EP2603754A2 - Method and device for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air - Google Patents

Method and device for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air

Info

Publication number
EP2603754A2
EP2603754A2 EP11743030.6A EP11743030A EP2603754A2 EP 2603754 A2 EP2603754 A2 EP 2603754A2 EP 11743030 A EP11743030 A EP 11743030A EP 2603754 A2 EP2603754 A2 EP 2603754A2
Authority
EP
European Patent Office
Prior art keywords
pressure
nitrogen
pressure column
stream
oxygen
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP11743030.6A
Other languages
German (de)
French (fr)
Other versions
EP2603754B1 (en
Inventor
Dirk Schwenk
Alexander Alekseev
Frances Masterson
Dimitri Goloubev
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to PL11743030T priority Critical patent/PL2603754T3/en
Priority to EP11743030.6A priority patent/EP2603754B1/en
Publication of EP2603754A2 publication Critical patent/EP2603754A2/en
Application granted granted Critical
Publication of EP2603754B1 publication Critical patent/EP2603754B1/en
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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    • 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
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
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    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
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    • 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
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    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
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    • F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/44—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being nitrogen

Definitions

  • the invention relates to a process for the production of pressure oxygen and
  • the distillation column system for nitrogen-oxygen separation can be formed in the invention as a two-column system (for example, as a classic Linde double column system), or as a three- or multi-column system.
  • other devices may be provided for recovering high purity products and / or other air components, particularly noble gases, for example, argon recovery and / or krypton-xenon recovery.
  • High-pressure column is meant here a column which under
  • the "low-pressure column” has a lower operating pressure and communicates with the high-pressure column via a common condenser-evaporator
  • the "main heat exchanger” is used for cooling of feed air and can by a single heat exchanger block or by a plurality of
  • Heat exchanger blocks are formed.
  • the invention relates to a process for the production of gaseous
  • High-pressure process stream evaporates (or - at
  • Nitrogen or feed air can be used as the high-pressure process stream.
  • the product pressure of the internal compression is for example 6 to 100 bar, preferably 30 to 95 bar.
  • the upper cycle pressure of the nitrogen cycle is, for example, between 20 and 90 bar, preferably between 20 and 75 bar.
  • JP 1 1 1 18352 A A method of the type mentioned is known from JP 1 1 1 18352 A.
  • the invention has for its object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable and in particular have a particularly low energy consumption with reasonable expenditure on equipment.
  • the cycle compressor is designed as a warm compressor, that is, it is operated at an inlet temperature which is above 250 K, in particular above 270 K. In addition, it is powered by external energy, for example, with an electric motor or a steam turbine, at least not with a turbine that relaxes a process stream of air separation. Contrary to the basic idea of JP 1 1 18352 ⁇ the cycle compressor is not operated as a cold compressor and not driven by a turbine in which the circulation nitrogen flow is relaxed.
  • the circulation embroidery stream can be set independently of the refrigeration requirement of the plant.
  • the heating power in the bottom evaporator of High pressure column can be freely selected.
  • the process can be adapted much more flexibly to current needs and thus operated energetically cheaper.
  • the high-pressure column with a
  • Operating pressure for example, 5 to 6.5 bar, preferably operated 5.2 to 6.2 bar.
  • Operating pressure for example, 5 to 6.5 bar, preferably operated 5.2 to 6.2 bar.
  • Nitrogen-oxygen separation to the cycle compressor is preferably withdrawn from the top of the high-pressure column.
  • the product pressure of the pressurized nitrogen product may be equal to, lower, or higher than the pressure at which the first substream is withdrawn from the cycle compressor, for example, at the level of the operating pressure of the high pressure column or higher.
  • the pressurized nitrogen product may be discharged in a plurality of sub-streams at different pressures; In this case, the entirety of the pressurized nitrogen product is referred to herein as a "second partial stream".
  • Section of the low pressure column ascending steam can be adjusted by adjusting the amount of the second partial flow of the cycle nitrogen flow and the amount of reflux liquid in the upper part of the low pressure column indirectly via the adjustment of the amount of the first partial flow of the circulating nitrogen stream, so the heating power of the high-pressure column sump evaporator. This can do that
  • Return ratio can be optimized both in the upper and in the lower part of the low pressure column. If the amount of the first partial flow of the cycle stream is increased or decreased and thereby more or less nitrogen condenses in the bottom evaporator, a correspondingly altered amount of liquid nitrogen is available as reflux liquid in the high-pressure column and it can be more or less high-pressure nitrogen removed; It does not matter if a part of the liquid nitrogen from the bottom evaporator is introduced directly into the low pressure column, or whether it is introduced into the high pressure column and thus correspondingly more (or less) liquid nitrogen from the high pressure column or from the main condenser can be transferred to the low pressure column. If less or more high-pressure column nitrogen is withdrawn as a "second partial flow" and thus more or less heating power is available at the main condenser, correspondingly more or less rising steam is generated for the lower part of the low-pressure column.
  • the method is particularly suitable for the extraction of impure
  • Pressure oxygen with a purity of less than 98 mol%, preferably of 97% or less. It can be used particularly advantageously in IGCC plants in which at least a portion of the pressure oxygen product in a coal gasification for
  • Pressure nitrogen product is used for coal transport.
  • Total nitrogen pressure product quantity is formed by the sum of the flow rates, the upstream and / or downstream of the cycle compressor and / or of an intermediate stage of the cycle compressor under a product pressure from the
  • the method is run with variable load, wherein
  • the feed air is introduced into the air compressor in a first quantity of feed air EL1,
  • the feed air is introduced in a second amount of feed air EL2 in the air compressor, wherein the second feed air quantity EL2 is equal to the first feed air quantity EL1 or only slightly higher, where applicable
  • Amount of air used is equal or is only slightly increased.
  • “insubstantial” means that the relative change in the amount of air is at most one-fifth, preferably less than one-tenth of the relative change in the amount of pressurized nitrogen product.
  • the second feed air quantity EL2 is increased by less than 10%, preferably remaining the same.
  • Recirculation compressor taken as the only pressure nitrogen product.
  • Load increase from a first to a second load case is the
  • Feed air quantity remains unchanged.
  • the change of the first partial flow is linearly related to the pressure nitrogen product change.
  • the amount of UN2 is reduced by 10,000 Nm 3 / h.
  • the load on the main condenser is therefore directly proportional to the pressure nitrogen removal. If, for example, 10,000 Nn more Vh are removed, 10,000 Nm / h less nitrogen is liquefied at the main condenser.
  • the regulation of the first partial flow can be carried out by means of an AIC controller (for example, keeping the oxygen product purity constant).
  • a third partial stream of the nitrogen cycle stream is taken as a turbine stream from the cycle compressor, work expanded and at least partially introduced into the distillation column system for nitrogen-oxygen separation. The at the work performing relaxation of the
  • Turbine power generated energy is preferably mechanically to a
  • Post-compressor in which, for example, the turbine stream upstream of the work-performing expansion and / or the first part of the flow
  • Circulating nitrogen flow upstream of its introduction into the main heat exchanger are recompressed.
  • process cooling can be obtained by work-performing expansion of a partial flow of the feed air.
  • the mechanical energy obtained is preferably transferred to a compressor for the turbine air.
  • Condenser-evaporator introduced and there in indirect heat exchange with At least a portion of the work performed relaxing turbine stream is at least partially evaporated, wherein the steam generated thereby is at least partially returned to the high-pressure column.
  • the boil up of the high pressure column improves their release effect.
  • a heating means in the invention is not used to be specially compressed stream, but the already existing at a suitable pressure level turbine flow. The cycle compressor is thus used for a further purpose, the heating of the high-pressure column.
  • the "condenser-evaporator” in which a liquid fraction is boiled from the high-pressure column is designed as a heat exchanger separate from the main heat exchanger, in particular as at least one plate heat exchanger block, most preferably as a single plate heat exchanger block; it may be located within the high pressure column or outside in a separate container.
  • the liquid fraction to the condenser-evaporator can from the bottom of the
  • High-pressure column are removed - the condenser-evaporator then represents the bottom evaporator and is preferably arranged directly in the bottom of the high-pressure column.
  • the condenser-evaporator is designed as an intermediate evaporator of the high-pressure column and arranged for example at an intermediate level in the interior of the high-pressure column; the liquid fraction for the condenser-evaporator is then withdrawn at the corresponding intermediate point of the high-pressure column.
  • the bottom and the intermediate evaporator are heated by different partial streams of the circulating nitrogen stream, which are removed at different suitable pressures from the cycle compressor.
  • the pressure of the first partial flow of the cycle nitrogen flow is the highest pressure required in the process.
  • the third partial flow of the circulating nitrogen stream (turbine stream) can also be withdrawn from the cycle compressor at this pressure level.
  • the inlet pressure of the work-performing expansion is then approximately at the level of the upper intermediate pressure, but may optionally by a coupled to the expansion machine
  • the first partial flow of the circulating nitrogen stream can be withdrawn from the cycle compressor at a high pressure (P4) which is higher than the intermediate pressure (P3) at which the third partial flow of the circulating nitrogen stream flows out of the circuit.
  • Circulation compressor is removed; Subsequently, the first partial flow is under this high pressure or under an even higher pressure in the
  • Circulation nitrogen flow can be obtained under the high pressure as a pressure nitrogen product, without additional machinery costs would be necessary.
  • a fourth substream of the loop nitrogen stream is subjected to a lower intermediate pressure (P2) from an intermediate stage of the
  • Turbine stream mixed upstream of the condenser-evaporator This is particularly favorable when the turbine stream for heating the
  • High-pressure column is used in the first condenser-evaporator. If relatively little cooling is needed, the turbine flow can be so small that it alone can no longer apply the heat needed for the column heating. By adding the fourth partial flow, additional heat can be introduced into the condenser-evaporator. Refrigeration and column operation are thus independent. The cooling capacity provided by the turbine flow can be widely varied without affecting the operation of the distillation column system.
  • part of the work can be done
  • the liquid oxygen stream for internal compression is preferably taken from the lower region of the low-pressure column
  • an intermediate liquid whose oxygen content is between that of the oxygen-enriched liquid and that of the nitrogen-enriched liquid can be taken out of the high-pressure column and fed to the low-pressure column at a second intermediate point located above the first intermediate point, the intermediate liquid being in particular at a height
  • the invention also relates to an apparatus for recovering pressure oxygen and pressurized nitrogen by cryogenic separation of air in accordance with
  • Figure 1 shows a first embodiment of the invention with two
  • FIG. 2 shows a modification of the first exemplary embodiment, in which the work-performing expansion leads to the inlet pressure of the second stage of the cycle compressor
  • FIG. 3 shows an exemplary embodiment with only one condenser-evaporator in the high-pressure column and re-compression of the turbine flow
  • Figure 4 shows a modification of this variant with recompression of the first
  • Figures 5 to 7 further embodiments with two condenser-evaporators in the high-pressure column and Figures 8 and 9 show two embodiments with only one condenser evaporator in the high pressure column and with an air turbine.
  • Main heat exchanger 20 is cooled to about dew point and fed via line 7 to a distillation column system for nitrogen-oxygen separation, which consists in the example of a high-pressure column 8 and its associated column evaporators, a bottom evaporator 9 and an intermediate evaporator 10, and a low-pressure column 460th and a main condenser 461 through which the high-pressure column 8 and the low-pressure column 460 are in heat-exchanging connection by bringing the top gas of the high-pressure column into indirect heat exchange with the bottom liquid.
  • the operating pressure at the top of the low-pressure column 460 is approximately 1.4 bar.
  • the main heat exchanger 20 can be implemented integrated or split, Figure 1 and the following drawings show only the
  • the bottom liquid 462 ("oxygen-enriched liquid") from the
  • Bottom evaporator 9 is passed completely through a first subcooling countercurrent 16 and a second subcooling countercurrent 415, expanded in a throttle valve 463 to low pressure column pressure and fed via line 464 of the low pressure column at a first intermediate point.
  • a portion 465 of the intermediate liquid of the high-pressure column 8, which is obtained at the liquefaction side of the intermediate evaporator 10 is withdrawn from there, also supercooled in the subcooling countercurrents 16 and 416 and fed after throttling 466 via line 467 at a second intermediate point of the high pressure column 8, the is above the first intermediate point.
  • a third feed stream in the form of impure liquid nitrogen 468 is after
  • Low pressure column 460 abandoned.
  • the liquid oxygen is taken here from the bottom of the low-pressure column 460 or from the liquefaction side of the main condenser 461 and analogously to stream 1 1 of Figure 1 in a mecanicverdichtungsstrom ("liquid oxygen stream") 412 and a liquid product (415/417) split.
  • liquid oxygen 1 1 is generated, the first part as a "liquid oxygen stream" 12 in a pump 13 of - depending on
  • Liquid (IC-LOX) is introduced into the main heat exchanger 20 at this elevated pressure, vaporized or pseudo-evaporated in the main heat exchanger and warmed to about ambient temperature. Finally, the oxygen is recovered as gaseous pressure oxygen product 14.
  • Another part 15 of the bottom liquid 1 1 of the low-pressure column 460 is - optionally after subcooling in the supercooling countercurrent 416 discharged via line 17 as a liquid oxygen product (LOX).
  • LOX liquid oxygen product
  • nitrogen is withdrawn via line 18 as a "gaseous circulating nitrogen stream", heated in the supercooling countercurrent 16 and further (line 19) in the main heat exchanger 20 and finally at least to a first part via line 21 of the first stage 23 of a cycle compressor 22 fed, which has four stages 23, 25, 560 with aftercoolers 24, 16, 561 in the example.
  • the two last compressor stages 560 and aftercooler 561 are shown in simplified form and can also be regarded as an additional product compressor for the then two-stage cycle compressor 23/25) and is driven by means of an electric motor; as an alternative to 23/25 you can
  • Circular compressors in the strict sense with three or more than four stages are used.
  • Another part of the circulating nitrogen stream can be obtained as compressed nitrogen product 27 (PGAN) below about the operating pressure of the high pressure column.
  • GPN compressed nitrogen product 27
  • the cycle nitrogen flow is compressed to a first intermediate pressure (P1-GAN) of approximately 9 bar and in the second stage 25 further to a second intermediate pressure (P2-GAN) of approximately 12 bar.
  • the last two stages 560 compress to a high pressure which is 1.4 to 2.5 times the oxygen pressure (P4-GAN), or a third one Intermediate pressure (P3-GAN).
  • P4-GAN oxygen pressure
  • P3-GAN third one Intermediate pressure
  • Turbine stream 40 is cooled in the main heat exchanger to an intermediate temperature and finally expanded in a relaxation machine 41, which is preferably formed by an expansion turbine, performing work.
  • the work performed relaxing turbine stream 42 is at least a first part 30 in the
  • one of the pressures P2-GAN to P4-GAN for the flow 540 is selected for a specific system and corresponding piping is realized.
  • the mechanical power produced in the expansion turbine 41 is transmitted to the booster 566 by mechanical coupling.
  • the turbine 41 may be coupled to another compressor, a generator or to a dissipative braking device.
  • liquid nitrogen 43 can be withdrawn as a further product stream (PLIN)
  • At least part of the circulating nitrogen flow which is at the final pressure of the
  • Circular compressor 22 is compressed, forms a "high-pressure process stream", which provides the heat in the main heat exchanger 20 for the (pseudo) evaporation of the liquid pressure oxygen.
  • the cold high pressure process stream 35 is in the
  • Subcooling countercurrent 16 cooled (not shown in Figure 1), expanded in a throttle valve 36 to high pressure column pressure and finally fed via line 37 to the top of the high pressure column 8.
  • High-pressure column pressure can alternatively work to perform in a liquid turbine 38th be performed;
  • the liquid turbine 38 is braked by a generator 39.
  • impure nitrogen 50 is withdrawn as residual gas, warmed in the subcooling countercurrents 416 and 16 and further (line 51, P-UN2) in the main heat exchanger 20 and finally discharged via line 52 as a residual product; it can still be used in the process as a regeneration gas or as a dry gas in an evaporative cooler.
  • Circular compressor 22 forms a "first partial flow of the circulating nitrogen stream" and is - after cooling in the main heat exchanger 20 - at least partially liquefied as intermediate pressure circulating nitrogen 46 in the bottom evaporator 9 of the high pressure column. Subsequently, the intermediate pressure circulation nitrogen flow via line 47, the subcooling countercurrent 16, and the throttle valve 48 is placed on the head of the high pressure column 8.
  • a conduit 44 leading through a passage group of the main heat exchanger 20 ("intermediate passage") is operated as a shuttle in the embodiment.
  • a fourth substream of the circulating nitrogen stream is withdrawn below the lower intermediate pressure (P1-GAN) from the first intermediate stage of the cycle compressor 22, in the intermediate pressure passage of the cycle
  • part of the work can be done
  • Circulation compressor 22 upstream of the second stage 25 are fed again. This is especially advantageous when a lot of cold is generated and the turbine flow is thus too large for the heating of the first condenser-evaporator.
  • the method of Figure 2 differs from that of Figure 1 that the work-performing expansion 41 has a higher outlet pressure.
  • Bottom evaporator 209 of the high-pressure column 8 to operate with the current 230.
  • the "first partial flow” for heating the bottom evaporator 209 is therefore partially identical to the turbine flow, the "third partial flow”.
  • the shuttle line 244 is also at the higher pressure level (P2-GAN).
  • a heating means for the intermediate evaporator 210 a partial stream 246 of the circulating nitrogen stream is used, which is branched off upstream of the second stage 25 of the cycle compressor 22.
  • the cycle compressor 322 can also have one stage less than in FIG.
  • FIG. 4 shows a modification of FIG. 3.
  • the turbine stream (“third partial stream”) 440 is not sent through the secondary compressor coupled to the turbine 41, but instead the "high-pressure process stream” 434, which subsequently flows into the
  • Main heat exchanger 20 for (pseudo) evaporation of the oxygen product is used. Both the first and the third partial flow come here from the outlet of the final stage of the cycle compressor 322 (pressure level P4-GAN).
  • FIGS. 1 to 3 instead of the turbine / compressor combination 41/566, a generator turbine can also be used.
  • the cycle compressor 322 is formed as in Figures 3 and 4, wherein it may have only two stages 23, 25. Otherwise, the method illustrated here more closely resembles that of FIG. 1; in particular, the high-pressure column 8 has an intermediate evaporator 10.
  • the circulating nitrogen stream is compressed to an intermediate pressure of about 9 bar and in the second stage 25 further to an upper circuit pressure of up to 16 bar.
  • Nitrogen under the upper circuit pressure is not withdrawn via line 29 as pressure nitrogen product, he serves here exclusively as a "first partial flow" for heating the bottom evaporator.
  • the refrigeration needed for the process is generated by work-in-progress expansion 541 of turbine flow 540, which in the example is nitrogen, which comes from a nitrogen compressor (for example, a separate compressor, not shown, or from an additional stage at
  • Work-performing expansion 541 is mixed with one of the nitrogen streams at one of the pressure levels PGAN, P1 GAN or P2GAN.
  • the mechanical power Pturb generated in the expansion turbine 41 is released into heat, in particular to a compressor, a generator or a dissipative brake.
  • a nitrogen flow 534 is used, which is under a suitable pressure and comes from a nitrogen compressor (for example, a separate, not shown
  • the nitrogen stream 34 can also originate from any other compressed nitrogen source, that is, the pressure levels PGAN, P1-GAN or P2-GAN. It may be depressurized to any suitable existing pressure level PGAN or P1 -GAN and then added to the appropriate cycle or pressurized product stream. Alternatively, the work-performing relaxation leads to atmospheric level and the relaxed turbine stream is finally released - after heating in the main heat exchanger 20 - without pressure.
  • the cold high pressure process stream 535 is performed as in FIG.
  • the method of Figure 6 differs from that of Figure 1 in that the outlet pressure of the work-performing expansion 641 (line 642) on the Level PGAN the operating pressure of the high-pressure column 8 is located. As a result, correspondingly more cold can be obtained for product liquefaction.
  • the turbine stream 540 is formed by at least a portion of one of the following three streams:
  • the turbine flow is expanded to approximately the operating pressure of the pressure column 8 in order to work.
  • the relaxed turbine stream 642 eventually becomes the
  • Circulating nitrogen stream 19 added, which comes from the head of the pressure column 8.
  • the turbine power is delivered here to a nitrogen booster 666, which further increases the pressure of the turbine flow.
  • the high pressure process stream 734 is not formed by nitrogen and by a substream of the feed air. This can, for example, branched off downstream of a cleaning device, not shown, and brought to the required pressure in a booster, which can be up to 90 bar. (Main air compressor, cleaning device,
  • Branch and re-compressors are not shown in FIG. 7.
  • the high-pressure process stream 734 in the main heat exchanger is cooled and (pseudo-) liquefied, expanded in the throttle valve 736 to high-pressure column pressure and finally via line 737 to a suitable intermediate point in the high-pressure column 8 fed.
  • the expansion to the pressure column pressure can also be carried out in a work-performing manner in a liquid turbine 738, which is preferably braked by a generator 739.
  • the use of air as a high-pressure process stream shown in FIG. 7 can also be applied to the process variants of FIGS. 1 to 6.
  • the turbine stream 840 for the work-performing expansion 841 is formed in FIG. 7 not by nitrogen but by another part of the feed air, here in particular the remainder of the feed air which is not used as the high-pressure process stream 734.
  • the total air in the air compressor to a significantly above High-pressure column pressure of up to 90 bar compressed and then divided into the turbine stream 840 and the high-pressure process stream 734.
  • the expanded turbine stream is introduced at a suitable intermediate point in the high-pressure column 8.
  • the second modification shown in FIG. 7 can also be used in the methods of FIGS. 1 to 6), alone or in combination with the use of air as a high-pressure process stream.
  • the method of Figure 8 also uses feed air as high pressure process stream 734 and turbine stream 840.
  • the total air is compressed in a main air compressor to about high pressure column pressure and then cleaned in a purifier (both not shown in the drawing).
  • the compressed at high pressure column pressure and purified air 801 is divided into a total of three sub-streams, the high-pressure process stream 734, the turbine stream 840 and also in a
  • the high-pressure process stream and the turbine stream are fed together via line 802 to a first externally driven booster 803 with aftercooler 804 and then further branched. While the high-pressure process stream is further compressed to a particularly high pressure in a further externally driven booster 808 with aftercooler 809, the turbine stream flows through a booster 810 which is driven by the expansion machine 841, which is formed by a turboexpander and mechanically via a common shaft is coupled to the booster 810.
  • the after-compressor 810 also has an after-cooler 81 1.
  • Part 865 of the liquid introduced via line 737 into the high-pressure column 8 is immediately taken out of the high-pressure column and, analogously to stream 465 in FIG. 1, fed to the low-pressure column 460 at an intermediate point.
  • the "first partial stream" of the circulating nitrogen stream is formed here by the stream 845/846, which is taken off between the two stages 23, 25 of the cycle compressor 22 and led to the bottom evaporator 9 of the high-pressure column 8.
  • the low-pressure column 460 is connected to a conventional argon recovery. The details of argon recovery with crude argon column are not shown here, which they are familiar to the expert.
  • an additional pressurized nitrogen product stream 853 is recovered by internal compression by liquidly pressurizing a portion 850 of the liquid nitrogen recovered in the main condenser 461 to a high pressure in a pump 851, passing it to the main heat exchanger 20 via line 852 and evaporating or pseudo-evaporating and warming to ambient temperature becomes.
  • Figure 9 corresponds largely to Figure 8, but has no nitrogen internal compression.
  • the subcooling countercurrents not shown in Figure 8 are shown.
  • the method differs by an additional medium-pressure column 900, which is operated under an operating pressure which is between the operating pressures of low-pressure column 760 and high-pressure column 8.
  • the bottom liquid 462 is operated under an operating pressure which is between the operating pressures of low-pressure column 760 and high-pressure column 8.
  • oxygen-enriched liquid from the high-pressure column 8 and from the liquefaction side of their bottom evaporator 9 is here not directly, but indirectly fed to the low-pressure column 460.
  • supercooling 16 it is first preceded by line 964 of the medium-pressure column 900 and further there.
  • the liquid air 865 is not supplied to the low-pressure column 460 here in contrast to the previous embodiments, but after flowing through the supercooling countercurrent 16 and a throttle valve via line 965 of the medium-pressure column 900 fed to an intermediate point. (A portion may be withdrawn via line 965 and fed into low pressure column 460 as shown in Figure 1 via 466 and 467.)
  • the medium-pressure column 900 has two condenser evaporators, a
  • the medium-pressure column bottom evaporator 901 is heated by means of a partial flow 903 of the top nitrogen of the high-pressure column 8.
  • the thereby condensed nitrogen 904 is charged as reflux liquid to the head of the medium-pressure column 900.
  • the medium-pressure column head condenser 902 is connected to the bottom liquid 905 of the medium-pressure column 900 or from the liquefaction side thereof Bottom evaporator 901 cooled.
  • the generated vapor 906 and the liquid remaining portion 907 are introduced into the low-pressure column 460.
  • the portion 908 of the liquid nitrogen recovered in the medium-pressure column overhead condenser 902, which is not introduced into the medium-pressure column 900 as reflux liquid, can be used after subcooling 16 as additional reflux liquid 909 for the low-pressure column 460.

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Abstract

The invention relates to a method and devoice for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air in a distillation column system for nitrogen-oxygen separation, said distillation column system having at least one high-pressure column (8) and one low-pressure column (460), wherein the low-pressure column (460) is in a heat-exchanging connection with the high-pressure column (8) by means of a main condenser (461) designed as a condenser-evaporator. Feed air is compressed in an air compressor (2). The compressed feed air (6, 734, 802, 840) is cooled down in a main heat exchanger (20) and at least partially introduced into the high-pressure column (8). An oxygen-enriched liquid (462, 465) is removed from the high-pressure column (8) and fed to the low-pressure column (460) at a first intermediate position (464, 467, 906). A nitrogen-enriched liquid (468, 470) is removed from the high-pressure column (8) and/or the main condenser (461) and fed to the head of the low-pressure column (460). A liquid oxygen flow (11, 12) is removed from the distillation column system for nitrogen-oxygen separation, brought to an elevated pressure in the liquid state (13), introduced into the main heat exchanger (20) at said elevated pressure, evaporated or pseudo-evaporated and heated to approximately ambient temperature in the main heat exchanger (20), and finally obtained as a gaseous compressed oxygen product (14). A high-pressure process flow (34, 734) is brought into indirect heat exchange with the oxygen flow in the main heat exchanger (20) and then depressurized (36, 38; 736, 738), wherein the depressurized high-pressure flow (37, 737) is introduced at least partially in the liquid state into the distillation column system for nitrogen-oxygen separation. A gaseous circuit nitrogen flow (18, 19) is drawn from the high-pressure column and at least partially (21) compressed in a circuit compressor (22). A first sub-flow (45, 46; 244, 242, 230; 845, 846) of the circuit nitrogen flow is removed from the circuit compressor (22, 322), cooled down in the main heat exchanger (20), at least partially condensed in the bottom evaporator (9, 209) of the high-pressure column (8) in indirect heat exchange with the bottom liquid of the high-pressure column (8), and conducted back into the distillation column system for nitrogen-oxygen separation. A second sub-flow of the circuit nitrogen flow is branched off upstream and/or downstream of the circuit compressor and/or from an intermediate stage of the circuit compressor at a product pressure (P, P1, P2, P3, P4) and obtained as a compressed nitrogen product (27, 29, 53, 564, 565). The circuit compressor (22, 322) is designed as a hot compressor and is driven by means of external energy.

Description

Beschreibung  description
Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Tieftemperaturzerlegung von Luft Process and apparatus for recovering pressure oxygen and pressurized nitrogen by cryogenic separation of air
Die Erfindung betrifft ein Verfahren zur Gewinnung von Drucksauerstoff und The invention relates to a process for the production of pressure oxygen and
Druckstickstoff durch Tieftemperaturzerlegung von Luft gemäß dem Oberbegriff des Patentanspruchs 1. Pressure nitrogen by cryogenic separation of air according to the preamble of patent claim 1.
Das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung kann bei der Erfindung als Zwei-Säulen-System (zum Beispiel als klassisches Linde-Doppelsäulensystem), oder auch als Drei- oder Mehr-Säulen-System ausgebildet. Zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung können weitere Vorrichtungen zur Gewinnung hochreiner Produkte und/oder anderer Luftkomponenten, insbesondere von Edelgasen vorgesehen sein, beispielsweise eine Argongewinnung und/oder eine Krypton-Xenon- Gewinnung. The distillation column system for nitrogen-oxygen separation can be formed in the invention as a two-column system (for example, as a classic Linde double column system), or as a three- or multi-column system. In addition to the nitrogen-oxygen separation columns, other devices may be provided for recovering high purity products and / or other air components, particularly noble gases, for example, argon recovery and / or krypton-xenon recovery.
Die Grundlagen der Tieftemperaturzerlegung von Luft im Allgemeinen sowie der Aufbau von Doppelsäulenanlagen im Speziellen sind in der Monografie "Tieftemperaturtechnik" von Hausen/Linde (2. Auflage, 1985) und in einem Aufsatz von Latimer in Chemical Engineering Progress (Vol. 63, No.2, 1967, Seite 35) beschrieben. Die Wärmeaustauschbeziehung zwischen Hochdrucksäule und Niederdrucksäule einer Doppelsäule wird im Regelfall durch einen Hauptkondensator realisiert, in dem The basics of cryogenic separation of air in general and the construction of double column systems in particular are described in the monograph "Cryogenic Technology" by Hausen / Linde (2nd edition, 1985) and in an article by Latimer in Chemical Engineering Progress (Vol. 2, 1967, page 35). The heat exchange relationship between high-pressure column and low-pressure column of a double column is usually realized by a main capacitor, in which
Kopfgas der Hochdrucksäule gegen verdampfende Sumpfflüssigkeit der Top gas of the high pressure column against vaporizing bottoms liquid the
Niederdrucksäule verflüssigt wird. Unter "Hochdrucksäule" wird hier eine Säule verstanden, die unter Low pressure column is liquefied. By "high-pressure column" is meant here a column which under
überatmosphärischem Betriebsdruck von mindestens 4 bar, in der Regel etwa zwischen 4 und 6 bar betrieben wird, manchmal auch unter weiter erhöhtem Druck. Die "Niederdrucksäule" weist einen niedrigeren Betriebsdruck auf und steht mit der Hochdrucksäule über einen gemeinsamen Kondensator-Verdampfer in superatmospheric operating pressure of at least 4 bar, usually between about 4 and 6 bar is operated, sometimes under further elevated pressure. The "low-pressure column" has a lower operating pressure and communicates with the high-pressure column via a common condenser-evaporator
wärmetauschender Verbindung. Der "Hauptwärmetauscher" dient zur Abkühlung von Einsatzluft und kann durch einen einzelnen Wärmetauscherblock oder auch durch eine Mehrzahl von heat exchanging connection. The "main heat exchanger" is used for cooling of feed air and can by a single heat exchanger block or by a plurality of
Wärmetauscherblöcken gebildet sein. Die Erfindung bezieht sich auf ein Verfahren zur Erzeugung von gasförmigem Heat exchanger blocks are formed. The invention relates to a process for the production of gaseous
Drucksauerstoff, bei dem die Druckerhöhung im Flüssigprodukt vorgenommen und die Hochdruckflüssigkeit anschließend in indirektem Wärmeaustausch mit einem  Pressure oxygen, in which the pressure increase made in the liquid product and the high-pressure liquid then in indirect heat exchange with a
Hochdruck-Prozessstrom (Wärmeträger) verdampft (beziehungsweise - bei High-pressure process stream (heat transfer medium) evaporates (or - at
überkritischem Druck - pseudo-verdampft) wird. Dieser Verfahrenstyp wird häufig als "Innenverdichtung" bezeichnet und ist beispielsweise in Hausen/Linde, supercritical pressure - pseudo-evaporated). This type of process is often referred to as "internal compaction" and is for example in Hausen / Linde,
Tieftemperaturtechnik, 2. Auflage 1985, S. 319-322 beschrieben. Als Hochdruck- Prozessstrom kann Stickstoff oder Einsatzluft eingesetzt werden. Der Produktdruck der Innenverdichtung beträgt beispielsweise 6 bis 100 bar, vorzugsweise 30 bis 95 bar. Der obere Kreislaufdruck des Stickstoffkreislaufs liegt beispielsweise zwischen 20 und 90 bar, vorzugsweise zwischen 20 und 75 bar.  Cryogenics, 2nd edition 1985, pp. 319-322. Nitrogen or feed air can be used as the high-pressure process stream. The product pressure of the internal compression is for example 6 to 100 bar, preferably 30 to 95 bar. The upper cycle pressure of the nitrogen cycle is, for example, between 20 and 90 bar, preferably between 20 and 75 bar.
Ein Verfahren der eingangs genannten Art ist aus JP 1 1 1 18352 A bekannt. A method of the type mentioned is known from JP 1 1 1 18352 A.
Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die wirtschaftlich besonders günstig sind und insbesondere einen besonders niedrigen Energieverbrauch bei vertretbarem apparativen Aufwand aufweisen. The invention has for its object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable and in particular have a particularly low energy consumption with reasonable expenditure on equipment.
Diese Aufgabe wird durch die kennzeichnenden Merkmale des Patentanspruchs 1 gelöst. Der Kreislaufverdichter ist als warmer Verdichter ausgebildet, das heißt er wird mit einer Eintrittstemperatur betrieben, die oberhalb von 250 K, insbesondere oberhalb von 270 K liegt. Außerdem wird er mittels externer Energie angetrieben, also zum Beispiel mit einem Elektromotor oder einer Dampfturbine, jedenfalls nicht mit einer Turbine, die einen Prozessstrom der Luftzerlegung entspannt. Entgegen der Grundidee der JP 1 1 1 18352 Ä wird der Kreislaufverdichter nicht als Kaltverdichter betrieben und auch nicht von einer Turbine angetrieben, in welcher der Kreislaufstickstoffstrom entspannt wird. This object is solved by the characterizing features of claim 1. The cycle compressor is designed as a warm compressor, that is, it is operated at an inlet temperature which is above 250 K, in particular above 270 K. In addition, it is powered by external energy, for example, with an electric motor or a steam turbine, at least not with a turbine that relaxes a process stream of air separation. Contrary to the basic idea of JP 1 1 18352 Ä the cycle compressor is not operated as a cold compressor and not driven by a turbine in which the circulation nitrogen flow is relaxed.
Hierdurch kann der Kreislaufstickstrom unabhängig vom Kältebedarf der Anlage eingestellt werden. Insbesondere kann die Heizleistung im Sumpfverdampfer der Hochdrucksäule frei gewählt werden. Damit kann das Verfahren erheblich flexibler an aktuelle Bedürfnisse angepasst und damit energetisch günstiger betrieben werden. As a result, the circulation embroidery stream can be set independently of the refrigeration requirement of the plant. In particular, the heating power in the bottom evaporator of High pressure column can be freely selected. Thus, the process can be adapted much more flexibly to current needs and thus operated energetically cheaper.
Bei dem erfindungsgemäßen Verfahren wird die Hochdrucksäule mit einem In the method according to the invention, the high-pressure column with a
Betriebsdruck (am Kopf) von beispielsweise 5 bis 6,5 bar, vorzugsweise 5,2 bis 6,2 bar betrieben. Im Fall des Einsatzes eines Zwei- oder Mehr-Kolonnehsystems als Operating pressure (at the top), for example, 5 to 6.5 bar, preferably operated 5.2 to 6.2 bar. In the case of using a two or more Kolonnehsystems as
Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung beträgt der Distillation column system for nitrogen-oxygen separation is the
Niederdrucksäulendruck weniger als 2 bar, vorzugsweise weniger als 1 ,6 bar. Der "gasförmige Kreislaufstickstoffstrom" aus dem Destilliersäulen-System zur Low pressure column pressure less than 2 bar, preferably less than 1, 6 bar. The "gaseous cycle nitrogen flow" from the distillation column system for
Stickstoff-Sauerstoff-Trennung zum Kreislaufverdichter wird vorzugsweise vom Kopf der Hochdrucksäule abgezogen.  Nitrogen-oxygen separation to the cycle compressor is preferably withdrawn from the top of the high-pressure column.
Der Produktdruck des Druckstickstoffprodukts kann gleich, niedriger oder höher als der Druck sein, unter dem der erste Teilstrom aus dem Kreislaufverdichter abgezogen wird, er liegt beispielsweise auf dem Niveau des Betriebsdrucks der Hochdrucksäule oder höher. Das Druckstickstoffprodukt kann in einer Mehrzahl von Unterströmen unter unterschiedlichen Drücken abgegeben werden; in diesem Fall wird die Gesamtheit des Druckstickstoffprodukts hier als "zweiter Teilstrom" bezeichnet. The product pressure of the pressurized nitrogen product may be equal to, lower, or higher than the pressure at which the first substream is withdrawn from the cycle compressor, for example, at the level of the operating pressure of the high pressure column or higher. The pressurized nitrogen product may be discharged in a plurality of sub-streams at different pressures; In this case, the entirety of the pressurized nitrogen product is referred to herein as a "second partial stream".
Im Rahmen einer Weiterbildung der Erfindung kann die Menge des im unteren As part of a development of the invention, the amount of the lower
Abschnitt der Niederdrucksäule aufsteigenden Dampfs durch die Einstellung der Menge des zweiten Teilstroms des Kreislaufstickstoffstroms eingestellt werden und die Menge der Rücklaufflüssigkeit im oberen Teil der Niederdrucksäule indirekt über die Einstellung der Menge des ersten Teilstroms des Kreislaufstickstoffstroms, also die Heizleistung des Hochdrucksäulen-Sumpfverdampfers. Hiermit kann das Section of the low pressure column ascending steam can be adjusted by adjusting the amount of the second partial flow of the cycle nitrogen flow and the amount of reflux liquid in the upper part of the low pressure column indirectly via the adjustment of the amount of the first partial flow of the circulating nitrogen stream, so the heating power of the high-pressure column sump evaporator. This can do that
Rücklaufverhältnis sowohl im oberen als auch im unteren Teil der Niederdrucksäule optimiert werden. Wird die Menge des ersten Teilstroms des Kreislaufstroms erhöht oder vermindert und dadurch mehr oder weniger Stickstoff im Sumpfverdampfer kondensiert, steht eine entsprechend veränderte Menge an flüssigem Stickstoff als Rücklaufflüssigkeit in der Hochdrucksäule zur Verfügung und es kann mehr oder weniger Hochdruckstickstoff entnommen werden; es spielt dabei keine Rolle ob ein Teil des flüssigen Stickstoffs aus dem Sumpfverdampfer unmittelbar in die Niederdrucksäule eingeleitet wird, oder ob er in die Hochdrucksäule eingeleitet wird und damit entsprechend mehr (oder weniger) flüssiger Stickstoff aus der Hochdrucksäule beziehungsweise aus dem Hauptkondensator in die Niederdrucksäule übergeleitet werden kann. Wird weniger oder mehr Hochdrucksäulen-Stickstoff als "zweiter Teilstrom" entnommen und steht somit mehr oder weniger Heizleistung am Hauptkondensator zur Verfügung, wird entsprechend mehr oder weniger aufsteigender Dampf für den unteren Teil der Niederdrucksäule erzeugt. Return ratio can be optimized both in the upper and in the lower part of the low pressure column. If the amount of the first partial flow of the cycle stream is increased or decreased and thereby more or less nitrogen condenses in the bottom evaporator, a correspondingly altered amount of liquid nitrogen is available as reflux liquid in the high-pressure column and it can be more or less high-pressure nitrogen removed; It does not matter if a part of the liquid nitrogen from the bottom evaporator is introduced directly into the low pressure column, or whether it is introduced into the high pressure column and thus correspondingly more (or less) liquid nitrogen from the high pressure column or from the main condenser can be transferred to the low pressure column. If less or more high-pressure column nitrogen is withdrawn as a "second partial flow" and thus more or less heating power is available at the main condenser, correspondingly more or less rising steam is generated for the lower part of the low-pressure column.
Das Verfahren eignet sich insbesondere für die Gewinnung von unreinem The method is particularly suitable for the extraction of impure
Drucksauerstoff mit einer Reinheit von weniger 98 mol-%, vorzugsweise von 97 % oder weniger. Es kann besonders vorteilhaft bei IGCC-Anlagen eingesetzt werden, in denen mindestens ein Teil des Drucksauerstoffprodukts in eine Kohlevergasung zur Pressure oxygen with a purity of less than 98 mol%, preferably of 97% or less. It can be used particularly advantageously in IGCC plants in which at least a portion of the pressure oxygen product in a coal gasification for
Erzeugung eines Brenngases eingeleitet wird und mindestens ein Teil des Generation of a fuel gas is initiated and at least part of the
Druckstickstoffprodukts zum Kohletransport eingesetzt wird. Pressure nitrogen product is used for coal transport.
Grundsätzlich kann das erfindungsgemäße Verfahren mit konstanter In principle, the inventive method with constant
Gesamtdruckstickstoffproduktmenge gefahren werden, wobei die Total nitrogen pressure product quantity to be driven, the
Gesamtdruckstickstoffproduktmenge durch die Summe der Mengenströme gebildet wird, die stromaufwärts und/oder stromabwärts des Kreislaufverdichters und/oder von einer Zwischenstufe des Kreislaufverdichters unter einem Produktdruck aus demTotal nitrogen pressure product quantity is formed by the sum of the flow rates, the upstream and / or downstream of the cycle compressor and / or of an intermediate stage of the cycle compressor under a product pressure from the
Kreislaufstickstoffstrom abgezweigt und als Druckstickstoffprodukt gewonnen werden, also die Gesamtmenge an Stickstoffprodukt, die letztendlich von der Hochdrucksäule kommt und nicht aus der Niederdrucksäule oder einer anderen Säule. (Diese und alle anderen Mengenangaben sind molar zu verstehen.) Circuit nitrogen flow diverted and recovered as pressurized nitrogen product, so the total amount of nitrogen product, which ultimately comes from the high pressure column and not from the low pressure column or other column. (These and all other quantities are to be understood as molar.)
In einer bevorzugten Ausgestaltung wird das Verfahren jedoch mit variabler Last gefahren, wobei In a preferred embodiment, however, the method is run with variable load, wherein
in einem ersten Lastfall in a first load case
- eine erste Gesamtdruckstickstoffproduktmenge PN1 gewonnen wird,  a first total pressure nitrogen product quantity PN1 is obtained,
- der erste Teilstrom in einer ersten Teilstrommenge TS1 durch den  - The first partial flow in a first partial flow TS1 by the
Sumpfverdampfer der Hochdrucksäule geführt wird und  Bottom evaporator of the high pressure column is performed and
- die Einsatzluft in einer ersten Einsatzluftmenge EL1 in den Luftverdichter eingeleitet wird,  the feed air is introduced into the air compressor in a first quantity of feed air EL1,
und wobei in einem zweiten Lastfall - eine zweite, höhere Gesamtdruckstickstoffproduktmenge PN2 gewonnen wird,and wherein in a second load case a second, higher total pressure nitrogen product quantity PN2 is obtained,
PN2 > PN1 , PN2> PN1,
- der erste Teilstrom in einer zweiten, höheren Teilstrommenge TS2 durch den - The first partial flow in a second, higher partial flow TS2 by the
Sumpfverdampfer der Hochdrucksäule geführt wird, TS2 > TS1 , und Sump evaporator of the high pressure column is led, TS2> TS1, and
- die Einsatzluft in einer zweiten Einsatzluftmenge EL2 in den Luftverdichter eingeleitet wird, wobei die zweite Einsatzluftmenge EL2 gleich der ersten Einsatzluftmenge EL1 oder nur unwesentlich höher ist, wobei gilt  - The feed air is introduced in a second amount of feed air EL2 in the air compressor, wherein the second feed air quantity EL2 is equal to the first feed air quantity EL1 or only slightly higher, where applicable
(EL2 - EL1 )/EL1 < 0,2 · (PN2 - PN1)/PN1. Trotz der erhöhten Gesamtproduktion an Druckstickstoff bleibt also die  (EL2 - EL1) / EL1 <0.2 · (PN2 - PN1) / PN1. Despite the increased total production of pressurized nitrogen remains so
Einsatzluftmenge gleich oder wird nur unwesentlich erhöht. "Unwesentlich" bedeutet hier, dass die relative Änderung der Luftmenge höchstens ein Fünftel, vorzugsweise weniger als ein Zehntel der relativen Änderung der Produktmenge an Druckstickstoff beträgt. Wenn in einem konkreten Beispiel die Gesamtdruckstickstoffproduktmenge PN2 im zweiten Lastfall um 50 % höher als im ersten, wird die zweite Einsatzluftmenge EL2 um weniger als 10 % erhöht, vorzugsweise bleibt sie gleich. Mit gleich bleibender oder nur geringfügig erhöhter Luftmenge kann also eine wesentliche Erhöhung der Gesamtproduktion an Druckstickstoff erreicht werden. Außerdem führt die im  Amount of air used is equal or is only slightly increased. As used herein, "insubstantial" means that the relative change in the amount of air is at most one-fifth, preferably less than one-tenth of the relative change in the amount of pressurized nitrogen product. In a concrete example, when the total pressure nitrogen product quantity PN2 is 50% higher in the second load case than in the first one, the second feed air quantity EL2 is increased by less than 10%, preferably remaining the same. With a constant or only slightly increased amount of air so a significant increase in the total production of pressurized nitrogen can be achieved. In addition, the leads in the
Wesentlichen gleich bleibende Luftmenge dazu, dass der Trennprozess innerhalb des Destilliersäulen-Systems bei einer Laständerung nur relativ wenig gestört wird und damit die Produktreinheiten weitgehend konstant bleiben. Außerdem kann die Menge an gasförmigem Drucksauerstoffprodukt gleich bleiben beziehungsweise sich nur unwesentlich ändern. In einem konkreten Beispiel wird ein zweiter Teilstrom stromabwärts des Essentially constant amount of air to the fact that the separation process within the distillation column system is only relatively little disturbed in a load change and thus the product purities remain largely constant. In addition, the amount of gaseous pressure oxygen product can remain the same or change only insignificantly. In a concrete example, a second partial flow downstream of the
Kreislaufverdichters als einziges Druckstickstoffprodukt entnommen. Bei einer  Recirculation compressor taken as the only pressure nitrogen product. At a
Lasterhöhung von einem ersten zu einem zweiten Lastfall wird die Load increase from a first to a second load case is the
Gesamtdruckstickstoffproduktmenge (also hier die Menge des zweiten Teilstroms) um 25 % erhöht (PN2 = 1 ,25 PN1 ). Gleichzeitig wird die Menge des Heizstroms des Hochdrucksäulen-Sumpfverdampfers um ca. 45 % erhöht (TS2 = 1 ,45 TS1 ), dieTotal pressure nitrogen product quantity (ie here the amount of the second partial flow) increased by 25% (PN2 = 1, 25 PN1). At the same time, the amount of heating current of the high-pressure column bottom evaporator is increased by approximately 45% (TS2 = 1, 45 TS1), the
Einsatzluftmenge bleibt dabei aber unverändert. Die Änderung des ersten Teilstroms hängt linear mit der Druckstickstoffprodukt-Änderung zusammen. Feed air quantity remains unchanged. The change of the first partial flow is linearly related to the pressure nitrogen product change.
Die Erhöhung der Druckstickstoff-Entnahme mit gleich bleibender Einsatzluftmenge hat einen fast unveränderten Sauerstoffgehalt im unreinen Stickstoff-Produkt der Niederdrucksäule (UN2) zur Folge. Die Menge des innenverdichteten Produkt - Sauerstoffs bleibt konstant. Mit der Erhöhung der Druckstickstoff-Entnahme wird die UN2-Menge kleiner, die gleichzeitig die aufsteigende Gasmenge in der The increase in pressure nitrogen removal with a constant amount of feed air has an almost unchanged oxygen content in the impure nitrogen product of Low pressure column (UN2) result. The amount of internally compressed product oxygen remains constant. As the removal of the pressure nitrogen increases, the amount of UN2 becomes smaller and at the same time the increasing amount of gas in the
Niederdrucksäule bestimmt. Erhöht man die Druckstickstoff-Entnahme um Low pressure column determined. If the pressure nitrogen removal is increased
10.000 Nm3/h, vermindert sich auch die UN2-Menge um 10.000 Nm3/h. Die Last am Hauptkondensator ist also direkt proportional der Druckstickstoff-Entnahme. Werden zum Beispiel 10.000 Nn Vh mehr entnommen, werden 10.000 Nm /h weniger Stickstoff am Hauptkondensator verflüssigt. Die Wasch-LIN-Flüssigkeit für die Niederdrucksäule wird ebenfalls entsprechend kleiner (um ca. 0,4*10.000 = 4.000 Nm3/h). Das heißt das Rücklaufverhältnis im oberen Abschnitt der Niederdrucksäule bleibt fast unverändert. Die Wasch-LIN-Flüssigkeit für die Drucksäule (aus dem Hauptkondensator) wird dabei um ca. 0,6*10.000 = 6.000 Nm3/h geringer. Um aber die Produktreinheiten nicht zu verlieren, muss das Rücklaufverhältnis in der Drucksäule "wiederhergestellt" werden. Dieses wird nun durch entsprechende Erhöhung des ersten Teilstroms sichergestellt. 10,000 Nm 3 / h, the amount of UN2 is reduced by 10,000 Nm 3 / h. The load on the main condenser is therefore directly proportional to the pressure nitrogen removal. If, for example, 10,000 Nn more Vh are removed, 10,000 Nm / h less nitrogen is liquefied at the main condenser. The wash LIN liquid for the low pressure column is also correspondingly smaller (by about 0.4 * 10,000 = 4,000 Nm 3 / h). That is, the reflux ratio in the upper section of the low-pressure column remains almost unchanged. The wash LIN liquid for the pressure column (from the main condenser) is thereby reduced by about 0.6 * 10,000 = 6,000 Nm 3 / h. But in order not to lose the product purities, the reflux ratio in the pressure column must be "restored". This is now ensured by a corresponding increase in the first partial flow.
Die Regelung des ersten Teilstroms kann dabei mittels eines AIC-Reglers erfolgen (zum Beispiel mit Konstanthalten der Sauerstoff-Produktreinheit). The regulation of the first partial flow can be carried out by means of an AIC controller (for example, keeping the oxygen product purity constant).
Es ist ferner vorteilhaft, wenn ein dritter Teilstrom des Kreislaufstickstoffstroms als Turbinenstrom aus dem Kreislaufverdichter entnommen wird, arbeitsleistend entspannt und mindestens teilweise in das Destilliersäulen-System zur Stickstoff-Sauerstoff- Trennung eingeleitet wird. Die bei der arbeitsleistenden Entspannung des It is also advantageous if a third partial stream of the nitrogen cycle stream is taken as a turbine stream from the cycle compressor, work expanded and at least partially introduced into the distillation column system for nitrogen-oxygen separation. The at the work performing relaxation of the
Turbinenstroms erzeugte Energie wird vorzugsweise mechanisch auf einen Turbine power generated energy is preferably mechanically to a
Nachverdichter übertragen, in dem beispielsweise der Turbinenstrom stromaufwärts der arbeitsleistenden Entspannung und/oder der erste Teilstrom des Post-compressor in which, for example, the turbine stream upstream of the work-performing expansion and / or the first part of the flow
Kreislaufstickstoffstroms stromaufwärts seiner Einleitung in den Hauptwärmetauscher nachverdichtet werden.  Circulating nitrogen flow upstream of its introduction into the main heat exchanger are recompressed.
Alternativ kann Prozesskälte durch arbeitsleistende Entspannung eines Teilstroms der Einsatzluft gewonnen werden. Die dabei gewonnene mechanische Energie wird vorzugsweise auf einen Nachverdichter für die Turbinenluft übertragen. Alternatively, process cooling can be obtained by work-performing expansion of a partial flow of the feed air. The mechanical energy obtained is preferably transferred to a compressor for the turbine air.
Es ist günstig, wenn bei dem erfindungsgemäßen Verfahren eine Flüssigfraktion aus der Hochdrucksäule unter dem Betriebsdruck der Hochdrucksäule in einen It is favorable if in the process according to the invention a liquid fraction from the high-pressure column under the operating pressure of the high-pressure column into a
Kondensator-Verdampfer eingeleitet und dort in indirektem Wärmeaustausch mit mindestens einem Teil des arbeitsleistend entspannten Turbinenstroms mindestens teilweise verdampft wird, wobei der dabei erzeugte Dampf mindestens teilweise in die Hochdrucksäule zurückgeleitet wird. Das Aufkochen der Hochdrucksäule verbessert deren Trennwirkung. Als Heizmittel wird im Rahmen der Erfindung kein eigens zu verdichtender Strom eingesetzt, sondern der ohnehin auf geeignetem Druckniveau vorhandene Turbinenstrom. Der Kreislaufverdichter wird somit zu einem weiteren Zweck, der Ausheizung der Hochdrucksäule genutzt. Condenser-evaporator introduced and there in indirect heat exchange with At least a portion of the work performed relaxing turbine stream is at least partially evaporated, wherein the steam generated thereby is at least partially returned to the high-pressure column. The boil up of the high pressure column improves their release effect. As a heating means in the invention is not used to be specially compressed stream, but the already existing at a suitable pressure level turbine flow. The cycle compressor is thus used for a further purpose, the heating of the high-pressure column.
Der "Kondensator-Verdampfer", in dem eine Flüssigfraktion aus der Hochdrucksäule aufgekocht wird, ist als vom Hauptwärmetauscher getrennter Wärmetauscher ausgeführt, insbesondere als mindestens ein Plattenwärmetauscherblock, höchst vorzugsweise als ein einziger Plattenwärmetauscherblock; er kann innerhalb der Hochdrucksäule angeordnet sein oder auch außerhalb in einem separaten Behälter. Die Flüssigfraktion zum Kondensator- Verdampfer kann aus dem Sumpf der The "condenser-evaporator" in which a liquid fraction is boiled from the high-pressure column is designed as a heat exchanger separate from the main heat exchanger, in particular as at least one plate heat exchanger block, most preferably as a single plate heat exchanger block; it may be located within the high pressure column or outside in a separate container. The liquid fraction to the condenser-evaporator can from the bottom of the
Hochdrucksäule entnommen werden - der Kondensator-Verdampfer stellt dann den Sumpfverdampfer dar und ist vorzugsweise unmittelbar im Sumpf der Hochdrucksäule angeordnet. Alternativ ist der Kondensator-Verdampfer als Zwischenverdampfer der Hochdrucksäule ausgebildet und beispielsweise auf einem Zwischenniveau im Inneren der Hochdrucksäule angeordnet; die Flüssigfraktion für den Kondensator-Verdampfer wird dann an der entsprechenden Zwischenstelle der Hochdrucksäule abgezogen. In diesem Fall werden der Sumpf- und der Zwischenverdampfer von verschiedenen Teilströmen des Kreislaufstickstoffstroms beheizt, die bei unterschiedlichen geeigneten Drücken aus dem Kreislaufverdichter entnommen werden.  High-pressure column are removed - the condenser-evaporator then represents the bottom evaporator and is preferably arranged directly in the bottom of the high-pressure column. Alternatively, the condenser-evaporator is designed as an intermediate evaporator of the high-pressure column and arranged for example at an intermediate level in the interior of the high-pressure column; the liquid fraction for the condenser-evaporator is then withdrawn at the corresponding intermediate point of the high-pressure column. In this case, the bottom and the intermediate evaporator are heated by different partial streams of the circulating nitrogen stream, which are removed at different suitable pressures from the cycle compressor.
Häufig ist der Druck des ersten Teilstroms des Kreislaufstickstoffstroms der höchste im Verfahren benötigte Druck. Bei besonders hohem Kältebedarf kann auch der dritte Teilstrom des Kreislaufstickstoffstroms (Turbinenstrom) auf diesem Druckniveau aus dem Kreislaufverdichter abgezogen werden. In vielen Fällen ist es aber günstig, den dritten Teilstrom des Kreislaufstickstoffstroms unter einem oberen Zwischendruck (P3, P4) von einer Zwischenstufe des Kreislaufverdichters abzuziehen und anschließend der arbeitsleistenden Entspannung zuzuführen. Der Eintrittsdruck der arbeitsleistenden Entspannung liegt dann etwa auf dem Niveau des oberen Zwischendrucks, kann aber gegebenenfalls durch einen an die Entspannungsmaschine gekoppelten Often, the pressure of the first partial flow of the cycle nitrogen flow is the highest pressure required in the process. In the case of particularly high refrigeration demand, the third partial flow of the circulating nitrogen stream (turbine stream) can also be withdrawn from the cycle compressor at this pressure level. In many cases, however, it is favorable to subtract the third partial flow of the circulating nitrogen stream under an upper intermediate pressure (P3, P4) from an intermediate stage of the cycle compressor and then to supply the work-performing expansion. The inlet pressure of the work-performing expansion is then approximately at the level of the upper intermediate pressure, but may optionally by a coupled to the expansion machine
Nachverdichter erhöht werden. Der erste Teilstrom des Kreislaufstickstoffstroms kann unter einem hohen Druck (P4) aus dem Kreislaufverdichter abgezogen werden, der höher als der Zwischendruck (P3) ist, bei dem der dritte Teilstrom des Kreislaufstickstoffstroms aus dem . Booster be increased. The first partial flow of the circulating nitrogen stream can be withdrawn from the cycle compressor at a high pressure (P4) which is higher than the intermediate pressure (P3) at which the third partial flow of the circulating nitrogen stream flows out of the circuit.
Kreislaufverdichter entnommen wird; anschließend wird der erste Teilstrom unter diesem hohen Druck oder unter einem noch höheren Druck in den Circulation compressor is removed; Subsequently, the first partial flow is under this high pressure or under an even higher pressure in the
Hauptwärmetauscher eingeleitet. Damit lässt sich einerseits ein besonders hoher Produktdruck für das gasförmige Drucksauerstoffprodukt realisieren, andererseits ist dieses Druckniveau entkoppelt von dem Eintrittsdruck der arbeitsleistenden Main heat exchanger initiated. On the one hand, this makes it possible to realize a particularly high product pressure for the gaseous pressure oxygen product, on the other hand, this pressure level is decoupled from the inlet pressure of the work-producing
Entspannung, der niedriger sein kann. Darüber hinaus kann auch ein Teil des Relaxation, which can be lower. In addition, part of the
Kreislaufstickstoffstroms unter dem hohen Druck als Druckstickstoffprodukt gewonnen werden, ohne dass zusätzlicher Maschinenaufwand notwendig wäre.  Circulation nitrogen flow can be obtained under the high pressure as a pressure nitrogen product, without additional machinery costs would be necessary.
In einer ersten Betriebsweise wird ein vierter Teilstrom des Kreislaufstickstoffstroms unter einem unteren Zwischendruck (P2) von einer Zwischenstufe des In a first mode of operation, a fourth substream of the loop nitrogen stream is subjected to a lower intermediate pressure (P2) from an intermediate stage of the
Kreislaufverdichters abgezogen, in einer Zwischendruckpassage des Withdrawn circuit compressor, in an intermediate pressure passage of the
Hauptwärmetauschers abgekühlt und mit dem arbeitsleistend entspannten Main heat exchanger cooled and with the work performing relaxed
Turbinenstrom stromaufwärts des Kondensator-Verdampfers vermischt. Dies ist insbesondere dann günstig, wenn der Turbinenstrom zur Ausheizung der Turbine stream mixed upstream of the condenser-evaporator. This is particularly favorable when the turbine stream for heating the
Hochdrucksäule in dem ersten Kondensator-Verdampfer genutzt wird. Wenn relativ wenig Kälte benötigt wird, kann der Turbinenstrom so klein sein, dass er alleine nicht mehr die für die Kolonnenheizung benötigte Wärme aufbringen kann. Durch die Zumischung des vierten Teilstroms kann zusätzliche Wärme in den Kondensator- Verdampfer eingetragen werden. Kälteerzeugung und Kolonnenbetrieb sind damit unabhängig. Die Kälteleistung, die durch den Turbinenstrom erbracht wird, kann in weitem Bereich variiert werden, ohne dass die den Betrieb des Destilliersäulen- Systems beeinflusst. High-pressure column is used in the first condenser-evaporator. If relatively little cooling is needed, the turbine flow can be so small that it alone can no longer apply the heat needed for the column heating. By adding the fourth partial flow, additional heat can be introduced into the condenser-evaporator. Refrigeration and column operation are thus independent. The cooling capacity provided by the turbine flow can be widely varied without affecting the operation of the distillation column system.
Umgekehrt kann in einer zweiten Betriebsweise ein Teil des arbeitsleistend Conversely, in a second mode of operation, part of the work can be done
entspannten Turbinenstroms in der Zwischendruckpassage des Hauptwärmetauschers angewärmt und dem Kreislaufverdichter an einer Zwischenstufe zugeführt werden. Dies ist vor Allem dann vorteilhaft, wenn viel Kälte erzeugt wird und der Turbinenstrom damit zu groß für die Beheizung des ersten Kondensator-Verdampfers ist. Für diese Rückführung und für die Führung des vierten Teilstroms in der ersten Betriebsweise wird vorzugsweise eine Pendelleitung, die durch dieselben Passagen des Hauptwärmetauschers führt ("Zwischenpassage"). heated turbine stream in the intermediate pressure passage of the main heat exchanger and fed to the cycle compressor at an intermediate stage. This is especially advantageous when a lot of cold is generated and the turbine flow is thus too large for the heating of the first condenser-evaporator. For this return and for the management of the fourth partial flow in the first mode is preferably a shuttle line that passes through the same passages of the main heat exchanger ("intermediate passage").
Vorzugsweise wird der flüssige Sauerstoffstrom für die Innenverdichtung aus dem unteren Bereich der Niederdrucksäule entnommen The liquid oxygen stream for internal compression is preferably taken from the lower region of the low-pressure column
Zusätzlich kann eine Zwischenflüssigkeit, deren Sauerstoffgehalt zwischen demjenigen der sauerstoffangereicherten Flüssigkeit und demjenigen der stickstoffangereicherten Flüssigkeit liegt, aus der Hochdrucksäule entnommen und der Niederdrucksäule an einer zweiten Zwischenstelle zugeführt werden, die oberhalb der ersten Zwischenstelle angeordnet ist, wobei die Zwischenflüssigkeit insbesondere in Höhe eines In addition, an intermediate liquid whose oxygen content is between that of the oxygen-enriched liquid and that of the nitrogen-enriched liquid can be taken out of the high-pressure column and fed to the low-pressure column at a second intermediate point located above the first intermediate point, the intermediate liquid being in particular at a height
Zwischenverdampfers der Hochdrucksäule entnommen wird. Intermediate evaporator is removed from the high pressure column.
Die Erfindung betrifft außerdem eine Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Tieftemperaturzerlegung von Luft gemäß den The invention also relates to an apparatus for recovering pressure oxygen and pressurized nitrogen by cryogenic separation of air in accordance with
Patentansprüchen 12 bis 14. Claims 12 to 14.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert, die alle als Zwei-Säulen-Systeme ausgebildet sind. Hierbei zeigen: The invention and further details of the invention are explained in more detail below with reference to embodiments shown in the drawings, which are all designed as two-pillar systems. Hereby show:
Figur 1 ein erstes Ausführungsbeispiel der Erfindung mit zwei Figure 1 shows a first embodiment of the invention with two
Kondensator-Verdampfern in der Hochdrucksäule, bei dem die arbeitsleistende Entspannung auf den Eintrittsdruck der zweiten Stufe des Kreislaufverdichters führt,  Condenser-evaporators in the high-pressure column, in which the work-performing expansion leads to the inlet pressure of the second stage of the cycle compressor,
Figur 2 eine Abwandlung des ersten Ausführungsbeispiels, bei dem die arbeitsleistende Entspannung auf den Eintrittsdruck der zweiten Stufe des Kreislaufverdichters führt,  FIG. 2 shows a modification of the first exemplary embodiment, in which the work-performing expansion leads to the inlet pressure of the second stage of the cycle compressor,
Figur 3 ein Ausführungsbeispiel mit nur einem Kondensator-Verdampfer in der Hochdrucksäule und Nachverdichtung des Turbinenstroms, FIG. 3 shows an exemplary embodiment with only one condenser-evaporator in the high-pressure column and re-compression of the turbine flow,
Figur 4 eine Abwandlung dieser Variante mit Nachverdichtung des ersten Figure 4 shows a modification of this variant with recompression of the first
Teilstroms des Kreislaufstickstoffstroms,  Partial flow of the circulating nitrogen stream,
Figuren 5 bis 7 weitere Ausführungsbeispiele mit zwei Kondensator-Verdampfern in der Hochdrucksäule und Figuren 8 und 9 zwei Ausführungsbeispiele mit nur einem Kondensator- Verdampfer in der Hochdrucksäule und mit einer Luftturbine. Figures 5 to 7 further embodiments with two condenser-evaporators in the high-pressure column and Figures 8 and 9 show two embodiments with only one condenser evaporator in the high pressure column and with an air turbine.
In den Zeichnungen nicht dargestellt ist, wie atmosphärische Luft auf bekannte Weise über ein Filter von einem Luftverdichter angesaugt und auf einen Druck von ca. 6 bar verdichtet und weiter über eine Vorkühlungseinrichtung und eine Not shown in the drawings, as atmospheric air sucked in a known manner via a filter of an air compressor and compressed to a pressure of about 6 bar and further via a pre-cooling device and a
Reinigungseinrichtung geführt wird. Cleaning device is guided.
In Figur 1 wird die verdichtete und gereinigte Einsatzluft 6 in einem In Figure 1, the compressed and purified feed air 6 in a
Hauptwärmetauscher 20 auf etwa Taupunkt abgekühlt und über Leitung 7 einem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung zugeführt, das in dem Beispiel aus einer Hochdrucksäule 8 und den ihr zugeordneten Kolonnenverdampfern, einem Sumpfverdampfer 9 und einem Zwischenverdampfer 10 besteht, sowie aus einer Niederdrucksäule 460 und aus einem Hauptkondensator 461 , über den die Hochdrucksäule 8 und die Niederdrucksäule 460 in wärmetauschender Verbindung stehen, indem das Kopfgas der Hochdrucksäule in indirekten Wärmeaustausch mit der Sumpfflüssigkeit der gebracht wird. Der Betriebsdruck am Kopf der Niederdrucksäule 460 beträgt ca. 1 ,4 bar. Der Hauptwärmetauscher 20 kann integriert oder gesplittet ausgeführt werden, Figur 1 und die nachfolgenden Zeichnungen zeigen nur die Main heat exchanger 20 is cooled to about dew point and fed via line 7 to a distillation column system for nitrogen-oxygen separation, which consists in the example of a high-pressure column 8 and its associated column evaporators, a bottom evaporator 9 and an intermediate evaporator 10, and a low-pressure column 460th and a main condenser 461 through which the high-pressure column 8 and the low-pressure column 460 are in heat-exchanging connection by bringing the top gas of the high-pressure column into indirect heat exchange with the bottom liquid. The operating pressure at the top of the low-pressure column 460 is approximately 1.4 bar. The main heat exchanger 20 can be implemented integrated or split, Figure 1 and the following drawings show only the
Grundfunktion des Tauschers - warme Ströme werden durch kalte gekühlt. Basic function of the exchanger - warm currents are cooled by cold.
Die Sumpfflüssigkeit 462 ("sauerstoffangereicherte Flüssigkeit") aus der The bottom liquid 462 ("oxygen-enriched liquid") from the
Hochdrucksäule 8 beziehungsweise von der Verflüssigungsseite ihres High pressure column 8 and the liquefaction side of their
Sumpfverdampfers 9 wird vollständig durch einen ersten Unterkühlungs-Gegenströmer 16 und einen zweiten Unterkühlungs-Gegenströmer 415 geführt, in einem Drosselventil 463 auf Niederdrucksäulendruck entspannt und über Leitung 464 der Niederdrucksäule an einer ersten Zwischenstelle zugeführt. Ein Teil 465 der Zwischenflüssigkeit der Hochdrucksäule 8, die an der Verflüssigungsseite des Zwischenverdampfers 10 anfällt, wird von dort abgezogen, ebenfalls in den Unterkühlungs-Gegenströmern 16 und 416 unterkühlt und nach Drosselung 466 über Leitung 467 an einer zweiten Zwischenstelle der Hochdrucksäule 8 zugeleitet, die oberhalb der ersten Zwischenstelle liegt. Ein dritter Einsatzstrom in Form von unreinem flüssigen Stickstoff 468 wird nach Bottom evaporator 9 is passed completely through a first subcooling countercurrent 16 and a second subcooling countercurrent 415, expanded in a throttle valve 463 to low pressure column pressure and fed via line 464 of the low pressure column at a first intermediate point. A portion 465 of the intermediate liquid of the high-pressure column 8, which is obtained at the liquefaction side of the intermediate evaporator 10 is withdrawn from there, also supercooled in the subcooling countercurrents 16 and 416 and fed after throttling 466 via line 467 at a second intermediate point of the high pressure column 8, the is above the first intermediate point. A third feed stream in the form of impure liquid nitrogen 468 is after
Unterkühlung 16/416 und Drosselung 469 über Leitung 470 auf den Kopf der Undercooling 16/416 and throttling 469 via line 470 on the head of the
Niederdrucksäule 460 aufgegeben. Der flüssige Sauerstoff wird hier vom Sumpf der Niederdrucksäule 460 beziehungsweise von der Verflüssigungsseite des Hauptkondensators 461 entnommen und analog zu Strom 1 1 der Figur 1 in einen Innenverdichtungsstrom ("flüssiger Sauerstoffstrom") 412 und ein Flüssigprodukt (415/417) aufgeteilt. Low pressure column 460 abandoned. The liquid oxygen is taken here from the bottom of the low-pressure column 460 or from the liquefaction side of the main condenser 461 and analogously to stream 1 1 of Figure 1 in a Innenverdichtungsstrom ("liquid oxygen stream") 412 and a liquid product (415/417) split.
Im Sumpf der Niederdrucksäule 460 wird flüssiger Sauerstoff 1 1 erzeugt, der zu einem ersten Teil als "flüssiger Sauerstoffstrom" 12 in einer Pumpe 13 der - je nach In the bottom of the low-pressure column 460 liquid oxygen 1 1 is generated, the first part as a "liquid oxygen stream" 12 in a pump 13 of - depending on
Produktanforderungen - auf einen Druck von 6 bis 100 bar gebracht wird. Die Product requirements - brought to a pressure of 6 to 100 bar. The
Flüssigkeit (IC-LOX) wird unter diesem erhöhten Druck in den Hauptwärmetauscher 20 eingeleitet, im Hauptwärmetauscher verdampft oder pseudo-verdampft und auf etwa Umgebungstemperatur angewärmt. Schließlich wird der Sauerstoff als gasförmiges Drucksauerstoffprodukt 14 gewonnen. Liquid (IC-LOX) is introduced into the main heat exchanger 20 at this elevated pressure, vaporized or pseudo-evaporated in the main heat exchanger and warmed to about ambient temperature. Finally, the oxygen is recovered as gaseous pressure oxygen product 14.
Ein anderer Teil 15 der Sumpfflüssigkeit 1 1 der Niederdrucksäule 460 wird - gegebenenfalls nach Unterkühlung in dem Unterkühlungs-Gegenströmer 416 über Leitung 17 als flüssiges Sauerstoffprodukt (LOX) abgegeben. Another part 15 of the bottom liquid 1 1 of the low-pressure column 460 is - optionally after subcooling in the supercooling countercurrent 416 discharged via line 17 as a liquid oxygen product (LOX).
Vom Kopf der Hochdrucksäule 8 wird über Leitung 18 Stickstoff als "gasförmiger Kreislaufstickstoffstrom" abgezogen, in dem Unterkühlungs-Gegenströmer 16 und weiter (Leitung 19) im Hauptwärmetauscher 20 angewärmt und schließlich mindestens zu einem ersten Teil über Leitung 21 der ersten Stufe 23 eines Kreislaufverdichters 22 zugeführt, der in dem Beispiel vier Stufen 23, 25, 560 mit Nachkühlern 24, 16, 561 aufweist. (Die beiden letzten Verdichterstufen 560 und Nachkühler 561 sind vereinfacht dargestellt und können verfahrenstechnisch auch als zusätzlicher Produktverdichter zum dann als zweistufig anzusehenden Kreislaufverdichter 23/25 betrachtet werden) und mittels eines Elektromotors angetrieben wird; alternativ zu 23/25 kann ein From the top of the high-pressure column 8, nitrogen is withdrawn via line 18 as a "gaseous circulating nitrogen stream", heated in the supercooling countercurrent 16 and further (line 19) in the main heat exchanger 20 and finally at least to a first part via line 21 of the first stage 23 of a cycle compressor 22 fed, which has four stages 23, 25, 560 with aftercoolers 24, 16, 561 in the example. (The two last compressor stages 560 and aftercooler 561 are shown in simplified form and can also be regarded as an additional product compressor for the then two-stage cycle compressor 23/25) and is driven by means of an electric motor; as an alternative to 23/25 you can
Kreislaufverdichter im engeren Sinne mit drei oder mehr als vier Stufen eingesetzt werden.) Ein anderer Teil des Kreislaufstickstoffstroms kann als Druckstickstoffprodukt 27 (PGAN) unter etwa dem Betriebsdruck der Hochdrucksäule gewonnen werden. Circular compressors in the strict sense with three or more than four stages are used.) Another part of the circulating nitrogen stream can be obtained as compressed nitrogen product 27 (PGAN) below about the operating pressure of the high pressure column.
In der ersten Stufe 23 des Kreislaufverdichters 22 wird der Kreislaufstickstoffstrom auf einen ersten Zwischendruck (P1-GAN) von ca. 9 bar und in der zweiten Stufe 25 weiter auf einen zweiten Zwischendruck (P2-GAN) von ca. 12 bar verdichtet. Die beiden letzten Stufen 560 komprimieren auf einen hohen Druck, der das 1 ,4 bis 2,5- Fache des Sauerstoffdrucks beträgt (P4-GAN), beziehungsweise einen dritten Zwischendruck (P3-GAN). (Weitere) Druckstickstoffproduktströme können - je nach Bedarf - von jedem dieser Druckniveaus (Leitungen 27, 53, 29, 565, 564) abgezogen werden; die Gesamtheit dieser Druckstickstoffproduktströme bildet einen "zweiten Teilstrom des Kreislaufstickstoffstroms". Ein Teil des Kreislaufstickstoffstroms auf einem dieser Niveaus bildet einen "dritten Teilstrom", wird in einem Nachverdichter 566 auf den 1 ,3 bis 2-fachen Druck nachverdichtet und nach Nachkühlung als In the first stage 23 of the cycle compressor 22, the cycle nitrogen flow is compressed to a first intermediate pressure (P1-GAN) of approximately 9 bar and in the second stage 25 further to a second intermediate pressure (P2-GAN) of approximately 12 bar. The last two stages 560 compress to a high pressure which is 1.4 to 2.5 times the oxygen pressure (P4-GAN), or a third one Intermediate pressure (P3-GAN). (Further) pressurized nitrogen product streams may be withdrawn from each of these pressure levels (lines 27, 53, 29, 565, 564) as needed; the entirety of these pressure nitrogen product streams forms a "second partial stream of the cycle nitrogen stream". Part of the circulating nitrogen flow at one of these levels forms a "third partial flow", is recompressed to 1, 3 to 2 times the pressure in a secondary compressor 566 and after after-cooling as
Turbinenstrom 40 im Hauptwärmetauscher auf eine Zwischentemperatur abgekühlt und schließlich in einer Entspannungsmaschine 41 , die vorzugsweise durch eine Expansionsturbine gebildet wird, arbeitsleistend entspannt. Der arbeitsleistend entspannte Turbinenstrom 42 wird zu mindestens einem ersten Teil 30 in dem Turbine stream 40 is cooled in the main heat exchanger to an intermediate temperature and finally expanded in a relaxation machine 41, which is preferably formed by an expansion turbine, performing work. The work performed relaxing turbine stream 42 is at least a first part 30 in the
Zwischenverdampfer 9 ("erster Kondensator-Verdampfer") der Hochdrucksäule 8 als Heizmittel eingesetzt. Hierbei wird er in indirektem Wärmeaustausch mit  Intermediate evaporator 9 ("first condenser-evaporator") of the high pressure column 8 used as a heating medium. Here he is in indirect heat exchange with
verdampfender Zwischenflüssigkeit der Hochdrucksäule 8 mindestens teilweise verflüssigt. Anschließend wird dieser Strom über die Leitung 31 , durch den evaporating intermediate liquid of the high-pressure column 8 at least partially liquefied. Subsequently, this current via the line 31, through the
Unterkühlungs-Gegenströmer 16, das Drosselventil 32 und schließlich Leitung 33 wieder in den Kopf der Hochdrucksäule 8 zurückgeleitet. Subcooling countercurrent 16, the throttle valve 32 and finally line 33 back into the head of the high pressure column 8 returned.
Für eine konkrete Anlage wird je nach Kältebedarf einer der Drücke P2-GAN bis P4- GAN für den Strom 540 ausgewählt und eine entsprechende Verrohrung realisiert. Die in der Expansionsturbine 41 erzeigt mechanische Leistung wird durch mechanische Kopplung auf den Nachverdichter 566 übertragen. Alternativ kann die Turbine 41 an einen anderen Verdichter, einen Generator oder an eine dissipative Bremseinrichtung gekoppelt sein. Am Kopf der Hochdrucksäule 8 kann Flüssigstickstoff 43 als weiterer Produktstrom (PLIN) abgezogen werden Depending on the refrigeration requirement, one of the pressures P2-GAN to P4-GAN for the flow 540 is selected for a specific system and corresponding piping is realized. The mechanical power produced in the expansion turbine 41 is transmitted to the booster 566 by mechanical coupling. Alternatively, the turbine 41 may be coupled to another compressor, a generator or to a dissipative braking device. At the top of the high-pressure column 8, liquid nitrogen 43 can be withdrawn as a further product stream (PLIN)
Mindestens ein Teil des Kreislaufstickstoffstroms, der auf den Enddruck des At least part of the circulating nitrogen flow, which is at the final pressure of the
Kreislaufverdichters 22 verdichtet wurde, bildet eine "Hochdruck-Prozessstrom", der im Hauptwärmetauscher 20 die Wärme für die (Pseudo-)Verdampfung des flüssigen Drucksauerstoffs liefert. Der kalte Hochdruck-Prozessstrom 35 wird in dem Circular compressor 22 is compressed, forms a "high-pressure process stream", which provides the heat in the main heat exchanger 20 for the (pseudo) evaporation of the liquid pressure oxygen. The cold high pressure process stream 35 is in the
Unterkühlungs-Gegenströmer 16 abgekühlt (in Figur 1 nicht dargestellt), in einem Drosselventil 36 auf Hochdrucksäulendruck entspannt und schließlich über Leitung 37 auf den Kopf der Hochdrucksäule 8 aufgegeben. Die Entspannung auf Subcooling countercurrent 16 cooled (not shown in Figure 1), expanded in a throttle valve 36 to high pressure column pressure and finally fed via line 37 to the top of the high pressure column 8. The relaxation on
Hochdrucksäulendruck kann alternativ auch arbeitsleistend in einer Flüssigturbine 38 durchgeführt werden; in dem dargestellten Beispiel wird die Flüssigturbine 38 durch einen Generator 39 gebremst. High-pressure column pressure can alternatively work to perform in a liquid turbine 38th be performed; In the example shown, the liquid turbine 38 is braked by a generator 39.
Vom Kopf der Niederdrucksäule 460 wird Unreinstickstoff 50 als Restgas abgezogen, in den Unterkühlungs-Gegenströmern 416 und 16 und weiter (Leitung 51 , P-UN2) im Hauptwärmetauscher 20 angewärmt und schließlich über Leitung 52 als Restprodukt abgegeben; es kann in dem Verfahren noch als Regeneriergas oder als trockenes Gas in einem Verdunstungskühler genutzt werden. Ein Teil 45 des Kreislaufstickstoffstroms stromabwärts der ersten Stufe 23 des From the top of the low-pressure column 460 impure nitrogen 50 is withdrawn as residual gas, warmed in the subcooling countercurrents 416 and 16 and further (line 51, P-UN2) in the main heat exchanger 20 and finally discharged via line 52 as a residual product; it can still be used in the process as a regeneration gas or as a dry gas in an evaporative cooler. A portion 45 of the cycle nitrogen stream downstream of the first stage 23 of the
Kreislaufverdichters 22 bildet einen "ersten Teilstrom des Kreislaufstickstoffstroms" und wird - nach Abkühlung im Hauptwärmetauscher 20 - als Zwischendruck- Kreislaufstickstoffstrom 46 in dem Sumpfverdampfer 9 der Hochdrucksäule mindestens teilweise verflüssigt. Anschließend wird der Zwischendruck-Kreislaufstickstoffstrom über Leitung 47, den Unterkühlungs-Gegenströmer 16, und das Drosselventil 48 auf den Kopf der Hochdrucksäule 8 aufgegeben.  Circular compressor 22 forms a "first partial flow of the circulating nitrogen stream" and is - after cooling in the main heat exchanger 20 - at least partially liquefied as intermediate pressure circulating nitrogen 46 in the bottom evaporator 9 of the high pressure column. Subsequently, the intermediate pressure circulation nitrogen flow via line 47, the subcooling countercurrent 16, and the throttle valve 48 is placed on the head of the high pressure column 8.
Eine Leitung 44, die durch eine Passagengruppe des Hauptwärmetauschers 20 ("Zwischenpassage") führt, wird in dem Ausführungsbeispiel als Pendelleitung betrieben. A conduit 44 leading through a passage group of the main heat exchanger 20 ("intermediate passage") is operated as a shuttle in the embodiment.
In einer ersten Betriebsweise wird ein vierter Teilstrom des Kreislaufstickstoffstroms unter einem unteren Zwischendruck (P1-GAN) von der ersten Zwischenstufe des Kreislaufverdichters 22 abgezogen, in der Zwischendruckpassage des In a first mode of operation, a fourth substream of the circulating nitrogen stream is withdrawn below the lower intermediate pressure (P1-GAN) from the first intermediate stage of the cycle compressor 22, in the intermediate pressure passage of the cycle
Hauptwärmetauschers abgekühlt und über die - in diesem Fall nach rechts Main heat exchanger cooled and over - in this case to the right
durchströmte - Pendelleitung mit dem arbeitsleistend entspannten Turbinenstrom 42 stromaufwärts des ersten Kondensator- Verdampfers 10 vermischt. Dies ist flowed through - commutation line with the work-performing relaxed turbine stream 42 upstream of the first condenser evaporator 10 is mixed. This is
insbesondere dann günstig, wenn relativ wenig Kälte benötigt wird und deshalb der Turbinenstrom für die Kolonnehheizung nicht ausreicht. especially favorable when relatively little cold is needed and therefore the turbine flow is not sufficient for the Kolonnehheizung.
Umgekehrt kann in einer zweiten Betriebsweise ein Teil des arbeitsleistend Conversely, in a second mode of operation, part of the work can be done
entspannten Turbinenstroms in der Pendelleitung nach links geführt, in der relaxed turbine flow in the pendulum line led to the left, in the
Zwischendruckpassage des Hauptwärmetauschers angewärmt und dem Intermediate pressure passage of the main heat exchanger warmed and the
Kreislaufverdichter 22 stromaufwärts der zweiten Stufe 25 wieder zugeführt werden. Dies ist vor Allem dann vorteilhaft, wenn viel Kälte erzeugt wird und der Turbinenstrom damit zu groß für die Beheizung des ersten Kondensator-Verdampfers ist. Circulation compressor 22 upstream of the second stage 25 are fed again. This is especially advantageous when a lot of cold is generated and the turbine flow is thus too large for the heating of the first condenser-evaporator.
Das Verfahren von Figur 2 unterscheidet sich dadurch von demjenigen der Figur 1 , dass die arbeitsleistende Entspannung 41 einen höheren Austrittsdruck aufweist. The method of Figure 2 differs from that of Figure 1 that the work-performing expansion 41 has a higher outlet pressure.
Dieser liegt auf einem Niveau von ca. 12 bar, das hier am Austritt der zweiten Stufe 25 des Kreislaufverdichters 22 anliegt (P2-GAN). Dieser Druck reicht aus, um den  This is at a level of about 12 bar, which here at the outlet of the second stage 25 of the cycle compressor 22 is applied (P2-GAN). This pressure is enough to the
Sumpfverdampfer 209 der Hochdrucksäule 8 mit dem Strom 230 zu betreiben. Der "erste Teilstrom" zur Ausheizung des Sumpfverdampfers 209 ist also teilweise identisch mit dem Turbinenstrom, dem "dritten Teilstrom". Die Pendelleitung 244 befindet sich ebenfalls auf dem höheren Druckniveau (P2-GAN). Als Heizmittel für den Zwischenverdampfer 210 wird hier ein Teilstrom 246 des Kreislaufstickstoffstroms verwendet, der stromaufwärts der zweiten Stufe 25 des Kreislaufverdichters 22 abgezweigt wird. Bottom evaporator 209 of the high-pressure column 8 to operate with the current 230. The "first partial flow" for heating the bottom evaporator 209 is therefore partially identical to the turbine flow, the "third partial flow". The shuttle line 244 is also at the higher pressure level (P2-GAN). As a heating means for the intermediate evaporator 210, a partial stream 246 of the circulating nitrogen stream is used, which is branched off upstream of the second stage 25 of the cycle compressor 22.
Bei dem Ausführungsbeispiel der Figur 3 weist die Hochdrucksäule nur einen einzigen Kondensator-Verdampfer auf, den Sumpfverdampfer 209. Gegenüber Figur 2 wurde der Zwischenverdampfer weggelassen. Dadurch kann auch der Kreislaufverdichter 322 eine Stufe weniger als in Figur 2 aufweisen. In the embodiment of Figure 3, the high-pressure column only a single condenser-evaporator, the bottom evaporator 209. Compared with Figure 2, the intermediate evaporator has been omitted. As a result, the cycle compressor 322 can also have one stage less than in FIG.
Figur 4 zeigt eine Abwandlung von Figur 3. Hier wird nicht der Turbinenstrom ("dritter Teilstrom") 440 durch den an die Turbine 41 gekoppelten Nachverdichter geschickt, sondern der "Hochdruck-Prozessstrom" 434, der anschließend im FIG. 4 shows a modification of FIG. 3. Here, the turbine stream ("third partial stream") 440 is not sent through the secondary compressor coupled to the turbine 41, but instead the "high-pressure process stream" 434, which subsequently flows into the
Hauptwärmetauscher 20 zur (Pseudo-)Verdampfung des Sauerstoffprodukts eingesetzt wird. Sowohl der erste als auch der dritte Teilstrom stammen hier vom Austritt der Endstufe des Kreislaufverdichters 322 (Druckniveau P4-GAN). Main heat exchanger 20 for (pseudo) evaporation of the oxygen product is used. Both the first and the third partial flow come here from the outlet of the final stage of the cycle compressor 322 (pressure level P4-GAN).
Alternativ kann in den Figuren 1 bis 3 statt der Turbinen-Nachverdichter-Kombination 41/566 auch eine Generatorturbine eingesetzt werden. Alternatively, in FIGS. 1 to 3, instead of the turbine / compressor combination 41/566, a generator turbine can also be used.
In Figur 5 ist der Kreislaufverdichter 322 wie in den Figuren 3 und 4 ausgebildet, wobei er lediglich zwei Stufen 23, 25 aufweisen kann. Ansonsten ähnelt das hier dargestellte Verfahren mehr demjenigen von Figur 1 , insbesondere weist die Hochdrucksäule 8 einen Zwischenverdampfer 10 auf. In der ersten Stufe 23 des Kreislaufverdichters 22 wird der Kreislaufstickstoffstrom auf einen Zwischendruck von ca. 9 bar und in der zweiten Stufe 25 weiter auf einen oberen Kreislaufdruck von bis zu 16 bar verdichtet. Soweit den. Stickstoff unter dem oberen Kreislaufdruck nicht über Leitung 29 als Druckstickstoffprodukt abgezogen wird, dient er hier ausschließlich als "erster Teilstrom" zur Ausheizung des Sumpfverdampfers 9. In Figure 5, the cycle compressor 322 is formed as in Figures 3 and 4, wherein it may have only two stages 23, 25. Otherwise, the method illustrated here more closely resembles that of FIG. 1; in particular, the high-pressure column 8 has an intermediate evaporator 10. In the first stage 23 of the cycle compressor 22, the circulating nitrogen stream is compressed to an intermediate pressure of about 9 bar and in the second stage 25 further to an upper circuit pressure of up to 16 bar. As far as the. Nitrogen under the upper circuit pressure is not withdrawn via line 29 as pressure nitrogen product, he serves here exclusively as a "first partial flow" for heating the bottom evaporator. 9
Die für das Verfahren benötigte Kälte wird durch arbeitsleistende Entspannung 541 eines Turbinenstroms 540 erzeugt, der in dem Beispiel durch Stickstoff gebildet wird, der er kommt von einem Stickstoffverdichter (zum Beispiel einem nicht dargestellten separaten Verdichter oder von einer zusätzlichen Stufe am The refrigeration needed for the process is generated by work-in-progress expansion 541 of turbine flow 540, which in the example is nitrogen, which comes from a nitrogen compressor (for example, a separate compressor, not shown, or from an additional stage at
Stickstoffkreislaufverdichter). Der Austrittsstrom 542 stromabwärts der  Nitrogen cycle compressor). The exit stream 542 downstream of the
arbeitsleistenden Entspannung 541 wird mit einem der Stickstoffströme auf einem der Druckniveaus PGAN, P1 GAN oder P2GAN vermischt. Die in der Expansionsturbine 41 erzeigt mechanische Leistung Pturb wird ins Warme abgegeben, insbesondere an einen Verdichter, einen Generator oder eine dissipative Bremse. Work-performing expansion 541 is mixed with one of the nitrogen streams at one of the pressure levels PGAN, P1 GAN or P2GAN. The mechanical power Pturb generated in the expansion turbine 41 is released into heat, in particular to a compressor, a generator or a dissipative brake.
Als Hochdruck-Prozessstrom, der im Hauptwärmetauscher die Wärme für die As a high-pressure process stream, the heat in the main heat exchanger for the
(Pseudo-)Verdampfung des flüssigen Drucksauerstoffs liefert, wird in dem Beispiel ein Stickstoffstrom 534 eingesetzt, der unter einem geeigneten Druck steht und von einem Stickstoffverdichter kommt (zum Beispiel einem nicht dargestellten separaten (Pseudo-) evaporation of the liquid pressure oxygen, in the example, a nitrogen flow 534 is used, which is under a suitable pressure and comes from a nitrogen compressor (for example, a separate, not shown
Verdichter oder von einer zusätzlichen Stufe am Stickstoffkreislaufverdichter). Der Stickstoffstrom 34 kann grundsätzlich auch von jeder anderen Druckstickstoffquelle, also den Druckniveaus PGAN, P1 -GAN oder P2-GAN stammen. Er kann auf jedes geeignete vorhandene Druckniveau PGAN oder P1 -GAN entspannt und dann dem entsprechenden Kreislauf- oder Druckproduktstrom hinzugefügt werden. Alternativ führt die arbeitsleistende Entspannung führt auf Atmosphärenniveau und der entspannte Turbinenstrom wird schließlich - nach Anwärmung im Hauptwärmetauscher 20 - drucklos abgegeben. Compressor or from an additional stage on the nitrogen cycle compressor). In principle, the nitrogen stream 34 can also originate from any other compressed nitrogen source, that is, the pressure levels PGAN, P1-GAN or P2-GAN. It may be depressurized to any suitable existing pressure level PGAN or P1 -GAN and then added to the appropriate cycle or pressurized product stream. Alternatively, the work-performing relaxation leads to atmospheric level and the relaxed turbine stream is finally released - after heating in the main heat exchanger 20 - without pressure.
Der kalte Hochdruck-Prozessstrom 535 wird wie in Figur 1 geführt. The cold high pressure process stream 535 is performed as in FIG.
Das Verfahren von Figur 6 unterscheidet sich von demjenigen der Figur 1 dadurch, dass der Austrittsdruck der arbeitsleistenden Entspannung 641 (Leitung 642) auf dem Niveau PGAN des Betriebsdrucks der Hochdrucksäule 8 liegt. Dadurch kann entsprechend mehr Kälte für die Produktverflüssigung gewonnen werden. The method of Figure 6 differs from that of Figure 1 in that the outlet pressure of the work-performing expansion 641 (line 642) on the Level PGAN the operating pressure of the high-pressure column 8 is located. As a result, correspondingly more cold can be obtained for product liquefaction.
Der Turbinenstrom 540 wird durch mindestens einen Teil eines der folgenden drei Ströme gebildet: The turbine stream 540 is formed by at least a portion of one of the following three streams:
- 29 (P2-GAN) von der Endstufe des Kreislaufverdichters 28 - 29 (P2-GAN) from the final stage of the cycle compressor 28
- 565 (P3-GAN) von einer Zwischenstufe des Produktverdichters 560  - 565 (P3-GAN) from an intermediate stage of the product compressor 560
- 564 (P4-GAN) von der Endstufe des Produktverdichters 560  - 564 (P4-GAN) from the final stage of the product compressor 560
Der Turbinenstrom wird arbeitsleistend auf etwa den Betriebsdruck der Drucksäule 8 entspannt. Der entspannte Turbinenstrom 642 wird schließlich dem The turbine flow is expanded to approximately the operating pressure of the pressure column 8 in order to work. The relaxed turbine stream 642 eventually becomes the
Kreislaufstickstoffstrom 19 zugemischt, der vom Kopf der Drucksäule 8 kommt. Die Turbinenleistung wird hier an einen Stickstoff-Nachverdichter 666 abgegeben, der den Druck des Turbinenstroms weiter erhöht. Circulating nitrogen stream 19 added, which comes from the head of the pressure column 8. The turbine power is delivered here to a nitrogen booster 666, which further increases the pressure of the turbine flow.
In dem Prozess von Figur 7 wird der Hochdruck-Prozessstrom 734 nicht durch Stickstoff sondernd durch einen Teilstrom der Einsatzluft gebildet. Dieser kann beispielsweise stromabwärts einer nicht dargestellten Reinigungseinrichtung abgezweigt und in einem Nachverdichter auf den benötigten Druck gebracht werden, der bis zu 90 bar betragen kann. (Hauptluftverdichter, Reinigungseinrichtung, In the process of FIG. 7, the high pressure process stream 734 is not formed by nitrogen and by a substream of the feed air. This can, for example, branched off downstream of a cleaning device, not shown, and brought to the required pressure in a booster, which can be up to 90 bar. (Main air compressor, cleaning device,
Abzweigung und Nachverdichter sind in Figur 7 nicht dargestellt.) Analog zu den Figuren 1 bis 6 wird der Hochdruck-Prozessstrom 734 im Hauptwärmetauscher abgekühlt und (pseudo-)verflüssigt, im Drosselventil 736 auf Hochdrucksäulendruck entspannt und schließlich über Leitung 737 an einer geeigneten Zwischenstelle in die Hochdrucksäule 8 eingespeist. Ebenso analog zu den Figuren 1 bis 6 kann die Entspannung auf Drucksäulendruck auch arbeitsleistend in einer Flüssigturbine 738 durchgeführt werden, die vorzugsweise durch einen Generator 739 gebremst wird. Die in Figur 7 dargestellte Verwendung von Luft als Hochdruck-Prozessstrom kann auch auf die Prozessvarianten der Figuren 1 bis 6 angewendet werden. Branch and re-compressors are not shown in FIG. 7. Analogously to FIGS. 1 to 6, the high-pressure process stream 734 in the main heat exchanger is cooled and (pseudo-) liquefied, expanded in the throttle valve 736 to high-pressure column pressure and finally via line 737 to a suitable intermediate point in the high-pressure column 8 fed. Similarly to FIGS. 1 to 6, the expansion to the pressure column pressure can also be carried out in a work-performing manner in a liquid turbine 738, which is preferably braked by a generator 739. The use of air as a high-pressure process stream shown in FIG. 7 can also be applied to the process variants of FIGS. 1 to 6.
Der Turbinenstrom 840 für die arbeitsleistende Entspannung 841 wird in Figur 7 nicht durch Stickstoff, sondern durch einen anderen Teil der Einsatzluft gebildet, hier insbesondere den Rest der Einsatzluft, der nicht als Hochdruck-Prozessstrom 734 eingesetzt wird. Hierbei wird die Gesamtluft im Luftverdichter auf einen deutlich über Hochdrucksäulendruck liegenden Druck von bis zu 90 bar verdichtet und anschließend auf den Turbinenstrom 840 und den Hochdruck-Prozessstrom 734 aufgeteilt. The turbine stream 840 for the work-performing expansion 841 is formed in FIG. 7 not by nitrogen but by another part of the feed air, here in particular the remainder of the feed air which is not used as the high-pressure process stream 734. Here, the total air in the air compressor to a significantly above High-pressure column pressure of up to 90 bar compressed and then divided into the turbine stream 840 and the high-pressure process stream 734.
(Alternativ können der Turbinenstrom 840 und/oder der Hochdruck-Prozessstrom (Alternatively, the turbine stream 840 and / or the high pressure process stream
c-■ c- ■
separat weiter nachverdichtet werden.) Der entspannte Turbinenstrom wird an einer geeigneten Zwischenstelle in die Hochdrucksäule 8 eingeleitet. be further recompressed separately.) The expanded turbine stream is introduced at a suitable intermediate point in the high-pressure column 8.
Die zweite in Figur 7 dargestellte Abwandlung (Luftturbine statt Stickstoffturbine) kann ebenfalls bei den Verfahren der Figuren 1 bis 6), alleine oder in Kombination mit der Verwendung von Luft als Hochdruck-Prozessstrom. The second modification shown in FIG. 7 (air turbine instead of nitrogen turbine) can also be used in the methods of FIGS. 1 to 6), alone or in combination with the use of air as a high-pressure process stream.
Das Verfahren von Figur 8 nutzt ebenfalls Einsatzluft als Hochdruck-Prozessstrom 734 und als Turbinenstrom 840. Die Gesamtluft wird in einem Hauptluftverdichter auf etwa Hochdrucksäulendruck verdichtet und anschließend in einer Reinigungseinrichtung gereinigt (beides ist in der Zeichnung nicht dargestellt). Die auf Hochdrucksäulendruck verdichtete und gereinigte Luft 801 wird in insgesamt drei Teilströme aufgeteilt, den Hochdruck-Prozessstrom 734, den Turbinenstrom 840 und außerdem in einen The method of Figure 8 also uses feed air as high pressure process stream 734 and turbine stream 840. The total air is compressed in a main air compressor to about high pressure column pressure and then cleaned in a purifier (both not shown in the drawing). The compressed at high pressure column pressure and purified air 801 is divided into a total of three sub-streams, the high-pressure process stream 734, the turbine stream 840 and also in a
Direktluftstrom 802, 806, der ohne weitere druckverändemde Maßnahmen über Leitung 807 gasförmig in die Hochdrucksäule 8 eingeleitet wird. Der Hochdruck- Prozessstrom und der Turbinenstrom werden gemeinsam über Leitung 802 zu einem ersten extern angetriebenen Nachverdichter 803 mit Nachkühler 804 geführt und anschließend weiter verzweigt. Während der Hochdruck-Prozessstrom in einem weiteren extern angetriebenen Nachverdichter 808 mit Nachkühler 809 auf einen besonders hohen Druck weiter verdichtet wird, strömt der Turbinenstrom durch einen Nachverdichter 810, der von der Entspannungsmaschine 841 angetrieben wird, die durch einen Turboexpander gebildet wird und mechanisch über eine gemeinsame Welle mit dem Nachverdichter 810 gekoppelt ist. Der Nachverdichter 810 weist ebenfalls einen Nachkühler 81 1 auf. Direct air stream 802, 806, which is introduced into the high-pressure column 8 via line 807 without further pressure-changing measures. The high-pressure process stream and the turbine stream are fed together via line 802 to a first externally driven booster 803 with aftercooler 804 and then further branched. While the high-pressure process stream is further compressed to a particularly high pressure in a further externally driven booster 808 with aftercooler 809, the turbine stream flows through a booster 810 which is driven by the expansion machine 841, which is formed by a turboexpander and mechanically via a common shaft is coupled to the booster 810. The after-compressor 810 also has an after-cooler 81 1.
Ein Teil 865 der über Leitung 737 flüssig in die Hochdrucksäule 8 eingeleiteten Luft wird gleich wieder aus der Hochdrucksäule entnommen und analog zu Strom 465 in Figur 1 der Niederdrucksäule 460 an einer Zwischenstelle zugeleitet. Part 865 of the liquid introduced via line 737 into the high-pressure column 8 is immediately taken out of the high-pressure column and, analogously to stream 465 in FIG. 1, fed to the low-pressure column 460 at an intermediate point.
Der "erste Teilstrom" des Kreislaufstickstoffstroms wird hier durch den Strom 845/846 gebildet, der zwischen den beiden Stufen 23, 25 des Kreislaufverdichters 22 entnommen und zum Sumpfverdampfer 9 der Hochdrucksäule 8 geführt wird. Über die Leitungen ist die Niederdrucksäule 460 mit einer konventionellen Argongewinnung verbunden. Die Details der Argongewinnung mit Rohargonsäule sind hier nicht dargestellt, das sie dem Fachmann geläufig sind. The "first partial stream" of the circulating nitrogen stream is formed here by the stream 845/846, which is taken off between the two stages 23, 25 of the cycle compressor 22 and led to the bottom evaporator 9 of the high-pressure column 8. Via the lines, the low-pressure column 460 is connected to a conventional argon recovery. The details of argon recovery with crude argon column are not shown here, which they are familiar to the expert.
In einer Alternative wird in Figur 8 statt des Stroms 845 ein anderer. In an alternative, in Figure 8 instead of the current 845 another.
Druckstickstoffstrom als Heizmedium für den Sumpfverdampfer 9 der Hochdrucksäule 8 genutzt. Außerdem wird ein zusätzlicher Druckstickstoffproduktstrom 853 durch Innenverdichtung gewonnen, indem ein Teil 850 des im Hauptkondensator 461 gewonnenen flüssigen Stickstoffs in einer Pumpe 851 flüssig auf einen hohen Druck gebracht, über Leitung 852 zum Hauptwärmetauscher 20 geführt und dort verdampft beziehungsweise pseudo-verdampft und auf Umgebungstemperatur angewärmt wird. Pressure nitrogen stream used as a heating medium for the bottom evaporator 9 of the high-pressure column 8. In addition, an additional pressurized nitrogen product stream 853 is recovered by internal compression by liquidly pressurizing a portion 850 of the liquid nitrogen recovered in the main condenser 461 to a high pressure in a pump 851, passing it to the main heat exchanger 20 via line 852 and evaporating or pseudo-evaporating and warming to ambient temperature becomes.
Figur 9 entspricht weitgehend Figur 8, weist aber keine Stickstoff-Innenverdichtung auf. Hier sind die in Figur 8 nicht dargestellten Unterkühlungs-Gegenströmer gezeigt. Das Verfahren unterscheidet sich durch eine zusätzliche Mitteldrucksäule 900, die unter einem Betriebsdruck betrieben wird, der zwischen den Betriebsdrücke von Niederdrucksäule 760 und Hochdrucksäule 8 liegt. Die Sumpfflüssigkeit 462 Figure 9 corresponds largely to Figure 8, but has no nitrogen internal compression. Here, the subcooling countercurrents, not shown in Figure 8 are shown. The method differs by an additional medium-pressure column 900, which is operated under an operating pressure which is between the operating pressures of low-pressure column 760 and high-pressure column 8. The bottom liquid 462
("sauerstoffangereicherte Flüssigkeit") aus der Hochdrucksäule 8 beziehungsweise von der Verflüssigungsseite ihres Sumpfverdampfers 9 wird hier nicht direkt, sondern indirekt der Niederdrucksäule 460 zugeleitet. Sie wird nach Unterkühlung 16 zunächst über Leitung 964 der Mitteldrucksäule 900 und dort weiter vorzerlegt. Auch die flüssige Luft 865 wird im Gegensatz zu den vorigen Ausführungsbeispielen hier nicht der Niederdrucksäule 460 zugeleitet, sondern nach Durchströmen des Unterkühlungs- Gegenströmers 16 und eines Drosselventils über Leitung 965 der Mitteldrucksäule 900 an einer Zwischenstelle zugeleitet. (Ein Teil kann über Leitung 965 wieder entnommen und wie in Figur 1 über 466 und 467 in die Niederdrucksäule 460 eingespeist werden.) ("oxygen-enriched liquid") from the high-pressure column 8 and from the liquefaction side of their bottom evaporator 9 is here not directly, but indirectly fed to the low-pressure column 460. After supercooling 16, it is first preceded by line 964 of the medium-pressure column 900 and further there. The liquid air 865 is not supplied to the low-pressure column 460 here in contrast to the previous embodiments, but after flowing through the supercooling countercurrent 16 and a throttle valve via line 965 of the medium-pressure column 900 fed to an intermediate point. (A portion may be withdrawn via line 965 and fed into low pressure column 460 as shown in Figure 1 via 466 and 467.)
Die Mitteldrucksäule 900 weist zwei Kondensator-Verdampfer auf, einen The medium-pressure column 900 has two condenser evaporators, a
Mitteldrucksäulen-Sumpfverdampfer 901 und einen Mitteldrucksäulen-Kopfkondensator 902. Der Mitteldrucksäulen-Sumpfverdampfer 901 wird mittels eines Teilstroms 903 des Kopfstickstoffs der Hochdrucksäule 8 beheizt. Der dabei kondensierte Stickstoff 904 wird als Rücklaufflüssigkeit auf den Kopf der Mitteldrucksäule 900 aufgegeben. Der Mitteldrucksäulen-Kopfkondensator 902 wird mit der Sumpfflüssigkeit 905 der Mitteldrucksäule 900 beziehungsweise von der Verflüssigungsseite deren Sumpfverdampfers 901 gekühlt. Der dabei erzeugte Dampf 906 und der flüssig verbliebene Anteil 907 werden in die Niederdrucksäule 460 eingeleitet. Der Teil 908 des im Mitteldrucksäulen-Kopfkondensator 902 gewonnenen flüssigen Stickstoffs, der nicht als Rücklaufflüssigkeit in die Mitteldrucksäule 900 eingeleitet wird, kann nach Unterkühlung 16 als zusätzliche Rücklaufflüssigkeit 909 für die Niederdrucksäule 460 genutzt werden. Medium-pressure column bottom evaporator 901 and a medium-pressure column overhead condenser 902. The medium-pressure column bottom evaporator 901 is heated by means of a partial flow 903 of the top nitrogen of the high-pressure column 8. The thereby condensed nitrogen 904 is charged as reflux liquid to the head of the medium-pressure column 900. The medium-pressure column head condenser 902 is connected to the bottom liquid 905 of the medium-pressure column 900 or from the liquefaction side thereof Bottom evaporator 901 cooled. The generated vapor 906 and the liquid remaining portion 907 are introduced into the low-pressure column 460. The portion 908 of the liquid nitrogen recovered in the medium-pressure column overhead condenser 902, which is not introduced into the medium-pressure column 900 as reflux liquid, can be used after subcooling 16 as additional reflux liquid 909 for the low-pressure column 460.

Claims

Patentansprüche claims
Verfahren zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Process for the production of pressure oxygen and pressure nitrogen by
Tieftemperaturzerlegung von Luft in einem Destilliersäulen-System zur Stickstoff- Sauerstoff-Trennung, das mindestens eine Hochdrucksäule (8) mit Cryogenic separation of air in a distillation column system for nitrogen-oxygen separation, the at least one high-pressure column (8) with
Sumpfverdampfer (9, 209) und eine Niederdrucksäule (460) aufweist, wobei die Niederdrucksäule (460) über einen als Kondensator-Verdampfer ausgebildeten Hauptkondensator (461) mit der Hochdrucksäule (8) in wärmetauschender Verbindung steht, wobei bei dem Verfahren Sump evaporator (9, 209) and a low pressure column (460), wherein the low pressure column (460) via a designed as a condenser-evaporator main condenser (461) with the high-pressure column (8) in heat exchanging connection, wherein the method
- Einsatzluft in einem Luftverdichter (2) verdichtet wird,  - compressed air in an air compressor (2) is compressed,
- die verdichtete Einsatzluft (6, 734, 802, 840) in einem Hauptwärmetauscher (20) abgekühlt und mindestens teilweise in die Hochdrucksäule (8) eingeleitet wird,  the compressed feed air (6, 734, 802, 840) is cooled in a main heat exchanger (20) and introduced at least partially into the high-pressure column (8),
- eine sauerstoffangereicherte Flüssigkeit (462, 465) aus der Hochdrucksäule (8) entnommen und der Niederdrucksäule (460) an einer ersten Zwischenstelle zugeführt (464, 467, 906) wird,  an oxygen-enriched liquid (462, 465) is taken from the high-pressure column (8) and fed to the low-pressure column (460) at a first intermediate point (464, 467, 906),
- eine stickstoffangereicherte Flüssigkeit (468, 470) aus der Hochdrucksäule (8) und/oder dem Hauptkondensator (461) entnommen und auf den Kopf der Niederdrucksäule (460) aufgegeben wird,  a nitrogen-enriched liquid (468, 470) is taken from the high-pressure column (8) and / or the main condenser (461) and applied to the top of the low-pressure column (460),
- ein flüssiger Sauerstoffstrom (11 , 12) aus dem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung entnommen, in flüssigem Zustand auf einen erhöhten Druck gebracht (13), unter diesem erhöhten Druck in den  - A liquid oxygen stream (11, 12) taken from the distillation column system for nitrogen-oxygen separation, brought in a liquid state to an elevated pressure (13), under this increased pressure in the
Hauptwärmetauscher (20) eingeleitet, im Hauptwärmetauscher (20) verdampft oder pseudo-verdampft und auf etwa Umgebungstemperatur angewärmt und schließlich als gasförmiges Drucksauerstoffprodukt (14) gewonnen wird, Main heat exchanger (20) is introduced, evaporated in the main heat exchanger (20) or pseudo-evaporated and heated to about ambient temperature and finally recovered as a gaseous pressure oxygen product (14),
- ein Hochdruck-Prozessstrom (34, 734) in dem Hauptwärmetauscher (20) in indirekten Wärmeaustausch mit dem Sauerstoffstrom gebracht und - A high pressure process stream (34, 734) in the main heat exchanger (20) brought in indirect heat exchange with the oxygen flow and
anschließend entspannt (36, 38; 736, 738) wird, wobei der entspannte  subsequently relaxed (36, 38; 736, 738), with the relaxed one
Hochdruckstrom (37, 737) mindestens teilweise in flüssigem Zustand in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung eingeleitet wird, High-pressure stream (37, 737) is at least partially introduced in the liquid state in the distillation column system for nitrogen-oxygen separation,
- ein gasförmiger Kreislaufstickstoffstrom (18, 19) aus der Hochdrucksäule abgezogen wird und mindestens zum Teil (21) in einem Kreislaufverdichter (22) verdichtet wird, - A gaseous circulating nitrogen stream (18, 19) is withdrawn from the high-pressure column and at least partially (21) is compressed in a cycle compressor (22),
- ein erster Teilstrom (45, 46; 244, 242, 230; 845, 846) des  a first substream (45, 46, 244, 242, 230, 845, 846) of the
Kreislauf stickstoffstroms aus dem Kreislaufverdichter (22, 322) entnommen, in dem Hauptwärmetauscher (20) abgekühlt, in dem Sumpfverdampfer (9, 209) der Hochdrucksäule (8) in indirektem Wärmeaustausch mit der Sumpfflüssigkeit der Hochdrucksäule (8) mindestens teilweise verflüssigt und in das Circuit nitrogen flow removed from the cycle compressor (22, 322), in the main heat exchanger (20) cooled in the sump evaporator (9, 209) of the high pressure column (8) in indirect heat exchange with the bottom liquid of the high pressure column (8) at least partially liquefied and in the
Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung zurückgeleitet wird und bei dem  Distillation column system is returned to the nitrogen-oxygen separation and in the
- ein zweiter Teilstrom des Kreislaufstickstoffstroms stromaufwärts und/oder stromabwärts des Kreislaufverdichters und/oder von einer Zwischenstufe des Kreislaufverdichters unter einem Produktdruck (P, P1 , P2, P3, P4) abgezweigt und als Druckstickstoffprodukt (27, 29, 53, 564, 565) gewonnen wird,  a second substream of the circulating nitrogen stream upstream and / or downstream of the cycle compressor and / or from an intermediate stage of the cycle compressor is diverted under a product pressure (P, P1, P2, P3, P4) and used as compressed nitrogen product (27, 29, 53, 564, 565) is won,
dadurch gekennzeichnet, dass characterized in that
- der Kreislaufverdichter (22, 322) als warmer Verdichter ausgebildet ist und  - The cycle compressor (22, 322) is designed as a hot compressor and
mittels externer Energie angetrieben wird.  powered by external energy.
Verfahren nach Anspruch 1 , dadurch gekennzeichnet, dass eine A method according to claim 1, characterized in that a
Gesamtdruckstickstoffproduktmenge (PN) gewonnen wird, die durch die Summe der Mengenströme gebildet wird, die stromaufwärts und/oder stromabwärts des Kreislaufverdichters und/oder von einer Zwischenstufe des Kreislaufverdichters unter einem Produktdruck (P, P1 , P2, P3, P4) aus dem Kreislaufstickstoffstrom abgezweigt und als Druckstickstoffprodukt (27, 29, 53, 564, 565) gewonnen werden, wobei in einem ersten Lastfall Total pressure nitrogen product quantity (PN) formed by the sum of the flow rates branched upstream and / or downstream of the cycle compressor and / or from an intermediate stage of the cycle compressor under a product pressure (P, P1, P2, P3, P4) from the cycle nitrogen flow and obtained as pressurized nitrogen product (27, 29, 53, 564, 565), wherein in a first load case
- eine erste Gesamtdruckstickstoffproduktmenge P 1 gewonnen wird,  a first total pressure nitrogen product quantity P 1 is obtained,
- der erste Teilstrom in einer ersten Teilstrommenge TS1 durch den  - The first partial flow in a first partial flow TS1 by the
Sumpfverdampfer (9, 209) der Hochdrucksäule (8) geführt wird und  Bottom evaporator (9, 209) of the high-pressure column (8) is guided and
- die Einsatzluft in einer ersten Einsatzluftmenge EL1 in den Luftverdichter (2) eingeleitet wird,  the feed air is introduced into the air compressor (2) in a first quantity of feed air EL1,
und wobei in einem zweiten Lastfall and wherein in a second load case
- eine zweite, höhere Gesamtdruckstickstoffproduktmenge PN2 gewonnen wird, a second, higher total pressure nitrogen product quantity PN2 is obtained,
PN2 > PN1 , PN2> PN1,
- der erste Teilstrom in einer zweiten, höheren Teilstrommenge TS2 durch den - The first partial flow in a second, higher partial flow TS2 by the
Sumpfverdampfer (9, 209) der Hochdrucksäule (8) geführt wird, TS2 > TS1 , undSump evaporator (9, 209) of the high pressure column (8) is performed, TS2> TS1, and
- die Einsatzluft in einer zweiten Einsatzluftmenge EL2 in den Luftverdichter (2) eingeleitet wird, wobei die zweite Einsatzluftmenge EL2 gleich der ersten Einsatzluftmenge EL1 oder nur unwesentlich höher ist, wobei gilt - The feed air is introduced in a second amount of feed air EL2 in the air compressor (2), wherein the second feed air quantity EL2 equal to the first feed air quantity EL1 or only slightly higher, where applicable
(EL2 - EL1)/EL1 < 0,2 · (PN2 - PN1)/PN1 . Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass ein dritter Teilstrom (30) des Kreislaufstickstoffstroms als Turbinenstrom (40; 242) aus dem Kreislaufverdichter (22, 322) entnommen, arbeitsleistend entspannt (41) und mindestens teilweise in das Destilliersäulen-System zur Stickstoff-Sauerstoff- Trennung eingeleitet wird. (EL2 - EL1) / EL1 <0.2 · (PN2 - PN1) / PN1. A method according to claim 1 or 2, characterized in that a third partial stream (30) of the circulating nitrogen stream as a turbine stream (40; 242) taken from the cycle compressor (22, 322), working expanded (41) and at least partially in the distillation column system for Nitrogen-oxygen separation is initiated.
Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass eine Flüssigfraktion aus der Hochdrucksäule (8) unter dem Betriebsdruck der Method according to one of claims 1 to 3, characterized in that a liquid fraction from the high-pressure column (8) under the operating pressure of
Hochdrucksäule in einen Kondensator- Verdampfer (9, 10) eingeleitet und dort in indirektem Wärmeaustausch mit mindestens einem Teil des arbeitsleistend entspannten Turbinenstroms mindestens teilweise verdampft wird, wobei der dabei erzeugte Dampf mindestens teilweise in die Hochdrucksäule (8) zurückgeleitet wird. High-pressure column in a condenser-evaporator (9, 10) introduced and there is at least partially evaporated in indirect heat exchange with at least a portion of the work-performing relaxed turbine flow, wherein the steam generated thereby at least partially in the high-pressure column (8) is returned.
Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass die Flüssigfraktion vom Sumpf der Hochdrucksäule (8) oder von einer Zwischenstelle der A method according to claim 4, characterized in that the liquid fraction from the bottom of the high-pressure column (8) or from an intermediate point of the
Hochdrucksäule (8) abgezogen wird. High pressure column (8) is withdrawn.
Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass der Kreislaufverdichter (22, 322) mehrstufig ausgebildet ist und der dritte Teilstrom des Kreislaufstickstoffstroms unter einem oberen Zwischendruck (P2, P3, P4) von einer Zwischenstufe des Kreislaufverdichters abgezogen und anschließend der arbeitsleistenden Entspannung zugeführt wird. Method according to one of claims 1 to 5, characterized in that the cycle compressor (22, 322) is formed in multiple stages and the third partial flow of the circulating nitrogen stream under an upper intermediate pressure (P2, P3, P4) subtracted from an intermediate stage of the cycle compressor and then the work-performing Relaxation is supplied.
Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass ein Teilstrom des Kreislaufstickstoffstroms unter einem hohen Druck (P4) aus dem A method according to claim 6, characterized in that a partial flow of the circulating nitrogen stream under a high pressure (P4) from the
Kreislaufverdichter abgezogen wird, der höher als der Zwischendruck (P3) ist, und anschließend als Hochdruck-Prozessstrom (34) verwendet wird. Circulation compressor is withdrawn, which is higher than the intermediate pressure (P3), and then used as a high-pressure process stream (34).
Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass der Kreislaufverdichter mehrstufig ausgebildet ist und in einer ersten Betriebsweise ein vierter Teilstrom (45) des Kreislaufstickstoffstroms unter einem unteren Method according to one of claims 1 to 7, characterized in that the cycle compressor is designed in multiple stages and in a first mode of operation, a fourth partial stream (45) of the circulating nitrogen stream under a lower
Zwischendruck (P1-GAN, P2-GAN) von einer Zwischenstufe des Intermediate pressure (P1-GAN, P2-GAN) from an intermediate stage of the
Kreislaufverdichters abgezogen, in einer Zwischendruckpassage des Withdrawn circuit compressor, in an intermediate pressure passage of the
Hauptwärmetauschers abgekühlt und mit dem arbeitsleistend entspannten Turbinenstrom (42) stromaufwärts des Sumpfverdampfers (9) vermischt wird und das Gemisch den ersten Teilstrom (30) bildet.. Main heat exchanger cooled and with the work performing relaxed Turbine stream (42) upstream of the bottom evaporator (9) is mixed and the mixture forms the first part stream (30).
9. Verfahren nach Anspruch 8, dadurch gekennzeichnet, dass in einer zweiten 9. The method according to claim 8, characterized in that in a second
Betriebsweise ein Teil des arbeitsleistend entspannten Turbinenstroms (42) in der Operating mode, a part of the work done relaxed turbine flow (42) in the
Zwischendruckpassage des Hauptwärmetauschers angewärmt und dem Intermediate pressure passage of the main heat exchanger warmed and the
Kreislaufverdichter an einer Zwischenstufe zugeführt wird, wobei mindestens ein Teil des Restes des arbeitsleistend entspannten Turbinenstroms (42) den ersten Teilstrom (30) bildet.  Circular compressor is supplied to an intermediate stage, wherein at least a portion of the rest of the work-performing expanded turbine stream (42) forms the first partial stream (30).
10. Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, dass der flüssige Sauerstoffstrom (41 1 , 412) aus dem unteren Bereich der 10. The method according to any one of claims 1 to 9, characterized in that the liquid oxygen stream (41 1, 412) from the lower region of
Niederdrucksäule (460) entnommen wird. 1 1. Verfahren nach einem der Ansprüche 1 bis 10, dadurch gekennzeichnet, dass eine Zwischenflüssigkeit (465, 467), deren Sauerstoffgehalt zwischen demjenigen der sauerstoffangereicherten Flüssigkeit (462) und demjenigen der  Low pressure column (460) is removed. 11. The method according to any one of claims 1 to 10, characterized in that an intermediate liquid (465, 467), whose oxygen content between that of the oxygen-enriched liquid (462) and that of the
stickstoffangereicherten Flüssigkeit (468) liegt, aus der Hochdruckrucksäule (8) entnommen und der Niederdrucksäule (460) an einer zweiten Zwischenstelle zugeführt wird, die oberhalb der ersten Zwischenstelle angeordnet ist, wobei die Nitrogen-enriched liquid (468) is taken from the high-pressure pressure column (8) and the low-pressure column (460) is supplied at a second intermediate point, which is arranged above the first intermediate point, wherein the
Zwischenflüssigkeit (465) insbesondere in Höhe eines Zwischenverdampfers (10) der Hochdrucksäule (8) entnommen wird. Intermediate liquid (465), in particular at the level of an intermediate evaporator (10) of the high-pressure column (8) is removed.
12. Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch 12. Apparatus for recovering pressure oxygen and pressure nitrogen by
Tieftemperaturzerlegung von Luft mit  Cryogenic decomposition of air with
- einem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung, das  - A distillation column system for nitrogen-oxygen separation, the
mindestens eine Hochdrucksäule (8) und eine Niederdrucksäule (460) aufweist, wobei die Niederdrucksäule (460) über sowie einen als Kondensator- Verdampfer ausgebildeten Hauptkondensator (461), zur wärmetauschenden Verbindung von Niederdrucksäule (460) und Hochdrucksäule (8) aufweist, at least one high-pressure column (8) and one low-pressure column (460), the low-pressure column (460) having and a condenser-designed as the main evaporator (461), the heat exchange connection of low-pressure column (460) and high-pressure column (8),
- einem Luftverdichter (2) zum Verdichten von Einsatzluft, an air compressor (2) for compressing feed air,
- einem Hauptwärmetauscher (20) zum Abkühlen der verdichteten Einsatzluft (6, 734, 802, 840),  a main heat exchanger (20) for cooling the compressed feed air (6, 734, 802, 840),
- Mitteln zum Einleiten der abgekühlten Einsatzluft in die Hochdrucksäule (8), - Mitteln zum Entnehmen einer sauerstoffangereicherte Flüssigkeit (462, 465) aus der Hochdrucksäule (8) und zum Zuführen dieser Flüssigkeit (464, 467) oder einer daraus abgeleiteten Flüssigkeit (467, 906) zu der Niederdrucksäule (460) an einer ersten Zwischenstelle, Means for introducing the cooled feed air into the high-pressure column (8), - means for removing an oxygen-enriched liquid (462, 465) from the high-pressure column (8) and supplying this liquid (464, 467) or a liquid (467, 906) derived therefrom to the low-pressure column (460) at a first intermediate point,
- Mitteln zum Entnehmen einer stickstoffangereicherten Flüssigkeit (468, 470) aus der Hochdrucksäule (8) und/oder dem Hauptkondensator (461) und zum Aufgeben dieser Flüssigkeit auf den Kopf der Niederdrucksäule (460), - means for removing a nitrogen-enriched liquid (468, 470) from the high-pressure column (8) and / or the main condenser (461) and for applying this liquid to the top of the low-pressure column (460),
- Mitteln zum Entnehmen eines flüssigen Sauerstoffstroms (1 1 , 12, 41 1 , 412) aus dem Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung,  - means for removing a liquid oxygen stream (1 1, 12, 41 1, 412) from the distillation column system for nitrogen-oxygen separation,
- Mitteln um den Sauerstoffstrom in flüssigem Zustand auf einen erhöhten Druck zu bringen (13), unter diesem erhöhten Druck in den Hauptwärmetauscher (20) einzuleiten, im Hauptwärmetauscher (20) zu verdampfen oder - means to bring the oxygen flow in the liquid state to an elevated pressure (13), to initiate under this increased pressure in the main heat exchanger (20) to evaporate in the main heat exchanger (20) or
pseudozuverdampfen und auf etwa Umgebungstemperatur anzuwärmen und schließlich als gasförmiges Drucksauerstoffprodukt (14) abzuziehen,  pseudoevaporate and warm to about ambient temperature and finally withdraw as a gaseous pressure oxygen product (14),
- Mitteln, um einen Hochdruck-Prozessstrom (34, 734) in dem Means to a high-pressure process stream (34, 734) in the
Hauptwärmetauscher (20) in indirekten Wärmeaustausch mit dem  Main heat exchanger (20) in indirect heat exchange with the
Sauerstoffstrom zu bringen und anschließend zu entspannen (36, 38, 736, 738),  Bring oxygen flow and then relax (36, 38, 736, 738),
- Mitteln zum Einleiten des entspannten Hochdruck-Prozessstroms (37, 737) mindestens teilweise in flüssigem Zustand in das Destilliersäulen-System zur Means for introducing the expanded high-pressure process stream (37, 737) at least partially in the liquid state in the distillation column system for
Stickstoff-Sauerstoff-Trennung, Nitrogen-oxygen separation,
- Mitteln zum Abziehen eines gasförmigen Kreislaufstickstoffstroms (18, 19) aus der Hochdrucksäule,  Means for withdrawing a gaseous circulating nitrogen stream (18, 19) from the high-pressure column,
- einem Kreislaufverdichter (22, 322) zum Verdichten mindestens eines Teils (21) des Kreislaufstickstoffstroms,  a cycle compressor (22, 322) for compressing at least a portion (21) of the cycle nitrogen stream,
- Mitteln zum Entnehmen eines ersten Teilstroms (45, 46; 244, 242, 230; 845, 846) des Kreislaufstickstoffstroms aus dem Kreislaufverdichter (22, 322), zum Abkühlen des ersten Teilstroms in dem Hauptwärmetauscher (20), zum  - means for removing a first part stream (45, 46; 244, 242, 230; 845, 846) of the circulating nitrogen stream from the cycle compressor (22, 322), for cooling the first part stream in the main heat exchanger (20), to
Einleiten des ersten Teilstroms in den Sumpfverdampfer (9) der  Introducing the first partial flow in the bottom evaporator (9) of the
Hochdrucksäule (8) zwecks mindestens teilweisem Verflüssigen in indirektem High-pressure column (8) for the purpose of at least partial liquefaction in indirect
Wärmeaustausch mit der Sumpfflüssigkeit der Hochdrucksäule (8) und zum Zurückleiten des mindestens teilweise verflüssigten ersten Teilstroms in das Destilliersäulen-System zur Stickstoff-Sauerstoff-Trennung und mit Heat exchange with the bottom liquid of the high pressure column (8) and for returning the at least partially liquefied first part stream in the distillation column system for nitrogen-oxygen separation and with
- Mitteln zum Abzweigen eines zweites Teilstrom des Kreislaufstickstoffstroms stromaufwärts und/oder stromabwärts des Kreislaufverdichters und/oder von einer Zwischenstufe des Kreislaufverdichters unter einem Produktdruck (P, P1 , P2, P3, P4) und zum Abziehen als Druckstickstoffprodukt (27, 29, 53, 564, 565), - Means for branching a second partial flow of the circulating nitrogen stream upstream and / or downstream of the cycle compressor and / or of an intermediate stage of the cycle compressor under a product pressure (P, P1, P2, P3, P4) and for drawing off as pressurized nitrogen product (27, 29, 53, 564, 565),
dadurch gekennzeichnet, dass  characterized in that
- der Kreislaufverdichter (22, 322) als warmer Verdichter ausgebildet ist und einen Antrieb aufweist, der mittels externer Energie angetrieben wird.  - The cycle compressor (22, 322) is designed as a hot compressor and having a drive which is driven by means of external energy.
3. Vorrichtung nach Anspruch 12, gekennzeichnet durch Regelungsmittel, durch welche die 3. Apparatus according to claim 12, characterized by regulating means, through which the
- die Gesamtdruckstickstoffproduktmenge (PN), die durch die Summe der  - the total pressure nitrogen product quantity (PN), which is the sum of the
Mengenströme gebildet wird, die stromaufwärts und/oder stromabwärts des Kreislaufverdichters und/oder von einer Zwischenstufe des Kreislaufverdichters unter einem Produktdruck (P, P1 , P2, P3, P4) aus dem Kreislaufstickstoffstrom abgezweigt und als Druckstickstoffprodukt (27, 29, 53, 564, 565) gewonnen werden,  Flows formed upstream and / or downstream of the cycle compressor and / or from an intermediate stage of the cycle compressor under a product pressure (P, P1, P2, P3, P4) from the circulation nitrogen stream and as compressed nitrogen product (27, 29, 53, 564, 565),
- die Teilstrommenge (TS) an erstem Teilstrom, der durch den Sumpfverdampfer (9, 209) der Hochdrucksäule (8) geführt wird, und  - The partial flow amount (TS) at first partial flow, which is passed through the bottom evaporator (9, 209) of the high-pressure column (8), and
- die Einsatzluftmenge (EL), die in die Hochdrucksäule (8) eingeleitet wird, einstellen, wobei die Regelungsmittel so ausgebildet sind, dass  adjust the amount of feed air (EL) introduced into the high-pressure column (8), the control means being designed so that
- in einem ersten Lastfall  - in a first load case
- eine erste Gesamtdruckstickstoffproduktmenge PN1 gewonnen wird,  a first total pressure nitrogen product quantity PN1 is obtained,
- der erste Teilstrom in einer ersten Teilstrommenge TS1 durch den  - The first partial flow in a first partial flow TS1 by the
Sumpfverdampfer (9, 209) der Hochdrucksäule (8) geführt wird und  Bottom evaporator (9, 209) of the high-pressure column (8) is guided and
- die Einsatzluft in einer ersten Einsatzluftmenge EL1 in die Hochdrucksäule (8) eingeleitet wird,  the feed air is introduced into the high-pressure column (8) in a first quantity of feed air EL1,
- und in einem zweiten Lastfall  - and in a second load case
- eine zweite, höhere Gesamtdruckstickstoffproduktmenge PN2 gewonnen wird, PN2 > PN1 ,  a second, higher total nitrogen pressure product quantity PN2 is obtained, PN2> PN1,
- der erste Teilstrom in einer zweiten, höheren Teilstrommenge TS2 durch den - The first partial flow in a second, higher partial flow TS2 by the
Sumpfverdampfer (9, 209) der Hochdrucksäule (8) geführt wird, TS2 > TS1 , und Sump evaporator (9, 209) of the high pressure column (8) is performed, TS2> TS1, and
- die Einsatzluft in einer zweiten Einsatzluftmenge EL2 in die Hochdrucksäule - The feed air in a second amount of feed air EL2 in the high pressure column
(8) eingeleitet wird, wobei die zweite Einsatzluftmenge EL2 gleich der ersten Einsatzluftmenge EL1 oder nur unwesentlich höher ist, (8) is initiated, wherein the second amount of feed air EL2 is equal to the first amount of feed air EL1 or only slightly higher,
EL1 <= EL2 < EL1 · 0,2■ PN2/PN1. EL1 <= EL2 <EL1 · 0.2 ■ PN2 / PN1.
14. Vorrichtung nach Anspruch 13, mit Mitteln zum Entnehmen einer14. The apparatus of claim 13, comprising means for removing a
Zwischenflüssigkeit (465, 467), deren Sauerstoffgehalt zwischen demjenigen der sauerstoffangereicherten Flüssigkeit (462) und demjenigen der Intermediate liquid (465, 467) whose oxygen content is between that of the oxygen-enriched liquid (462) and that of the
stickstoffangereicherten Flüssigkeit (468) liegt, aus der Hochdrucksäule (8) und zum Zuführen dieser Flüssigkeit zu der Niederdrucksäule (460) an einer zweiten Zwischenstelle, die oberhalb der ersten Zwischenstelle angeordnet ist, wobei die die Mittel zum Entnehmen der Zwischenflüssigkeit (465) insbesondere in Höhe eines Zwischenverdampfers (10) der Hochdrucksäule (8) angeordnet sind.  nitrogen enriched liquid (468) from the high pressure column (8) and for supplying that liquid to the low pressure column (460) at a second intermediate location located above the first intermediate location, wherein the means for withdrawing the intermediate liquid (465) is in particular Height of an intermediate evaporator (10) of the high-pressure column (8) are arranged.
EP11743030.6A 2010-08-13 2011-08-09 Method and device for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air Not-in-force EP2603754B1 (en)

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PCT/EP2011/003982 WO2012019753A2 (en) 2010-08-13 2011-08-09 Method and device for obtaining compressed oxygen and compressed nitrogen by the low-temperature separation of air
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EP1750074A1 (en) 2005-08-02 2007-02-07 Linde Aktiengesellschaft Process and device for the cryogenic separation of air
US20090320520A1 (en) * 2008-06-30 2009-12-31 David Ross Parsnick Nitrogen liquefier retrofit for an air separation plant

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019214847A1 (en) 2018-05-07 2019-11-14 Linde Aktiengesellschaft Method for obtaining one or more air products and air separation system

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EP2603754B1 (en) 2016-11-30
US20130205831A1 (en) 2013-08-15
CN103069238A (en) 2013-04-24
DE102010056560A1 (en) 2012-02-16
US9733014B2 (en) 2017-08-15
WO2012019753A2 (en) 2012-02-16
CN103069238B (en) 2016-06-01
PL2603754T3 (en) 2017-08-31

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