EP1284403B1 - Process and apparatus for the production of oxygen by low temperature air separation - Google Patents

Process and apparatus for the production of oxygen by low temperature air separation 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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EP
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Prior art keywords
column
oxygen
stream
air
pressure column
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EP01125721A
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German (de)
French (fr)
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EP1284403A1 (en
Inventor
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)

Abstract

To produce oxygen, by breaking down air under low temperatures, an oxygen column is used in a distillation system. An initial airflow (2) is relaxed (22) to reduce its working power, and passed into the oxygen column (7). A further feed flow (14) is fed into the head of the oxygen column, with an oxygen content at least equal to the feed air. At least one oxygen product flow (16) is taken from the lower section of the column, and a residual gas flow (17) is extracted at the column head and is relaxed (19). The oxygen column can be part of a twin-column system, as a low pressure column, with a high pressure column (6), and a heat exchange link between them through a condenser/evaporator (8).

Description

Die Erfindung betrifft ein Verfahren zur Erzeugung von Sauerstoff durch Tieftemperatur-Zerlegung von Luft in einem Destilliersystem, das eine Sauerstoffsäule aufweist, wobei ein erster Luftstrom arbeitsleistend entspannt und mindestens teilweise in die Sauerstoffsäule eingeleitet wird, ein weiterer Einsatzstrom, dessen Sauerstoffgehalt mindestens gleich demjenigen der Einsatzluft ist, auf den Kopf der Sauerstoffsäule aufgegeben wird, mindestens ein Sauerstoff-Produktstrom aus dem unteren Bereich der Sauerstoffsäule entnommen wird und ein Restgasstrom vom Kopf der Sauerstoffsäule abgezogen wird.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.

Die Grundlagen der Tieftemperaturzerlegung von Luft im Allgemeinen sowie der Aufbau von Einzel- und Doppelsäulen-Anlagen im Speziellen sind in der Monografie "Tieftemperaturtechnik" von Hausen/Linde (2. Auflage, 1985) beschrieben. Ein Verfahren der eingangs genannten Art mit einer als Einzelsäule ausgebildeten Sauerstoffsäule ist aus DE 1229561 B bekannt.The basics of cryogenic decomposition of air in general as well as the Construction of single and double column systems in particular are in the monograph "Cryogenic technology" by Hausen / Linde (2nd edition, 1985) described. One Method of the type mentioned above with a designed as a single column Oxygen column is known from DE 1229561 B.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren und eine Vorrichtung anzugeben, die mit relativ geringem apparativen und/oder energetischem Aufwand eine besonders hohe Flüssigproduktion erlauben, wobei insbesondere die Herstellung entsprechender Mengen flüssigen Sauerstoffs und/oder flüssigen Stickstoffs in dem Destilliersystem möglich sein soll.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.

Diese Aufgabe wird dadurch gelöst, dass der Restgasstrom vom Kopf der Sauerstoffsäule arbeitsleistend entspannt wird. Auf diese Weise kann zusätzlich Kälte für die Produktverflüssigung gewonnen werden, ohne dass hoher Aufwand wie ein zusätzlicher extern angetriebener Verdichter oder gar ein Kreislauf notwendig wären.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.

Damit eine Druckdifferenz für die arbeitsleistende Entspannung des Restgasstroms vorhanden ist, wird die Sauerstoffsäule unter einem überatmosphärischen Druck betrieben. Der Betriebsdruck der Sauerstoffsäule beträgt beispielsweise mindestens 1,7 bar, vorzugsweise 1,7 bis 3,5 bar, höchst, vorzugsweise 2,0 bis 3,0 bar. So that a pressure difference for the working capacity relaxation of the residual gas flow is present, 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.

In einer ersten Variante der Erfindung ist die Sauerstoffsäule als Einzelsäule ausgebildet. Diese wird durch indirekten Wärmeaustausch mit einem Heizmittel aufgekocht. Als Heizmittel wird vorzugsweise ein zweiter Luftstrom eingesetzt. Dieser kann beispielsweise gemeinsam mit dem ersten Luftstrom auf den dafür benötigten Druck verdichtet werden. Der zweite Luftstrom kondensiert bei dem indirekten Wärmeaustausch teilweise oder vollständig und wird anschließend als weiterer Einsatzstrom auf den Kopf der Sauerstoffsäule aufgegeben.In a first variant of the invention, 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.

In einer zweiten Variante der Erfindung weist das Destilliersystem zwei Säulen auf, eine Hochdrucksäule und eine Niederdrucksäule, die über einen Kondensator-Verdampfer in wärmetauschender Verbindung stehen. Die Sauerstoffsäule wird durch die Niederdrucksäule des Zwei-Säulen-Systems gebildet. Ein zweiter Luftstrom wird in die Hochdrucksäule eingeleitet. Hochdrucksäule und Niederdrucksäule können als Doppelsäule mit dazwischen liegendem Hauptkondensator (Kondensator-Verdampfer) ausgebildet sein. Der weitere Einsatzstrom für die Sauerstoffsäule (Niederdrucksäule) wird in diesem Fall vorzugsweise durch eine flüssige sauerstoffangereicherte Fraktion aus dem unteren Bereich der Hochdrucksäule gebildet. Diese weist im Allgemeinen eine Sauerstoffkonzentration von beispielsweise 20 bis 41 mol%, vorzugsweise 21 bis 30 mol% auf.In a second variant of the invention, 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.

In Abweichung von einer klassischen Linde-Doppelsäule wird die sauerstoffangereicherte Fraktion aus der Hochdrucksäule nicht an einer Zwischenstelle eingespeist, sondern am Kopf der Niederdrucksäule aufgegeben. Der Restgasstrom, der am Niederdrucksäulen-Kopf abgenommen wird, ist damit kein reines Stickstoffprodukt, sondern weist einen Sauerstoffgehalt auf, der kleiner ist als 21 mol%, aber mindestens 5 mol%, insbesondere mindestens 10 mol% beträgt. In der Praxis liegt der Sauerstoffgehalt des Restgasstroms beispielsweise bei 14 bis 18 mol%, vorzugsweise bei 15 bis 17 mol%.In deviation from a classic Linde double column is the oxygen-enriched fraction from the high-pressure column not at an intermediate point fed, but abandoned at the top of the low-pressure column. 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%. In practice For example, the oxygen content of the residual gas stream is 14 to 18 mol%, preferably at 15 to 17 mol%.

Es sind zwar Ein- beziehungsweise Zwei-Säulen-Verfahren bekannt (EP 584420 A, EP 518491 A), bei denen sowohl arbeitsleistend entspannte Luft in die Einzelbeziehungsweise Niederdrucksäule eingeblasen, als auch ein stickstoffreicher Strom aus der Einzel- beziehungsweise Niederdrucksäule turbinenentspannt wird. Diese Prozesse unterscheiden sich jedoch grundsätzlich vom Typ der eingangs genannten Art. Während bei der Erfindung Luft oder eine sauerstoffangereicherte Fraktion auf den Kopf der Einzel- beziehungsweise Niederdrucksäule aufgegeben wird, verwenden diese Verfahren stickstoffangereicherte Flüssigkeit als Rücklauf in dieser Säule, die damit eine andere Funktion erfüllt und deutlich komplizierter aufgebaut ist.Although one or two-column process are known (EP 584420 A, EP 518491 A), in which both work-performing relaxed air in the individual relationship Blown low pressure column, as well as a nitrogen-rich stream is relieved of turbines from the single or low pressure column. These However, processes differ fundamentally from the type of the aforementioned Art. While in the invention air or an oxygen-enriched fraction on the Head of the single or low pressure column is used, use these processes provide nitrogen-enriched liquid as the reflux in this column, the so that another function is fulfilled and constructed much more complicated.

Die Kälteleistung bei der arbeitsleistenden Entspannung des ersten Luftstroms kann bei beiden Varianten der Erfindung dadurch erhöht werden, dass der erste Luftstrom stromaufwärts seiner arbeitsleistenden Entspannung nachverdichtet wird. Die Nachverdichtung kann separat oder gemeinsam mit einem oder mehreren anderen Luftströmen erfolgen. Beispielsweise kann die Gesamtluft nachverdichtet werden. Mindestens ein Teil der bei der arbeitsleistenden Entspannung des ersten Luftstroms und/oder des Restgasstroms erzeugten mechanischen Energie kann dabei für die Nachverdichtung eingesetzt werden. Hierfür wird vorzugsweise eine direkte mechanische Kopplung zwischen entsprechender Entspannungsmaschine und entsprechendem Nachverdichter vorgenommen. Falls zwei Nachverdichter vorgesehen sind, können diese parallel oder seriell geschaltet sein. Anstelle der mechanischen Kopplung können eine oder mehrere Generatorturbinen eingesetzt werden.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. For this purpose, preferably a direct mechanical coupling between corresponding expansion machine and made corresponding compressor. If two booster provided can be connected in parallel or in series. Instead of the mechanical one Coupling can be used one or more generator turbines.

Die Erfindung betrifft außerdem eine Vorrichtung zur Tieftemperaturzerlegung von Luft gemäß Patentanspruch 8.The invention also relates to a device for the cryogenic separation of air according to claim 8.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:

Figur 1
ein vereinfachtes Schema eines ersten Ausführungsbeispiels der Erfindung in Form eines Doppelsäulen-Systems,
Figur 2
eine Abwandlung mit einem Turbinen-Booster,
Figur 3
eine weitere Abwandlung mit zwei Turbinen-Boostern,
Figur 4
ein Einzelsäulen-System gemäß der Erfindung und
Figur 5
ein weiteres Ausführungsbeispiel mit Doppelsäule und Innenverdichtung.
The invention and further details of the invention are explained in more detail below with reference to exemplary embodiments illustrated in the drawings. Hereby show:
FIG. 1
a simplified diagram of a first embodiment of the invention in the form of a double-column system,
FIG. 2
a modification with a turbine booster,
FIG. 3
another variation with two turbine boosters,
FIG. 4
a single column system according to the invention and
FIG. 5
another embodiment with double column and internal compression.

Einander entsprechende Verfahrensschritte beziehungsweise Bauteile sind in den Zeichnungen mit denselben Bezugszeichen gekennzeichnet. Corresponding process steps or components are in the Drawings with the same reference numerals.

In der Verfahren von Figur 1 wird über Leitung 1 verdichtete und gereinigte Luft herangeführt. Sie steht unter einem Druck von beispielsweise 10,5 bar und wird in einen ersten Luftstrom 2 und einen zweiten Luftstrom 3 aufgeteilt. Beide werden in einem Hauptwärmetauscher 4 abgekühlt.In the process of FIG. 1 , 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.

Der erste Luftstrom wird dem Hauptwärmetauscher bei einer Zwischentemperatur (zwischen dem warmen und dem kalten Ende) über Leitung 21 entnommen und in einer ersten Entspannungsmaschine 22 arbeitsleistend auf einen Druck von etwa 3 bar entspannt. Der arbeitsleistend entspannte erste Luftstrom wird ganz oder teilweise über Leitung 23 der Niederdrucksäule 7 eines Doppelsäulen-Systems zugeführt, das außerdem eine Hochdrucksäule 6 und einen Hauptkondensator (Kondensator-Verdampfer) 8 aufweist. (Die Niederdrucksäule bildet hier die Sauerstoffsäule im Sinne der Erfindung.) Ein Teil (im Allgemeinen 0 bis 60 %, beispielsweise 50 %) der in 22 entspannten Luft kann über eine Luft-Bypass-Leitung 46 an der Niederdrucksäule 7 vorbeigeführt werden.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.

Bis zum kalten Ende des Hauptwärmetauschers 4 wird der zweite Luftstrom 3 abgekühlt. Von dort aus strömt er über Leitung 9 in die Hochdrucksäule 6.Until the cold end of the main heat exchanger 4, the second air flow is the third cooled. From there it flows via line 9 into the high-pressure column 6.

Der am Kopf der Hochdrucksäule anfallende gasförmige Stickstoff 10 wird im Hauptkondensator 8 kondensiert. Die dabei gebildete Flüssigkeit 11 wird zu einem ersten Teil 12 als Rücklauf auf die Hochdrucksäule aufgegeben und zu einem zweiten Teil 13 als Flüssigprodukt (LIN) gewonnen. Sauerstoffangereicherte Sumpfflüssigkeit 5 der Hochdrucksäule 6 wird im Hauptwärmetauscher 4 unterkühlt und anschließend über Leitung 14 und Drosselventil 15 auf den Kopf der Niederdrucksäule 7 als weiterer Einsatzstrom aufgegeben. (Alternativ zu der in der Zeichnung dargestellten Verfahrensweise kann die Unterkühlung in einem separaten Wärmetauscher vorgenommen werden.)The resulting at the top of the high pressure column gaseous nitrogen 10 is in Main capacitor 8 condenses. The liquid 11 formed thereby becomes a abandoned first part 12 as reflux to the high pressure column and a second Part 13 recovered as a liquid product (LIN). Oxygenated bottoms liquid 5 the high pressure column 6 is supercooled in the main heat exchanger 4 and then via line 14 and throttle valve 15 to the head of the low-pressure column 7 as another Feed stream abandoned. (Alternatively to the one shown in the drawing Procedure, the subcooling in a separate heat exchanger be made.)

Dem Sumpf der Niederdrucksäule 7 wird Sauerstoff 16 - in dem vorliegenden Beispiel ausschließlich in flüssiger Form - als Sauerstoff-Produktstrom 16 entnommen. Vom Kopf der Niederdrucksäule 7 wird ein Restgasstrom 17 mit einem Sauerstoffgehalt von beispielsweise 15 mol% abgezogen und im Hauptwärmetauscher 4 auf eine Zwischentemperatur angewärmt, die etwa gleich der Temperatur des ersten Luftstroms 21 vor seiner arbeitsleistenden Entspannung 22 ist. Das angewärmte Restgas 18 wird in einer zweiten Entspannungsmaschine 19 arbeitsleistend entspannt, über Leitung 20 wieder dem kalten Ende des Hauptwärmetauschers 4 zugeführt und auf etwa Umgebungstemperatur angewärmt. (Die Bypass-Leitung 24 dient zur Regelung der Kälteleistung der Entspannungsmaschine 19.) Das warme Restgas 25 kann als Regeneriergas für eine (nicht dargestellte) Vorrichtung zur Reinigung der Einsatzluft eingesetzt werden.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. from Head of the low pressure column 7 is 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.

Die beiden Entspannungsmaschinen 22, 19 werden vorzugsweise durch Expansions-Turbinen gebildet. Als Bremsvorrichtungen 26, 27 kommen alle bekannten Mittel in Frage; in dem Beispiel der Figur 1 werden dissipative Bremsen oder Generatoren eingesetzt.The two expansion machines 22, 19 are preferably by expansion turbines educated. As braking devices 26, 27 all known means come in Question; In the example of FIG. 1, dissipative brakes or generators are used used.

Davon abweichend wird die erste Entspannungsmaschine 22 in Figur 2 durch einen Nachverdichter (Turbinen-Booster) 227 gebildet. Dieser dient zur Nachverdichtung des ersten Luftstroms 2, 229 auf einen Druck, der höher als der in Leitung 1 herrschende Druck ist. Dazu wird der erste Luftstrom 202 in einem Wärmetauscher 228 angewärmt, im Nachverdichter 227 komprimiert, durch einen Nachkühler 230 geleitet, im Wärmetauscher 228 wieder abgekühlt und über Leitung 231 analog zu Figur 1 dem warmen Ende des Hauptwärmetauschers 4 zugeführt. (Der Wärmetauscher 228 dient zur Optimierung, kann jedoch auch weggelassen werden, um die Apparatekosten zu reduzieren.)Deviating from this, the first expansion machine 22 in FIG. 2 is formed by a booster (turbine booster) 227. 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. For this purpose, 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.)

In Figur 3 ist zwischen den Nachverdichter 227 und den Nachkühler 230 ein weiterer Nachverdichter 332 geschaltet, der von der zweiten Entspannungsmaschine 19 angetrieben wird und eine weitere Druckerhöhung im ersten Luftstrom 231 bewirkt. Auf einen Kühler zwischen den beiden Nachverdichtern wurde in dem Beispiel verzichtet. Alternativ dazu könnte an dieser Stelle ein weiterer Nachkühler (Zwischenkühler) angeordnet sein. Eine weitere mögliche Abwandlung besteht in der Verwendung eines Wärmetauschers, wie er mit dem Bezugszeichen 228 in Figur 2 gezeigt ist. Ebenso könnte der erste Nachverdichter 227 mit der zweiten Entspannungsmaschine 19 gekoppelt sein.In FIG. 3 , 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. On a cooler between the two booster was omitted in the example. Alternatively, at this point, a further aftercooler (intercooler) could be arranged. Another possible modification is the use of a heat exchanger as shown at 228 in FIG. Likewise, the first after-compressor 227 could be coupled to the second expansion machine 19.

Falls kein Stickstoff-Produkt benötigt wird, kann die Hochdrucksäule weggelassen werden, wie es in Figur 4 dargestellt ist. Hier wird das Destilliersystem durch eine als Einzelsäule 407 ausgebildete Sauerstoffsäule mit Sumpfaufkocher 408 gebildet. Der zweite Luftstrom 409 wird unter einem Druck von etwa 10 bar im Verflüssigungsraum des Sumpfaufkochers 408 kondensiert. Die verflüssigte Luft 405 wird - analog zur Sumpfflüssigkeit der Hochdrucksäule in Figur 1- im Hauptwärmetauscher 4 unterkühlt und über 414 und 415 auf den Kopf der Säule 407 aufgegeben, die unter etwa 3 bar betrieben wird. Die übrigen Verfahrensschritte sind dieselben wie in Figur 1. Selbstverständlich können auch die Turbinen-Booster-Schaltungen der Figuren 2 und 3 auf die in Figur 4 gezeigte Säulenkonfiguration angewendet werden.If no nitrogen product is needed, the high pressure column can be omitted, as shown in FIG . Here, 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. Of course, the turbine booster circuits of Figures 2 and 3 can be applied to the column configuration shown in Figure 4.

Figur 5 basiert auf dem Ausführungsbeispiel der Figur 3 und zeigt eine Reihe zusätzlicher Optionen, die - wie dargestellt - gemeinsam oder auch einzeln im Rahmen er Erfindung verwirklicht werden können. 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.

Der Unterkühlungs-Gegenströmer 533, in dem die Sumpfflüssigkeit 5 der Hochdrucksäule 6 gegen Restgas 17 vom Kopf der Niederdrucksäule 7 abgekühlt wird, ist als separater Wärmetauscher ausgebildet und nicht in den Hauptwärmetauscher 504 integriert.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.

Ein Teil des am Kopf der Hochdrucksäule 6 gewonnenen gasförmigen Stickstoffs wird nicht über Leitung 10 zum Hauptkondensator 8 geführt, sondern strömt über Leitung 534 zum Hauptwärmetauscher 504 und wird schließlich als gasförmiges Druckprodukt 547 (PGAN) abgezogen.Part of the gaseous nitrogen recovered at the top of the high-pressure column 6 becomes not led via line 10 to the main capacitor 8, but flows via line 534 to the main heat exchanger 504 and finally as a gaseous pressure product 547 (PGAN).

Flüssiger Stickstoff aus der Hochdrucksäule 6 beziehungsweise dem Hauptkondensator 8 wird nicht nur direkt als Flüssigprodukt 513 gewonnen, sondern auch über Leitung 535 einer Innenverdichtung zugeführt. Dazu wird die Flüssigkeit in einer Pumpe 536 auf den gewünschten hohen Produktdruck gebracht, über Leitung 537 zum Hauptwärmetauscher 504 geführt, dort gegen den zweiten Luftstrom 3 verdampft (oder pseudo-verdampft, falls der Produktdruck überkritisch ist) und schließlich auf Umgebungstemperatur angewärmt. In Leitung 538 steht nun ein Stickstoffprodukt (PGAN-IC) unter besonders hohem Druck zur Verfügung.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. For this, 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. In line 538 is now a Nitrogen product (PGAN-IC) under particularly high pressure available.

Alternativ oder zusätzlich kann ein Sauerstoff-Produktstrom innenverdichtet werden. Hierzu wird über Leitung 539 flüssiger Sauerstoff aus dem unteren Bereich der Niederdrucksäule 7 entnommen (aus dem Sumpf oder - wie dargestellt - von oberhalb des Sumpfs), mittels einer Pumpe 540 auf den gewünschten hohen Produktdruck gebracht, über Leitung 541 zum Hauptwärmetauscher 504 geführt, dort gegen den zweiten Luftstrom 3 verdampft (oder pseudo-verdampft, falls der Produktdruck überkritisch ist) und schließlich auf Umgebungstemperatur angewärmt. In Leitung 542 steht nun ein Sauerstoffprodukt (GOX-IC) unter hohem Druck zur Verfügung.Alternatively or additionally, an oxygen product stream may be internally compressed. For this purpose, via line 539 liquid oxygen from the lower region of Low pressure column 7 taken (from the bottom or - as shown - from above the sump), by means of 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. In line 542 An oxygen product (GOX-IC) is now available under high pressure.

Die unterkühlte sauerstoffangereicherte-Flüssigkeit 14 aus der Hochdrucksäule 6 wird nach ihrer Entspannung zunächst in einen Abscheider (Phasentrenner) 543 eingeleitet. Von dort strömt nur der flüssige Anteil 544 als weiterer Einsatzstrom zum Kopf der Niederdrucksäule 7, während der Dampf 545 direkt in die Restgasleitung 17 eingeführt wird. Die Phasentrennung kann alternativ zu der in der Zeichnung dargestellten Ausführungsform in einem innerhalb der Säule angeordneten Abscheider stattfinden, oder aber in einem einfachen Gerinne, vorzugsweise am Kopf der Niederdrucksäule. Über eine weitere Bypass-Leitung 546 kann ein Teil der in 22 entspannten Luft 23 an der Niederdrucksäule 7 vorbeigeführt werden.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.

Claims (8)

  1. Process for producing oxygen by low-temperature fractionation of air in a distillation system which has an oxygen column, in which process
    a first air stream (2, 21, 229, 231) is expanded (22) in a work-performing manner and is at least in part introduced into the oxidation column (7, 407),
    a further charge stream (5, 14, 405, 414), the oxygen content of which is at least equal to that of the charge air, is added to the top of the oxygen column (7, 407),
    at least one oxygen product stream (16, 539) is removed from the lower region of the oxygen column (7, 407), and
    a residual gas stream (17, 18, 20, 25) is extracted from the top of the oxygen column (7, 407),
    characterized in that the residual gas stream (17, 18, 20, 25) is expanded (19) in a work-performing manner.
  2. Process according to Claim 1, characterized in that the oxygen column is designed as a single column (407) and is boiled by indirect heat exchange (408) with a heating means (409).
  3. Process according to Claim 2, characterized in that a second air stream (409) is used as the heating means.
  4. Process according to Claim 3, characterized in that the second air stream (414), downstream of the indirect heat exchange (408) in order to boil the individual column (407), is used at least in part as a further charge stream for the individual column (407).
  5. Process according to Claim 1, characterized in that the oxygen column is designed as a low-pressure column (7) of a two-column system which also has a high-pressure column (6), the low-pressure column (7) and the high-pressure column (6) being in a heat-exchanging relationship via a condenser-evaporator (8), and a second air stream (3, 9) being introduced into the high-pressure column (6).
  6. Process according to Claim 5, characterized in that a liquid oxygen-enriched fraction (5) is extracted from the lower region of the high-pressure column (6) and is used as a further charge stream (14) for the low-pressure column (7).
  7. Process according to one of Claims 1 to 6, characterized in that the first air stream (202) is recompressed (227, 332) upstream of its work-performing expansion (22), at least some of the mechanical energy which is generated during the work-performing expansion (22, 19) of the first air stream (231) and/or of the residual gas stream (18) being used for the recompression.
  8. Apparatus for producing oxygen by low-temperature fractionation of air using a distillation system which has an oxygen column,
    having a first air line (2, 21, 23, 229, 231), which leads through a first expansion machine (22) into the oxygen column (7, 407),
    having a further charge line (5, 14, 405, 414) for introducing a further charge stream, the oxygen content of which is at least equal to that of the charge air, into the top of the oxygen column (7, 407),
    having an oxygen product line (16, 539), which is connected to the lower region of the oxygen column (7, 407), and
    having a residual gas line (17, 18, 20, 25), which is connected to the top of the oxygen column (7, 407),
    characterized by a second expansion machine (19), which is arranged in the residual gas line (17, 18, 20, 25).
EP01125721A 2001-08-09 2001-10-27 Process and apparatus for the production of oxygen by low temperature air separation Expired - Lifetime EP1284403B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10139097A DE10139097A1 (en) 2001-08-09 2001-08-09 Method and device for producing oxygen by low-temperature separation of air
DE10139097 2001-08-09

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

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DE102006012241A1 (en) * 2006-03-15 2007-09-20 Linde Ag Method and apparatus for the cryogenic separation of air
EP2520886A1 (en) * 2011-05-05 2012-11-07 Linde AG Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air
WO2014154339A2 (en) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Method for air separation and air separation plant

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1229561B (en) * 1962-12-21 1966-12-01 Linde Ag Method and device for separating air by liquefaction and rectification with the aid of an inert gas cycle
FR2584803B1 (en) * 1985-07-15 1991-10-18 Air Liquide AIR DISTILLATION PROCESS AND INSTALLATION
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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EP1284403A1 (en) 2003-02-19
DE10139097A1 (en) 2003-02-20
ATE313772T1 (en) 2006-01-15
DE50108467D1 (en) 2006-01-26

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