EP1284403B1 - Procédé et appareil de production d'oxygène par séparation d'air cryogénique - Google Patents

Procédé et appareil de production d'oxygène par séparation d'air cryogénique Download PDF

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Publication number
EP1284403B1
EP1284403B1 EP01125721A EP01125721A EP1284403B1 EP 1284403 B1 EP1284403 B1 EP 1284403B1 EP 01125721 A EP01125721 A EP 01125721A EP 01125721 A EP01125721 A EP 01125721A EP 1284403 B1 EP1284403 B1 EP 1284403B1
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Prior art keywords
column
oxygen
stream
air
pressure column
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German (de)
English (en)
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EP1284403A1 (fr
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Stefan Dipl.-Ing. Lochner
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Linde GmbH
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Linde GmbH
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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
    • F25J3/04248—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
    • F25J3/04006—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
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • 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
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air

Definitions

  • the invention relates to a method for generating oxygen by Cryogenic decomposition of air in a distillation system containing an oxygen column having a first air flow work expanded and at least partially is introduced into the oxygen column, another feed stream whose Oxygen content is at least equal to that of the feed air, upside down Oxygen column is abandoned, at least one oxygen product stream from the Lower portion of the oxygen column is removed and a residual gas stream from the head the oxygen column is withdrawn.
  • the invention is based on the object, a method and an apparatus specify that with relatively little equipment and / or energy costs allow a particularly high liquid production, in particular the production corresponding amounts of liquid oxygen and / or liquid nitrogen in the Distillation system should be possible.
  • This object is achieved in that the residual gas stream from the head of Oxygen column work is relaxed. In this way can additionally cold be recovered for product liquefaction without requiring a lot of hassle like a additional externally driven compressor or even a cycle would be necessary.
  • the oxygen column is under a superatmospheric pressure operated.
  • the operating pressure of the oxygen column is at least for example 1.7 bar, preferably 1.7 to 3.5 bar, most, preferably 2.0 to 3.0 bar.
  • the oxygen column is a single column educated. This is done by indirect heat exchange with a heating medium boiled. As a heating means, a second air flow is preferably used. This can, for example, together with the first air flow on the required Pressure to be compressed. The second air stream condenses in the indirect Heat exchange partially or completely and then as another Feed stream to the head of the oxygen column abandoned.
  • the distillation system has two columns, a high pressure column and a low pressure column, via a condenser-evaporator to be in heat exchanging connection.
  • the oxygen column is going through formed the low-pressure column of the two-pillar system.
  • a second airflow is in introduced the high pressure column.
  • High pressure column and low pressure column can as Double column with intermediate main condenser (condenser-evaporator) be educated.
  • the additional feed stream for the oxygen column (low-pressure column) is preferably in this case by a liquid oxygen-enriched fraction formed from the lower part of the high-pressure column. This points in general an oxygen concentration of, for example, 20 to 41 mol%, preferably 21 to 30 mol% on.
  • the residual gas stream which is removed at the low-pressure column head, so it is not pure Nitrogen product, but has an oxygen content less than 21 mol%, but at least 5 mol%, in particular at least 10 mol%.
  • the oxygen content of the residual gas stream is 14 to 18 mol%, preferably at 15 to 17 mol%.
  • the cooling capacity at the work-performing relaxation of the first air flow can be increased in both variants of the invention in that the first air flow is recompressed upstream of his work-relaxing relaxation.
  • the Re-compaction may be done separately or together with one or more others Air currents take place. For example, the total air can be recompressed. At least a part of the work-performing relaxation of the first air flow and / or the residual gas flow generated mechanical energy can thereby for the Re-compaction be used.
  • the invention also relates to a device for the cryogenic separation of air according to claim 8.
  • compressed and purified air is introduced via line 1. It is under a pressure of for example 10.5 bar and is divided into a first air stream 2 and a second air stream 3. Both are cooled in a main heat exchanger 4.
  • the first air flow is the main heat exchanger at an intermediate temperature (between the hot and the cold end) removed via line 21 and in a first expansion machine 22 working to a pressure of about 3 bar relaxed.
  • the work-performing relaxed first air flow becomes completely or partially fed via line 23 of the low-pressure column 7 of a double-column system, the also a high-pressure column 6 and a main condenser (condenser-evaporator) 8 has.
  • the low-pressure column here forms the oxygen column in the sense of the invention.
  • a portion (generally 0 to 60%, for example 50%) of that in FIG relaxed air can via an air bypass line 46 at the low pressure column. 7 be passed.
  • the bottom of the low-pressure column 7 is oxygen 16 - in the present example exclusively in liquid form - taken as oxygen product stream 16.
  • a residual gas stream 17 having an oxygen content of For example, 15 mol% deducted and in the main heat exchanger 4 to a Warmed intermediate temperature, which is about equal to the temperature of the first air flow 21 before his work-relaxing relaxation is 22.
  • the heated residual gas 18 is in a second expansion machine 19 work-relaxed, via line 20 fed back to the cold end of the main heat exchanger 4 and at about Ambient temperature warmed up.
  • the bypass line 24 is used to control the Cooling capacity of the expansion machine 19.
  • the hot residual gas 25 can as Regenerating gas for a (not shown) device for cleaning the feed air be used.
  • the two expansion machines 22, 19 are preferably by expansion turbines educated.
  • braking devices 26, 27 all known means come in Question; In the example of FIG. 1, dissipative brakes or generators are used used.
  • the first expansion machine 22 in FIG. 2 is formed by a booster (turbine booster) 227.
  • a booster turbine booster
  • This serves for the recompression of the first air stream 2, 229 to a pressure which is higher than the pressure prevailing in line 1 pressure.
  • the first air stream 202 is heated in a heat exchanger 228, compressed in the secondary compressor 227, passed through an aftercooler 230, cooled again in the heat exchanger 228 and fed via line 231 analogous to Figure 1 the warm end of the main heat exchanger 4.
  • Heat exchanger 228 is for optimization, but may be omitted to reduce equipment costs.
  • a further after-compressor 332 which is driven by the second expansion machine 19 and effects a further pressure increase in the first air stream 231, is connected between the after-compressor 227 and the aftercooler 230.
  • a further aftercooler (intercooler) could be arranged.
  • Another possible modification is the use of a heat exchanger as shown at 228 in FIG.
  • the first after-compressor 227 could be coupled to the second expansion machine 19.
  • the high pressure column can be omitted, as shown in FIG .
  • the distillation system is formed by an oxygen column formed as a single column 407 with bottom reboiler 408.
  • the second air stream 409 is condensed under a pressure of about 10 bar in the liquefaction space of the bottom reboiler 408.
  • the liquefied air 405 is - subcooled analogously to the bottom liquid of the high-pressure column in Figure 1 in the main heat exchanger 4 and 414 and 415 on the top of the column 407 abandoned, which is operated at about 3 bar.
  • the remaining process steps are the same as in Figure 1.
  • the turbine booster circuits of Figures 2 and 3 can be applied to the column configuration shown in Figure 4.
  • Figure 5 is based on the embodiment of Figure 3 and shows a number of additional options, which - as shown - together or individually within the scope of the invention can be realized.
  • the subcooling countercurrent 533 in which the bottom liquid 5 of the High-pressure column 6 is cooled against residual gas 17 from the top of the low-pressure column 7, is designed as a separate heat exchanger and not in the main heat exchanger 504 integrated.
  • Liquid nitrogen from the high-pressure column 6 and the Main capacitor 8 is not only obtained directly as a liquid product 513, but also fed via line 535 an internal compression.
  • the liquid is in a pump 536 brought to the desired high product pressure, via line 537 led to the main heat exchanger 504, there against the second air stream.
  • 3 evaporated (or pseudo-evaporated, if the product pressure is supercritical) and finally warmed to ambient temperature.
  • line 538 is now a Nitrogen product (PGAN-IC) under particularly high pressure available.
  • an oxygen product stream may be internally compressed.
  • liquid oxygen from the lower region of Low pressure column 7 taken from the bottom or - as shown - from above the sump
  • a pump 540 to the desired high product pressure brought, led via line 541 to the main heat exchanger 504, there against the second air stream 3 evaporates (or pseudo-evaporates if the product pressure is supercritical) and finally warmed to ambient temperature.
  • An oxygen product (GOX-IC) is now available under high pressure.
  • the supercooled oxygen-enriched liquid 14 from the high pressure column 6 becomes after their relaxation, first introduced into a separator (phase separator) 543. From there, only the liquid portion 544 flows as another feed stream to the head of the Low pressure column 7, while the steam 545 introduced directly into the residual gas line 17 becomes.
  • the phase separation may alternatively to that shown in the drawing Embodiment take place in a separator arranged inside the column, or in a simple channel, preferably at the top of the low-pressure column. Via a further bypass line 546, a part of the air 23 relaxed in FIG the low pressure column 7 are passed.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)

Claims (8)

  1. Procédé de production d'oxygène par séparation d'air cryogénique dans un système de distillation, qui présente une colonne d'oxygène, où
    un premier courant d'air (2, 21, 229, 231) est détendu (22) en fournissant du travail et est introduit au moins en partie dans la colonne d'oxygène (7, 407),
    un autre courant de charge (5, 14, 405, 414), dont la teneur en oxygène est au moins égale à celle de l'air de charge, est alimenté à la tête de la colonne d'oxygène (7, 407),
    au moins un courant de produit d'oxygène (16, 539) est prélevé de la région inférieure de la colonne d'oxygène (7, 407) et
    un courant de gaz résiduel (17, 18, 20, 25) est extrait de la tête de la colonne d'oxygène (7, 407),
    caractérisé en ce que le courant de gaz résiduel (17, 18, 20, 25) est détendu (19) en fournissant du travail.
  2. Procédé selon la revendication 1, caractérisé en ce que la colonne d'oxygène est réalisée sous forme de colonne simple (407) et est chauffée par échange thermique indirect (408) avec un agent chauffant (409).
  3. Procédé selon la revendication 2, caractérisé en ce que l'on utilise un deuxième courant d'air (409) en tant qu'agent chauffant.
  4. Procédé selon la revendication 3, caractérisé en ce que le deuxième courant d'air (414) en aval de l'échange thermique indirect (408) pour chauffer la colonne simple (407) est utilisé au moins en partie en tant que courant de charge supplémentaire pour la colonne simple (407).
  5. Procédé selon la revendication 1, caractérisé en ce que la colonne d'oxygène est réalisée sous forme de colonne basse pression (7) d'un système à deux colonnes, qui présente en outre une colonne haute pression (6), la colonne basse pression (7) et la colonne haute pression (6) étant en liaison par échange thermique par le biais d'un condensateur-évaporateur (8) et un deuxième courant d'air (3, 9) étant introduit dans la colonne haute pression (6).
  6. Procédé selon la revendication 5, caractérisé en ce qu'une fraction fluide enrichie en oxygène (5) est extraite de la région inférieure de la colonne haute pression (6) et est utilisée en tant que courant de charge supplémentaire (14) pour la colonne basse pression (7).
  7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que le premier courant d'air (202) en amont de sa détente (22) produisant du travail est recomprimé (227, 332), au moins une partie de l'énergie mécanique produite lors de la détente (22, 19) produisant du travail du premier courant d'air (231) et/ou du courant de gaz résiduel (18) étant utilisée pour la recompression.
  8. Dispositif de production d'oxygène par séparation d'air cryogénique, comprenant un système de distillation qui présente une colonne d'oxygène,
    avec une première conduite d'air (2, 21, 23, 229, 231), qui conduit à travers une première machine de détente (22) dans la colonne d'oxygène (7, 407),
    avec une autre conduite de charge (5, 14, 405, 414) pour l'introduction d'un courant de charge supplémentaire, dont la teneur en oxygène est au moins égale à celle de l'air de charge, dans la tête de la colonne d'oxygène (7, 407),
    avec une conduite de produit d'oxygène (16, 539), qui est connectée à la région inférieure de la colonne d'oxygène (7, 407) et
    avec une conduite de gaz résiduel (17, 18, 20, 25), qui est connectée à la tête de la colonne d'oxygène (7, 407),
    caractérisé par une deuxième machine de détente (19) qui est disposée dans la conduite de gaz résiduel (17, 18, 20, 25).
EP01125721A 2001-08-09 2001-10-27 Procédé et appareil de production d'oxygène par séparation d'air cryogénique Expired - Lifetime EP1284403B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10139097 2001-08-09
DE10139097A DE10139097A1 (de) 2001-08-09 2001-08-09 Verfahren und Vorrichtung zur Erzeugung von Sauerstoff durch Tieftemperatur-Zerlegung von Luft

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EP1284403A1 EP1284403A1 (fr) 2003-02-19
EP1284403B1 true EP1284403B1 (fr) 2005-12-21

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DE (2) DE10139097A1 (fr)

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Publication number Priority date Publication date Assignee Title
DE102006012241A1 (de) * 2006-03-15 2007-09-20 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP2520886A1 (fr) * 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1229561B (de) * 1962-12-21 1966-12-01 Linde Ag Verfahren und Vorrichtung zum Zerlegen von Luft durch Verfluessigung und Rektifikation mit Hilfe eines Inertgaskreislaufes
FR2584803B1 (fr) * 1985-07-15 1991-10-18 Air Liquide Procede et installation de distillation d'air
US4869742A (en) * 1988-10-06 1989-09-26 Air Products And Chemicals, Inc. Air separation process with waste recycle for nitrogen and oxygen production
US5165245A (en) * 1991-05-14 1992-11-24 Air Products And Chemicals, Inc. Elevated pressure air separation cycles with liquid production
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
GB9404991D0 (en) * 1994-03-15 1994-04-27 Boc Group Plc Cryogenic air separation

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ATE313772T1 (de) 2006-01-15
DE50108467D1 (de) 2006-01-26
EP1284403A1 (fr) 2003-02-19
DE10139097A1 (de) 2003-02-20

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