement.
Examples of implementations of the invention will now be described with reference to the appended drawings in which:
  • Figure 1 illustrates the process of the invention by means of four diagrams (a) to (d);
  • Figure 2 very schematically shows an installation according to the invention;
  • Figure 3 shows the same installation in more detail;
  • FIG. 4 is a heat exchange diagram corresponding to this installation, with the temperatures on the abscissa (in ° C.) and the quantities of heat exchanged on the ordinate;
  • Figures 5 and 6 are views similar to Figure 2, respectively relating to two variants of the installation;
  • Figure 7 is a view similar to Figure 2 of another variant of the installation;
  • Figure 8 is a view similar to Figure 3 corresponding to the installation of Figure 7;
  • Figures 9 and 10 on the one hand, 11 and 12 on the other hand, represent two other embodiments of the installation, similarly to Figures 2 and 3 respectively.

La Figure 1 (a) illustre une courbe simplifiée de demande d'oxygène sous une pression d'utilisation P, au cours d'une période de temps s'étendant d'un temps t = 0 à un temps T. Dans ce qui suit, on supposera la pression P constante et égale à 16 bars, mais on comprendra que cette pression P peut également fluctuer autour d'une valeur moyenne.Figure 1 (a) illustrates a simplified curve oxygen demand under pressure of use P, over a period of time extending from a time t = 0 to a time T. In which follows, we will assume the pressure P constant and equal to 16 bars, but it will be understood that this pressure P can also fluctuate around an average value.

La demande variable d'oxygène est par exemple celle d'une installation sidérurgique à fours à arc électrique et comporte six intervalles de temps successifs :

  • de t = 0 à t1, le débit demandé est nul;
  • de t1 à t2, le débit demandé est D1;
  • de t2 à t3, le débit demandé est D2 > D1;
  • de t3 à t4, le débit demandé est D3 > D2;
  • de t4 à t5, le débit demandé est D4 < D1;
et
  • de t5 à T, le débit demandé est nul.
The variable oxygen demand is for example that of a steel plant with electric arc furnaces and comprises six successive time intervals:
  • from t = 0 to t1, the requested flow is zero;
  • from t1 to t2, the requested bit rate is D1;
  • from t2 to t3, the requested flow is D2>D1;
  • from t3 to t4, the requested bit rate is D3>D2;
  • from t4 to t5, the requested bit rate is D4 <D1;
and
  • from t5 to T, the requested flow is zero.

On a également indiqué par DN le débit nominal de l'installation de production d'oxygène. Ce débit DN est égal à D1 dans cet exemple, mais, en variante, il pourrait être supérieur à cette valeur, si l'installation est destinée à fournir également de l'oxygène à d'autres consommateurs.We also indicated by DN the flow nominal of the oxygen production installation. This DN flow is equal to D1 in this example, but, in variant it could be greater than this value if the installation is also intended to provide oxygen to other consumers.

La Figure 1(b) représente la production dl d'oxygène à 16 bars par l'installation. Cette production varie comme suit :

  • de t = 0 à t1 : d1 = 0
  • de t1 à t4, c'est-à-dire lorsque la demande en oxygène est supérieure ou égale à D1 : d1 = D1;
  • de t4 à t5, c'est-à-dire lorsque la demande en oxygène est supérieure à O mais inférieure à D1 : d1 = D4;
  • de t5 à T : d1 = 0.
Figure 1 (b) shows the production of oxygen at 16 bar by the installation. This production varies as follows:
  • from t = 0 to t1: d1 = 0
  • from t1 to t4, that is to say when the oxygen demand is greater than or equal to D1: d1 = D1;
  • from t4 to t5, that is to say when the oxygen demand is greater than O but less than D1: d1 = D4;
  • from t5 to T: d1 = 0.

La Figure 1 (c) représente la production d2 d'oxygène à une haute pression P1 nettement supérieure à 16 bars, typiquement de l'ordre de 30 bars :

  • de t = 0 à t1 : d2 = D1;
  • de t1 à t4 : d2 = 0;
  • de t4 à t5 : d2 = D1 - D4;
  • de t5 à T : d2 = D1.
FIG. 1 (c) represents the production d2 of oxygen at a high pressure P1 clearly greater than 16 bars, typically of the order of 30 bars:
  • from t = 0 to t1: d2 = D1;
  • from t1 to t4: d2 = 0;
  • from t4 to t5: d2 = D1 - D4;
  • from t5 to T: d2 = D1.

On voit donc que, sur toute la période 0, T, on a en permanence d1 + d2 = D1, débit constant considéré comme "débit total" d'oxygène, vis-à-vis de l'utilisation considérée.We therefore see that, over the entire period 0, T, we have permanently d1 + d2 = D1, constant flow considered as "total flow" of oxygen with respect to use considered.

Le débit d1 est directement envoyé à la conduite utilisatrice ou consommatrice, tandis que le débit d2 est envoyé à une capacité-tampon ou buffer. Lorsque le débit D demandé est supérieur à D1, soit de t2 à t4, le complément d3 = D - D1 est prélevé dans la capacité-tampon, détendu à la pression d'utilisation et introduit dans la conduite consommatrice. Ce débit d3 est représenté par le diagramme (d).The flow d1 is sent directly to the user or consumer behavior, while the flow d2 is sent to a buffer or buffer. When the requested flow D is greater than D1, either by t2 to t4, the complement d3 = D - D1 is taken from the buffer capacity, relaxed to operating pressure and introduced into the consumer line. This flow d3 is represented by diagram (d).

Ainsi, la demande d'oxygène est fournie :

  • de t1 à t2 et de t4 à t5, uniquement par la production d'oxygène sous 16 bars, et
  • de t2 à t4, partiellement par cette production sous 16 bars et partiellement par de l'oxygène prélevé dans la capacité-tampon et détendu.
Thus, the oxygen demand is provided:
  • from t1 to t2 and from t4 to t5, only by producing oxygen at 16 bars, and
  • from t2 to t4, partially by this production at 16 bars and partially by oxygen taken from the buffer capacity and expanded.

Les Figures 2, 3 et 5 à 11 représentent plusieurs installations différentes capables de mettre en oeuvre un tel procédé.Figures 2, 3 and 5 to 11 show several different installations capable of implement such a method.

Les Figures 2 et 3 sont relatives à une installation voisine de celle représentée à la Figure 1 du US-A-5 329 776, et ne diffèrent de celle-ci que par l'ajout d'une ligne additionnelle 35 de soutirage d'oxygène liquide, d'une pompe additionnelle 36 adaptée pour porter cet oxygène liquide à la pression P précitée, de passages additionnelles 37 de la ligne d'échange thermique, pour la vaporisation et le réchauffage jusqu'au voisinage de la température ambiante de cet oxygène, d'un buffer 38 de stockage de l'oxygène haute pression provenant du circuit pompe 12-passages 17, d'un régulateur de pression 138 disposé en amont de ce buffer, et d'une ligne 39 munie d'une vanne de détente 40, reliant ce buffer à la conduite consommatrice 15.Figures 2 and 3 relate to a installation close to that shown in Figure 1 from US-A-5,329,776, and differ from it only by the addition of an additional racking line 35 of liquid oxygen, of an additional pump 36 adapted to bring this liquid oxygen to the aforementioned pressure P, additional passages 37 of the exchange line thermal, for vaporization and reheating up to the ambient temperature of this oxygen, from a high oxygen storage buffer 38 pressure from the 12-passage pump circuit 17, from a pressure regulator 138 disposed upstream of this buffer, and a line 39 provided with an expansion valve 40, connecting this buffer to the consumer line 15.

Ainsi, comme décrit dans le US-A-5 329 776 précité, l'installation de distillation d'air représentée à la Figure 3 comprend essentiellement : un compresseur d'air 1; un appareil 2 d'épuration de l'air comprimé en eau et en CO2 par adsorption, cet appareil comprenant deux bouteilles d'adsorption 2A, 2B dont l'une fonctionne en adsorption pendant que l'autre est en cours de régénération; un ensemble turbine-surpresseur 3 comprenant une turbine de détente 4 et un surpresseur 5 dont les arbres sont couplés; un échangeur de chaleur 6 constituant la ligne d'échange thermique de l'installation; une double colonne de distillation 7 comprenant une colonne moyenne pression 8 surmontée d'une colonne basse pression 9, avec un vaporiseur-condenseur 10 mettant la vapeur de tête (azote) de la colonne 8 en relation d'échange thermique avec le liquide de cuve (oxygène) de la colonne 9; un réservoir d'oxygène liquide 11 dont le fond est relié à une pompe d'oxygène liquide 12; et un réservoir d'azote liquide 13 dont le fond est relié à une pompe d'azote liquide 14.Thus, as described in the aforementioned US-A-5,329,776, the air distillation installation shown in FIG. 3 essentially comprises: an air compressor 1; an apparatus 2 for purifying the compressed air into water and CO 2 by adsorption, this apparatus comprising two adsorption bottles 2A, 2B, one of which operates in adsorption while the other is being regenerated; a turbine-booster assembly 3 comprising an expansion turbine 4 and a booster 5 whose shafts are coupled; a heat exchanger 6 constituting the heat exchange line of the installation; a double distillation column 7 comprising a medium pressure column 8 surmounted by a low pressure column 9, with a vaporizer-condenser 10 putting the overhead vapor (nitrogen) from column 8 in heat exchange relation with the tank liquid (oxygen) from column 9; a liquid oxygen tank 11, the bottom of which is connected to a liquid oxygen pump 12; and a liquid nitrogen tank 13, the bottom of which is connected to a liquid nitrogen pump 14.

Cette installation est destinée à fournir, via une conduite utilisatrice 15, de l'oxygène gazeux sous la pression d'utilisation P.This facility is intended to provide, via a user line 15, gaseous oxygen under the operating pressure P.

Pour cela, de l'oxygène liquide soutiré de la cuve de la colonne 9 via une conduite 16 et stocké dans le réservoir 11, est amené à la haute pression P1 (30 bars) par la pompe 12 à l'état liquide, puis vaporisé et réchauffé sous cette haute pression dans des passages 17 de l'échangeur 6, dans les conditions de la Figure 1(c), et envoyé au buffer 38. Dans les conditions de la Figure 1(d), cet oxygène est détendu en 40 et envoyé dans la conduite 15 via la conduite 39.For this, liquid oxygen drawn from the column 9 tank via line 16 and stored in the reservoir 11 is brought to the high pressure P1 (30 bars) by the pump 12 in the liquid state, then vaporized and heated under this high pressure in passages 17 of the exchanger 6, under the conditions of FIG. 1 (c), and sent to buffer 38. Under the conditions of Figure 1 (d), this oxygen is expanded at 40 and sent to the line 15 via line 39.

La chaleur nécessaire à cette vaporisation et à ce réchauffage, ainsi qu'au réchauffage et éventuellement à la vaporisation d'autres fluides soutirés de la double colonne, est fournie par l'air à distiller, dans les conditions suivantes.The heat necessary for this vaporization and to this reheating, as well as to reheating and possibly vaporization of other fluids drawn from the double column, is supplied by the air to be distilled, in the following conditions.

La totalité de l'air à distiller est comprimée par le compresseur 1 à une première haute pression nettement supérieure à la moyenne pression de la colonne 8 d'utilisation. Puis l'air, prérefroidi en 18 et refroidi au voisinage de la température ambiante en 19, est épuré dans l'une, 2A par exemple, des bouteilles d'adsorption, et surpressé en totalité par le surpresseur 5, lequel est entraíné par la turbine 4.All of the air to be distilled is compressed by compressor 1 at a first high pressure significantly higher than the average column pressure 8 of use. Then the air, precooled in 18 and cooled to around room temperature in 19, is purified in one, 2A for example, of the bottles adsorption, and fully boosted by the booster 5, which is driven by the turbine 4.

L'air est alors introduit au bout chaud de l'échangeur 6 et refroidi en totalité jusqu'à une température intermédiaire. A cette température, une fraction de l'air poursuit son refroidissement et est liquéfiée dans des passages 20 de l'échangeur, puis est détendue à la basse pression dans une vanne de détente 21 et introduite à un niveau intermédiaire dans la colonne 9. Le reste de l'air est détendue à la moyenne pression dans la turbine 4 puis envoyé directement, via une conduite 22, à la base de la colonne 8.Air is then introduced at the hot end of exchanger 6 and completely cooled to a intermediate temperature. At this temperature, a fraction of the air continues to cool and is liquefied in passages 20 of the exchanger, then is relaxed at low pressure in an expansion valve 21 and introduced at an intermediate level in the column 9. The rest of the air is relaxed to average pressure in turbine 4 then sent directly, via a pipe 22, at the base of column 8.

On reconnait par ailleurs sur la Figure 3 les conduites habituelles des installations à double colonne, celle représentée étant du type dit "à minaret", c'est-à-dire avec production d'azote sous la basse pression : les conduites 23 à 25 d'injection dans la colonne 9, à des niveaux croissants, de "liquide riche" (air enrichi en oxygène) détendu, de "liquide pauvre inférieur" (azote impur) détendu et de "liquide pauvre supérieur" (azote pratiquement pur) détendu, respectivement, ces trois fluides étant respectivement soutirés à la base, en un point intermédiaire et au sommet de la colonne 8; et les conduites 26 de soutirage d'azote gazeux partant du sommet de la colonne 9 et 27 d'évacuation du gaz résiduaire (azote impur) partant du niveau d'injection du liquide pauvre inférieur. L'azote basse pression est réchauffé dans des passages 28 de l'échangeur 6 puis évacué via une conduite 29, tandis que le gaz résiduaire, après réchauffement dans des passages 30 de l'échangeur, est utilisé pour régénérer une bouteille d'adsorption, la bouteille 2B dans l'exemple considéré, avant d'être évacué via une conduite 31.We also recognize in Figure 3 the normal pipes in double column installations, that represented being of the type known as "minaret", that is to say with nitrogen production under low pressure: injection lines 23 to 25 in column 9, at increasing levels of "rich liquid" (air enriched in oxygen) relaxed, of "lower lean liquid" (nitrogen impure) relaxed and "superior poor liquid" (nitrogen practically pure) relaxed, respectively, these three fluids being respectively drawn off at the base, in a intermediate point and at the top of column 8; and the pipes 26 for withdrawing nitrogen gas leaving from top of column 9 and 27 for discharging the residual gas (impure nitrogen) from the injection level of the lower poor liquid. Low pressure nitrogen is heated in passages 28 of exchanger 6 then evacuated via a pipe 29, while the waste gas, after heating in passages 30 of the exchanger, is used to regenerate an adsorption bottle, the 2B bottle in the example considered, before being evacuated via a pipe 31.

On voit encore sur la Figure 3 qu'une partie de l'azote liquide moyenne pression est, après détente dans une vanne de détente 32, stockée dans le réservoir 13, et qu'une production d'azote liquide et/ou d'oxygène liquide est fournie via une conduite 33 (pour l'azote) et/ou 34 (pour l'oxygène).We can still see in Figure 3 that part medium pressure liquid nitrogen is, after expansion in an expansion valve 32, stored in the tank 13, and that a production of liquid nitrogen and / or oxygen liquid is supplied via line 33 (for nitrogen) and / or 34 (for oxygen).

De plus, de l'oxygène liquide supplémentaire soutiré du réservoir 11 par la pompe 36 est vaporisé et réchauffé sous la pression d'utilisation de 16 bars dans des passages 37, dans les conditions de la Figure 1(b).In addition, additional liquid oxygen withdrawn from the tank 11 by the pump 36 is vaporized and heated under the operating pressure of 16 bars in passages 37, under the conditions of Figure 1 (b).

La pression de l'air surpressé en 5 est la pression de condensation de l'air par échange de chaleur avec l'oxygène en cours de vaporisation sous la pression d'utilisation P, c'est-à-dire la pression pour laquelle le genou 100 de liquéfaction de l'air, sur le diagramme d'échange thermique est situé légèrement à droite du palier vertical 101 de vaporisation de l'oxygène sous la pression P (Figure 4). L'écart de température au bout chaud de la ligne d'échange est ajusté au moyen de la turbine 4, dont la température d'aspiration est indiquée en 102.The pressure of the compressed air at 5 is the air condensation pressure by heat exchange with oxygen being vaporized under pressure of use P, i.e. the pressure for which air liquefaction knee 100, on the diagram heat exchange is located slightly to the right of the vertical bearing 101 for vaporizing oxygen under the pressure P (Figure 4). The temperature difference at the end heat of the exchange line is adjusted by means of the turbine 4, the suction temperature of which is indicated in 102.

En ce qui concerne ce débit d'oxygène haute pression, son palier 103 de vaporisation (Figure 4) est décalé vers la droite par rapport au genou 100 de liquéfaction de l'air surpressé, mais reste inférieur, dans cet exemple, à la température du point 102.Regarding this high oxygen flow pressure, its vaporization level 103 (Figure 4) is shifted to the right with respect to the knee 100 of liquefaction of the compressed air, but remains lower, in this example, at the temperature of point 102.

Au cours de l'intervalle de temps O, T, la longueur de chaque palier 101, 103 varie, mais la somme des deux longueurs reste constante.During the time interval O, T, the length of each bearing 101, 103 varies, but the sum of the two lengths remains constant.

Par rapport à une installation analogue à une seule pompe 12, c'est-à-dire telle que celle de la Figure 1 du US-A-5 329 776 précité, on obtient, toutes choses égales par ailleurs, un gain d'énergie dû à la présence du palier 101 en regard du genou 100. Cet excédent d'énergie peut se valoriser soit en évacuant de l'installation un supplément de liquide, généralement de l'azote liquide, soit en abaissant la pression de compression de l'air en 1, en maintenant bien entendu le genou 100 à droite du palier 101. Le gain d'énergie précité fluctue, au cours de l'intervalle de temps O, T, avec la longueur du palier 101.Compared to an installation similar to a single pump 12, that is to say such as that of FIG. 1 of the aforementioned US-A-5,329,776, one obtains, all things also equal, an energy gain due to the presence of bearing 101 opposite knee 100. This excess energy can be enhanced either by evacuating installing additional liquid, usually liquid nitrogen, either by lowering the pressure air compression in 1, of course maintaining the knee 100 to the right of landing 101. Energy saving above fluctuates, during the time interval O, T, with the length of the bearing 101.

La Figure 2 schématise la même installation en représentant seulement :

  • la boíte froide 41 de l'installation, qui en contient les parties cryogéniques;
  • les deux pompes à oxygène liquide 12 et 36, lesquelles, en pratique, sont bien entendu contenues dans la boíte froide; et
  • la conduite consommatrice 15, le buffer 38, la ligne 39 et la vanne de détente 40.
Figure 2 shows schematically the same installation by representing only:
  • the cold box 41 of the installation, which contains the cryogenic parts thereof;
  • the two liquid oxygen pumps 12 and 36, which, in practice, are of course contained in the cold box; and
  • the consumer line 15, the buffer 38, the line 39 and the expansion valve 40.

On a ainsi schématisé le fait que les deux productions d'oxygène, respectivement sous 16 bars et sous 30 bars, dont la somme des débits est constamment égale à D1, sont fournies par compression-vaporisation-réchauffement de deux débits d'oxygène liquide provenant de la colonne basse pression 9.We have thus schematized the fact that the two oxygen production, respectively under 16 bars and under 30 bars, whose sum of flows is constantly equal to D1, are supplied by compression-vaporization-heating two liquid oxygen flows from of the low pressure column 9.

En variante, au lieu d'être branchées en parallèle sur le réservoir 11, les pompes 12 et 36 peuvent être montées en série, l'aspiration de la pompe 12 étant piquée sur la conduite de refoulement de la pompe 36.Alternatively, instead of being plugged in parallel on tank 11, pumps 12 and 36 can be connected in series, the pump suction 12 being stitched on the delivery line of the pump 36.

La Figure 5 représente une variante d'installation qui diffère de la précédente par la suppression de la pompe 36 et du circuit de vaporisation-réchauffement correspondant.Figure 5 shows a variant installation which differs from the previous one by the removal of pump 36 and of the vaporization-heating circuit corresponding.

Ainsi, la totalité du débit D1 est amenée par la pompe 12 à 16 bars, vaporisé, réchauffé et envoyé dans la conduite 15.Thus, the entire flow D1 is brought by the pump 12 to 16 bars, vaporized, heated and sent to driving 15.

Dans les conditions de la Figure 1(c), de l'oxygène est prélevé en un point 42 de la conduite 15, comprimé à 30 bars par un compresseur d'oxygène 43 et envoyé au buffer 38. Ce dernier est comme précédemment relié à la conduite 15 par la conduite 39 équipée de la vanne 40.Under the conditions of Figure 1 (c), of the oxygen is taken from a point 42 of the pipe 15, compressed to 30 bar by an oxygen compressor 43 and sent to buffer 38. The latter is as before connected to line 15 via line 39 fitted with the valve 40.

Dans la variante de la Figure 6, l'unique pompe 12 amène le débit D1 à 30 bars. Une fraction de ce débit est détendue à 16 bars dans une vanne de détente 143 et vaporisée, dans les conditions de la Figure 1(b), et envoyée à la conduite 15. Le reste du liquide est vaporisé sous la haute pression de 30 bars et envoyé au buffer 38.In the variant of Figure 6, the only pump 12 brings the flow D1 to 30 bars. A fraction of this flow is expanded to 16 bars in an expansion valve 143 and vaporized, under the conditions of Figure 1 (b), and sent to line 15. The rest of the liquid is sprayed under the high pressure of 30 bars and sent to the buffer 38.

Les Figures 7 et 8 représentent une autre variante de l'installation qui ne diffère de celle des Figures 2 et 3 que par le fait que l'oxygène à 16 bars est soutiré sous forme gazeuse de la cuve de la colonne basse pression 9, via une conduite 44, réchauffé sous la basse pression dans des passages 45 de la ligne d'échange 6, et porté à 16 bars par un compresseur d'oxygène 46. L'oxygène à 30 bars, quant à lui, est soutiré du réservoir 11 par la pompe 12, qui l'amène à cette haute pression sous forme liquide, puis est vaporisé et réchauffé dans les passages 17, et est envoyé directement au buffer 38.Figures 7 and 8 show another variant of the installation which does not differ from that of Figures 2 and 3 only by the fact that the oxygen at 16 bars is withdrawn in gaseous form from the column tank low pressure 9, via a line 44, heated under the low pressure in passages 45 of the exchange line 6, and brought to 16 bars by an oxygen compressor 46. Oxygen at 30 bar is drawn from the tank 11 by pump 12, which brings it to this high pressure in liquid form and then is vaporized and warmed in passages 17, and is sent directly to buffer 38.

Dans les modes de réalisation qui précèdent, il est possible d'ajouter une capacité-tampon d'air liquide, afin d'amortir les variations dans le temps du débit d'air liquéfié alimentant la double colonne.In the foregoing embodiments, it is possible to add an air buffer capacity liquid, to absorb variations over time liquefied air flow supplying the double column.

Les Figures 9 et 10 illustrent la mise en oeuvre de l'invention avec un appareil classique de distillation d'air sans pompe, à cycle azote (turbine 47 détendant à la basse pression de l'azote moyenne pression) et à colonne de séparation d'argon (non représentée) couplée à la colonne basse pression par deux conduites 48.Figures 9 and 10 illustrate the implementation work of the invention with a conventional apparatus of air distillation without pump, nitrogen cycle (turbine 47 releasing at low pressure medium pressure nitrogen) and an argon separation column (not shown) coupled to the low pressure column by two lines 48.

Dans ce cas, le débit D1 d'oxygène est soutiré sous forme gazeuse de la cuve de la colonne basse pression et, après réchauffement, est comprimé à 16 bars et/ou à 30 bars, dans les conditions décrites plus haut, par deux compresseurs d'oxygène respectifs 49 et 50. Le compresseur 49 refoule directement dans la conduite 15, tandis que le compresseur 50 refoule dans le buffer 38.In this case, the oxygen flow D1 is withdrawn in gaseous form from the bottom column tank pressure and, after heating, is compressed to 16 bars and / or at 30 bars, under the conditions described above, by two respective oxygen compressors 49 and 50. The compressor 49 discharges directly into line 15, while compressor 50 backs up in buffer 38.

L'installation des Figures 11 et 12 ne diffère de la précédente que par le fait que les deux compresseurs d'oxygène sont montés en série au lieu d'être montés en parallèle. Ainsi, le compresseur 49 comprime la totalité du débit D1 à 16 bars, et le compresseur 50 porte de 16 à 30 bars le débit d2 décrit en regard de la Figure 1(c).The installation of Figures 11 and 12 does not differs from the previous one only in that the two oxygen compressors are connected in series instead to be mounted in parallel. So the compressor 49 compresses the entire flow D1 to 16 bars, and the compressor 50 carries from 16 to 30 bars the flow d2 described next to Figure 1 (c).

Bien entendu, les compresseurs 49 et 50 peuvent être constitués par deux étages ou groupes d'étages d'une même machine.Of course, compressors 49 and 50 can be made up of two floors or groups stages of the same machine.

Dans tout ce qui précède, on a appelé "pression d'utilisation" la pression de la conduite 15. Toutefois, ceci n'exclut pas une modification ultérieure de cette pression, par exemple par détente.In all of the above, we have called "operating pressure" means the pressure in line 15. However, this does not exclude a subsequent modification of this pressure, for example by expansion.

Par ailleurs, dans chaque mode de réalisation de l'installation, le régulateur de pression 138 peut être supprimé. La pression du buffer évolue alors entre les pressions P et P1 en fonction du temps.Furthermore, in each embodiment of the installation, the pressure regulator 138 can be deleted. The buffer pressure then changes between pressures P and P1 as a function of time.

En variante encore, le procédé de l'invention peut utiliser plusieurs buffers à des hautes pressions P1, P2, ... différentes, toutes nettement supérieures à la pression d'utilisation P. Lorsque le débit demandé est supérieur à D1, on prélève alors du gaz dans l'un ou l'autre des buffers, suivant les variations de ce débit.In another variant, the method of the invention can use multiple buffers at high pressures P1, P2, ... different, all significantly greater than the operating pressure P. When the requested flow is greater than D1, gas is then taken from one or the other of the buffers, according to the variations of this flow.

Claims (16)

Procédé pour fournir à une conduite consommatrice (15), pendant un intervalle de temps (O, T), un débit demandé variable (D) d'un constituant de l'air, notamment d'oxygène, produit par un appareil de distillation d'air (7), caractérisé en ce que : on soutire de l'appareil (7) un débit total dudit constituant de valeur constante (D1) ; on divise l'intervalle de temps (O, T) en plusieurs types de périodes, à savoir : éventuellement, au moins une première période (t1 à t2) pendant laquelle le débit demandé (D) est égal audit débit total (D1) ; au moins une deuxième période (0 à t1, t4 à T) pendant laquelle le débit demandé (D) est inférieur audit débit total (D1) ; et au moins une troisième période (t2 à t4) pendant laquelle le débit demandé (D) est supérieur audit débit total (D1) ; pendant ladite ou lesdites premières périodes, on amène ledit débit total (D1) à la pression d'utilisation (P), et on l'envoie à la conduite consommatrice (15) ; pendant ladite ou lesdites deuxièmes périodes : on amène le débit demandé (D) à la pression d'utilisation, et on l'envoie à la conduite consommatrice (15) ; et on amène à une haute pression (P1) supérieure à la pression d'utilisation (P) un débit de stockage (d2) dudit constituant égal à la différence entre ledit débit total (D1) et le débit demandé (D), et on stocke ce débit de stockage dans au moins une capacité-tampon (38) ; et pendant ladite ou lesdites troisièmes périodes : on amène ledit débit total (D1) à la pression d'utilisation (P), et on l'envoie à la conduite consommatrice (15) ; et on envoie en outre dans la conduite consommatrice (15) un débit complémentaire (d3) dudit constituant égal à la différence entre le débit demandé (D) et ledit débit total (D1), ce débit complémentaire étant prélevé dans au moins une capacité-tampon (38) et détendu à la pression d'utilisation (P). Method for supplying a consuming line (15), during a time interval (O, T), with a variable demand flow (D) of an air component, in particular oxygen, produced by a distillation apparatus d 'air (7), characterized in that: withdrawing from the apparatus (7) a total flow of said constituent of constant value (D1); we divide the time interval (O, T) into several types of periods, namely: optionally, at least a first period (t1 to t2) during which the requested flow rate (D) is equal to said total flow rate (D1); at least a second period (0 to t1, t4 to T) during which the requested flow (D) is less than said total flow (D1); and at least a third period (t2 to t4) during which the requested flow (D) is greater than said total flow (D1); during said one or more first periods, said total flow rate (D1) is brought to the operating pressure (P), and it is sent to the consuming line (15); during said second period (s): the requested flow rate (D) is brought to the operating pressure, and it is sent to the consuming line (15); and a storage flow (d2) of said constituent is brought to a high pressure (P1) greater than the operating pressure (P) equal to the difference between said total flow (D1) and the requested flow (D), and it is stored this storage rate in at least one buffer capacity (38); and during said third period (s): said total flow (D1) is brought to the operating pressure (P), and it is sent to the consuming line (15); and a complementary flow (d3) of said constituent is also sent to the consuming line (15) equal to the difference between the requested flow (D) and said total flow (D1), this additional flow being taken from at least one buffer capacity (38) and relaxed to the operating pressure (P). Procédé suivant la revendication 1, caractérisé en ce qu'on soutire ledit débit total (D1) sous forme liquide de l'appareil de distillation (7), et on le comprime sous cette forme par pompage (en 12, 36) avant de le vaporiser (en 6).Method according to claim 1, characterized in that said total flow (D1) is drawn off in liquid form from the distillation apparatus (7), and it is compressed in this form by pumping (in 12, 36) before spraying (in 6). Procédé suivant la revendication 2, caractérisé en ce qu'on amène à la pression d'utilisation (P) un premier débit de liquide au moyen d'une première pompe (12), on amène à la haute pression (P1) le débit destiné à la capacité-tampon(38) au moyen d'une seconde pompe (36), et on vaporise (en 17, 37) chaque flux de liquide sous sa pression de pompage (Figures 2 et 3).Method according to claim 2, characterized in that it brings to the working pressure (P) a first flow of liquid by means of a first pump (12), the flow is brought to high pressure (P1) intended for the buffer tank (38) by means of a second pump (36), and one vaporizes (in 17, 37) each flow of liquid under its pumping pressure (Figures 2 and 3). Procédé suivant la revendication 2, caractérisé en ce qu'on amène ledit débit total (D1) à la pression d'utilisation (P) au moyen d'une pompe unique (12), on vaporise ce liquide (en 17) et on porte à la haute pression (P1) la fraction du gaz ainsi obtenu qui est destinée à la capacité-tampon (38) (Figure 5).Method according to claim 2, characterized in that said total flow (D1) is brought to operating pressure (P) by means of a single pump (12), this liquid is vaporized (in 17) and brought to the high pressure (P1) the fraction of the gas thus obtained which is intended for the buffer tank (38) (Figure 5). Procédé suivant la revendication 2, caractérisé en ce qu'on amène ledit débit total (D1) à la haute pression (P1) au moyen d'une pompe unique (12), on détend (en 143) une fraction de ce débit total à la pression d'utilisation (P), et on vaporise les deux flux chacun sous sa pression (Figure 6).Method according to claim 2, characterized in that said total flow (D1) is brought to high pressure (P1) by means of a single pump (12), we relax (in 143) a fraction of this total flow at the operating pressure (P), and the two flows are vaporized each under pressure (Figure 6). Procédé suivant la revendication 1, caractérisé en ce qu'on soutire sous forme liquide de l'appareil de distillation (7) un premier des deux débits, on le comprime par pompage (en 12), et on le vaporise sous cette pression (en 17) ; et on soutire sous forme gazeuse de l'appareil de distillation le reste dudit débit total, et on le comprime sous cette forme (en 46) (Figures 7 et 8).Method according to claim 1, characterized in that it is drawn off in liquid form from the distillation apparatus (7) a first of the two flow rates, it is compressed by pumping (in 12), and it is vaporizes under this pressure (in 17); and we draw under gaseous form of the distillation apparatus the rest of said total flow, and it is compressed in this form (in 46) (Figures 7 and 8). Procédé suivant la revendication 1, caractérisé en ce qu'on soutire ledit débit total (D1) sous forme gazeuse de l'appareil de distillation (7), on comprime à la pression d'utilisation (P) une fraction (dl) de ce gaz, et on comprime à la haute pression (P1) (en 50) le débit complémentaire (d2) destiné à la capacité-tampon (38) (Figures 9 à 12).Method according to claim 1, characterized in that said total flow (D1) is drawn off in the gaseous form of the distillation apparatus (7), compresses at operating pressure (P) a fraction (dl) of this gas, and it is compressed at high pressure (P1) (at 50) the additional flow (d2) intended for the buffer capacity (38) (Figures 9 to 12). Procédé suivant la revendication 7, caractérisé en ce qu'on comprime chaque débit indépendamment à partir de la pression de soutirage de l'appareil de distillation (7) (Figures 9 et 10).Process according to claim 7, characterized in that each flow is compressed independently from the device withdrawal pressure distillation (7) (Figures 9 and 10). Procédé suivant la revendication 7, caractérisé en ce qu'on comprime ledit débit total (D1) à la pression d'utilisation (P), et on comprime une fraction de ce premier débit de la pression (P) d'utilisation à la haute pression (P1) (Figures 11 et 12).Process according to claim 7, characterized in that said total flow is compressed (D1) at the operating pressure (P), and a fraction of this first pressure flow (P) of use at high pressure (P1) (Figures 11 and 12). Installation de distillation d'air destinée à fournir à une conduite consommatrice (15) un débit variable d'un constituant de l'air, notamment d'oxygène, caractérisée en ce qu'elle comprend des moyens pour soutirer de l'appareil de distillation (7) un débit total constant (D1) dudit constituant ; une capacité-tampon (38) ; des premiers moyens pour amener une partie au moins dudit débit total (D1) à la pression d'utilisation (P) et sous forme gazeuse, ces premiers moyens étant reliés à la conduite consommatrice (15) ; des seconds moyens pour amener un second débit (d2) dudit constituant à une haute pression (P1) supérieure à la pression d'utilisation (P) et sous forme gazeuse, ces seconds moyens étant reliés à la capacité-tampon (38) ; et une conduite auxiliaire (39) munie d'une vanne de détente commandée (40), reliant la capacité-tampon à la conduite consommatrice (15).Air distillation plant intended to provide a consumer line (15) with a variable flow of an air component, in particular oxygen, characterized in that it comprises means for withdrawing from the distillation apparatus (7) a flow constant total (D1) of said constituent; a buffer capacity (38); first means to bring a party at least said total flow (D1) at pressure of use (P) and in gaseous form, these first means being connected to the consumer line (15); of second means for bringing a second flow (d2) of said constituting at a high pressure (P1) greater than the operating pressure (P) and in gaseous form, these second means being connected to the buffer capacity (38); and an auxiliary line (39) provided with a shut-off valve controlled trigger (40), connecting the buffer capacity to the consumer line (15). Installation suivant la revendication 10, caractérisée en ce que les premiers moyens comprennent une première pompe (12) et des premiers moyens de vaporisation (17), et en ce que les seconds moyens comprennent une seconde pompe (36) et des seconds moyens de vaporisation (37) (Figures 2 et 3).Installation according to claim 10, characterized in that the first means include a first pump (12) and first means of vaporization (17), and in that the second means comprise a second pump (36) and second means spray (37) (Figures 2 and 3). Installation suivant la revendication 10, caractérisée en ce que les premiers moyens comprennent une pompe (12) et des moyens de vaporisation (17), et en ce que les seconds moyens comprennent un compresseur (43) dont l'aspiration est reliée à la sortie des moyens de vaporisation (Figure 5).Installation according to claim 10, characterized in that the first means include a pump (12) and vaporization means (17), and in that the second means comprise a compressor (43) whose suction is connected to the outlet of the vaporization means (Figure 5). Installation suivant la revendication 10, caractérisée en ce que les premiers moyens comprennent une pompe (12), une vanne de détente (143) et des premiers moyens de vaporisation (17), et en ce que les seconds moyens comprennent des seconds moyens de vaporisation (37) reliés au refoulement de la pompe (Figure 6).Installation according to claim 10, characterized in that the first means include a pump (12), an expansion valve (143) and first vaporization means (17), and in that the second means include second spray means (37) connected to the pump discharge (Figure 6). Installation suivant la revendication 10, caractérisée en ce que les premiers moyens comprennent un compresseur (46) dont l'aspiration est reliée à un point de soutirage de gaz de l'appareil de distillation (7), et en ce que les seconds moyens comprennent une pompe (12) et des moyens de vaporisation (17) reliés au refoulement de cette pompe (Figures 7 et 8).Installation according to claim 10, characterized in that the first means include a compressor (46) whose suction is connected to a gas withdrawal point from the distillation apparatus (7), and in that the second means include a pump (12) and vaporization means (17) connected to the discharge of this pump (Figures 7 and 8). Installation suivant la revendication 10, caractérisé en ce que les premiers et les seconds moyens comprennent respectivement deux compresseurs (49, 50) dont les aspirations sont reliées en parallèle à un point de soutirage de l'appareil de distillation (7) (Figures 9 et 10).Installation according to claim 10, characterized in that the first and the second means respectively comprise two compressors (49, 50) whose aspirations are connected in parallel to a draw-off point of the distillation apparatus (7) (Figures 9 and 10). Installation suivant la revendication 10, caractérisé en ce que les premiers moyens comprennent un premier compresseur (49) dont l'aspiration est reliée à un point de soutirage de gaz de l'appareil de distillation (7), et en ce que les seconds moyens comprennent un second compresseur (50) dont l'aspiration est reliée au refoulement du premier compresseur (Figures 11 et 12).Installation according to claim 10, characterized in that the first means include a first compressor (49) whose suction is connected at a gas withdrawal point from the distillation apparatus (7), and in that the second means include a second compressor (50) whose suction is connected to the delivery of the first compressor (Figures 11 and 12).
EP97402990A 1996-12-12 1997-12-10 Method and plant for supplying an air gas at variable quantities Revoked EP0848220B1 (en)

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FR9615281A FR2757282B1 (en) 1996-12-12 1996-12-12 METHOD AND INSTALLATION FOR PROVIDING A VARIABLE FLOW OF AN AIR GAS
FR9615281 1996-12-12

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0895045A2 (en) * 1997-07-30 1999-02-03 Linde Aktiengesellschaft Air separation process
WO2016025063A1 (en) * 2014-07-28 2016-02-18 Praxair Technolgy, Inc. Air separation method and apparatus

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2751737B1 (en) * 1996-07-25 1998-09-11 Air Liquide METHOD AND INSTALLATION FOR PRODUCING A VARIABLE FLOW AIR GAS
DE10013075A1 (en) * 2000-03-17 2001-09-20 Linde Ag Process for recovering gaseous nitrogen by the decomposition of air in a distillation column system comprises removing a part of the nitrogen-rich liquid from the condenser-vaporizer as a liquid product
US6357259B1 (en) * 2000-09-29 2002-03-19 The Boc Group, Inc. Air separation method to produce gaseous product
EP1207362A1 (en) 2000-10-23 2002-05-22 Air Products And Chemicals, Inc. Process and apparatus for the production of low pressure gaseous oxygen
EP1202013B3 (en) * 2000-10-23 2009-04-01 Air Products And Chemicals, Inc. Process and apparatus for the production of low pressure gaseous oxygen
GB0219415D0 (en) * 2002-08-20 2002-09-25 Air Prod & Chem Process and apparatus for cryogenic separation process
FR2854683B1 (en) * 2003-05-05 2006-09-29 Air Liquide METHOD AND INSTALLATION FOR PRODUCING PRESSURIZED AIR GASES BY AIR CRYOGENIC DISTILLATION
FR2872262B1 (en) * 2004-06-29 2010-11-26 Air Liquide METHOD AND INSTALLATION FOR PROVIDING SUPPORT OF A PRESSURIZED GAS
US7409835B2 (en) * 2004-07-14 2008-08-12 Air Liquide Process & Construction, Inc. Backup system and method for production of pressurized gas
AU2005225027A1 (en) * 2005-07-21 2007-02-08 L'air Liquide Societe Anonyme Pour L'etude Et L"Exploitation Des Procedes Georges Claude Process and apparatus for the separation of air by cryogenic distillation
FR2895068B1 (en) * 2005-12-15 2014-01-31 Air Liquide AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION
JP4688843B2 (en) * 2007-05-07 2011-05-25 株式会社神戸製鋼所 Air separation device
US7821158B2 (en) * 2008-05-27 2010-10-26 Expansion Energy, Llc System and method for liquid air production, power storage and power release
CN101769438A (en) * 2008-12-30 2010-07-07 湖北宜化化工股份有限公司 Method for running gas passing through gas cabinet by near path
US8623107B2 (en) 2009-02-17 2014-01-07 Mcalister Technologies, Llc Gas hydrate conversion system for harvesting hydrocarbon hydrate deposits
JP5407661B2 (en) * 2009-08-26 2014-02-05 Ｊｆｅスチール株式会社 Oxygen supply equipment and oxygen supply method
CN102072612B (en) * 2010-10-19 2013-05-29 上海加力气体有限公司 N-type pattern energy-saving gas manufacturing method
CN103575064B (en) * 2012-07-23 2015-10-28 中国石油化工股份有限公司 A kind of air separation oxygen nitrogen increases the device and method of pressure nitrogen gas load fast
US9631863B2 (en) * 2013-03-12 2017-04-25 Mcalister Technologies, Llc Liquefaction systems and associated processes and methods
US8907524B2 (en) 2013-05-09 2014-12-09 Expansion Energy Llc Systems and methods of semi-centralized power storage and power production for multi-directional smart grid and other applications
US10119756B2 (en) 2013-10-23 2018-11-06 Praxair Technology, Inc. Oxygen backup method and system
US20150168056A1 (en) * 2013-12-17 2015-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method For Producing Pressurized Gaseous Oxygen Through The Cryogenic Separation Of Air
DE102016004606A1 (en) * 2016-04-14 2017-10-19 Linde Aktiengesellschaft Process engineering plant and process for liquefied gas production
US10260801B2 (en) * 2016-06-30 2019-04-16 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes George Claude Method for operating an air separation plant

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1172934A (en) * 1966-03-14 1969-12-03 Air Reduction A Low-Temperature Regenerator and its use in Gas Storage
EP0250390A2 (en) * 1986-05-14 1987-12-23 VOEST-ALPINE Aktiengesellschaft Air-separating device using storage of a product gas in liquefied form
EP0628778A1 (en) * 1993-06-07 1994-12-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and high pressure gas supply unit for an air constituent consuming installation

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS61190277A (en) * 1985-02-16 1986-08-23 大同酸素株式会社 High-purity nitrogen and oxygen gas production unit
DE3913880A1 (en) * 1989-04-27 1990-10-31 Linde Ag METHOD AND DEVICE FOR DEEP TEMPERATURE DISPOSAL OF AIR
FR2670278B1 (en) * 1990-12-06 1993-01-22 Air Liquide METHOD AND INSTALLATION FOR AIR DISTILLATION IN A VARIABLE REGIME FOR THE PRODUCTION OF GASEOUS OXYGEN.
US5224336A (en) * 1991-06-20 1993-07-06 Air Products And Chemicals, Inc. Process and system for controlling a cryogenic air separation unit during rapid changes in production
FR2697620B1 (en) * 1992-10-30 1994-12-23 Air Liquide Process and installation for the production of nitrogen gas with variable flow.
FR2716816B1 (en) * 1994-03-02 1996-05-03 Air Liquide Method for restarting an auxiliary argon / oxygen separation column by distillation, and corresponding installation.

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1172934A (en) * 1966-03-14 1969-12-03 Air Reduction A Low-Temperature Regenerator and its use in Gas Storage
EP0250390A2 (en) * 1986-05-14 1987-12-23 VOEST-ALPINE Aktiengesellschaft Air-separating device using storage of a product gas in liquefied form
EP0628778A1 (en) * 1993-06-07 1994-12-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and high pressure gas supply unit for an air constituent consuming installation

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0895045A2 (en) * 1997-07-30 1999-02-03 Linde Aktiengesellschaft Air separation process
EP0895045A3 (en) * 1997-07-30 1999-06-16 Linde Aktiengesellschaft Air separation process
US6038885A (en) * 1997-07-30 2000-03-21 Linde Aktiengesellschaft Air separation process
WO2016025063A1 (en) * 2014-07-28 2016-02-18 Praxair Technolgy, Inc. Air separation method and apparatus

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CN1130538C (en) 2003-12-10
FR2757282B1 (en) 2006-06-23
JPH10259990A (en) 1998-09-29
ES2216119T3 (en) 2004-10-16
DE69727648D1 (en) 2004-03-25
US5941098A (en) 1999-08-24
BR9705641A (en) 1999-05-25
EP0848220B1 (en) 2004-02-18
KR100474464B1 (en) 2005-06-17
ZA9711131B (en) 1998-06-23
PL323709A1 (en) 1998-06-22
CA2224742A1 (en) 1998-06-12
KR19980063916A (en) 1998-10-07
CN1190726A (en) 1998-08-19
DE69727648T2 (en) 2004-10-14
AR008937A1 (en) 2000-02-23
FR2757282A1 (en) 1998-06-19

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