EP2979051B1 - Method and device for producing gaseous compressed oxygen having variable power consumption - Google Patents

Method and device for producing gaseous compressed oxygen having variable power consumption Download PDF

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Publication number
EP2979051B1
EP2979051B1 EP14714174.1A EP14714174A EP2979051B1 EP 2979051 B1 EP2979051 B1 EP 2979051B1 EP 14714174 A EP14714174 A EP 14714174A EP 2979051 B1 EP2979051 B1 EP 2979051B1
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amount
substream
pressure
heat exchanger
oxygen
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German (de)
French (fr)
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EP2979051A2 (en
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Dimitri Goloubev
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • 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
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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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
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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
    • F25J3/04248—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
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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
    • F25J3/04248—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.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2313/00—Compression machines, plants or systems with reversible cycle not otherwise provided for
    • F25B2313/031—Sensor arrangements
    • F25B2313/0314—Temperature sensors near the indoor heat exchanger
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2313/00—Compression machines, plants or systems with reversible cycle not otherwise provided for
    • F25B2313/031—Sensor arrangements
    • F25B2313/0315—Temperature sensors near the outdoor heat exchanger
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2700/00—Sensing or detecting of parameters; Sensors therefor
    • F25B2700/21—Temperatures
    • F25B2700/2115—Temperatures of a compressor or the drive means therefor
    • F25B2700/21151—Temperatures of a compressor or the drive means therefor at the suction side of the compressor
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2700/00—Sensing or detecting of parameters; Sensors therefor
    • F25B2700/21—Temperatures
    • F25B2700/2115—Temperatures of a compressor or the drive means therefor
    • F25B2700/21152—Temperatures of a compressor or the drive means therefor at the discharge side of the compressor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
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    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
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    • 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
    • F25J2240/42—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 air

Definitions

  • EP 1139046 A1 EP 1146301 A1 .
  • the invention has for its object to provide a method of the type mentioned above and a corresponding device that require a relatively low cost of equipment, yet allow variable in a particularly wide range operation of the system in terms of energy consumption and work very efficiently.
  • boosters for the second and the third can also be used in the invention
  • the secondary compressor is then designed with three or more strands upstream or downstream of the multistage compressor additional compressor can be used, which compress the second and third partial flow individually or together.
  • first pressure first partial flow, so-called throttle flow
  • second high pressure second partial flow, so-called turbine flow
  • first partial flow so-called throttle flow
  • second partial flow so-called turbine flow
  • the second partial flow is after his work-performing relaxation usually at least partially, preferably completely or substantially completely introduced into the high-pressure column.
  • total airflow is meant the amount of air that is ultimately introduced into the distillation column system. This is done in different ways, in the form of two, three or more part streams, which flow through the main heat exchanger on at least one section.
  • the second mode of operation preferably none of the process streams of the distillation column system is subjected to cold compaction.
  • no rotating machines are used in the second mode of operation, which are not used in the first mode of operation.
  • the hardware outlay for variable operation is thus very low.
  • cold compression is meant here a gas compression process in which the gas is supplied to the compression at a temperature which is well below the ambient temperature, in particular below 240 K.
  • the method according to the invention can be carried out particularly efficiently. All the cold that is supplied via the liquid feed can be used to reduce the amount of turbine air. By correspondingly less air must be recompressed or by - in processes with compression of the total air to a high pressure - the total air is compressed to a much lower pressure.
  • the two booster can each have a separate aftercooler; Alternatively, their heat of compression is removed in a common aftercooler.
  • variable operation according to the invention can be applied not only to systems that are designed from the outset to such a variable operation. Rather, the invention also relates to a method for retrofitting an existing cryogenic air separation plant according to the claims 9 to 11.

Description

Die Erfindung betrifft ein Verfahren zur variablen Erzeugung von gasförmigem Drucksauerstoff mit variablem Energieverbrauch gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to a method for the variable production of gaseous pressure oxygen with variable energy consumption according to the preamble of patent claim 1.

Verfahren und Vorrichtungen zur Tieftemperaturzerlegung von Luft sind zum Beispiel aus Hausen/Linde, Tieftemperaturtechnik, 2. Auflage 1985, Kapitel 4 (Seiten 281 bis 337 ) bekannt.For example, methods and apparatus for cryogenic decomposition of air are off Hausen / Linde, Tiefftemperaturtechnik, 2nd edition 1985, chapter 4 (pages 281 to 337 ) known.

Das Destillationssäulen-System kann als Zwei-Säulen-System (zum Beispiel als klassisches Linde-Doppelsäulensystem) ausgebildet sein, oder auch als Drei- oder Mehr-Säulen-System. Es kann zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung weitere Vorrichtungen zur Gewinnung hoch reiner Produkte und/oder anderer Luftkomponenten, insbesondere von Edelgasen aufweisen, beispielsweise eine Argongewinnung und/oder eine Krypton-Xenon-Gewinnung.The distillation column system can be designed as a two-column system (for example as a classic Linde double column system), or as a three-column or multi-column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining highly pure products and / or other air components, in particular of noble gases have, for example, an argon production and / or a krypton-xenon recovery.

Bei dem Prozess wird ein flüssig auf Druck gebrachter Sauerstoff-Produktstrom gegen einen Wärmeträger verdampft und schließlich als gasförmiges Druckprodukt gewonnen. Diese Methode wird auch als Innenverdichtung bezeichnet. Sie dient zur Gewinnung von Drucksauerstoff. Für den Fall eines überkritischen Drucks findet kein Phasenübergang im eigentlichen Sinne statt, der Produktsttom wird dann "pseudo-verdampft".In the process, a liquid pressurized oxygen product stream is vaporized against a heat carrier and finally recovered as a gaseous pressure product. This method is also called internal compression. It serves for the production of pressure oxygen. In the case of a supercritical pressure, no phase transition takes place in the true sense, the Produktsttom is then "pseudo-evaporated".

Gegen den (pseudo-)verdampfenden Produktstrom wird ein unter hohem Druck stehender Wärmeträger verflüssigt (beziehungsweise pseudo-verflüssigt, wenn er unter überkritischem Druck steht). Der Wärmeträger wird häufig durch einen Teil der Luft gebildet, im vorliegenden Fall von dem "zweiten Teilstrom" der verdichteten Einsatzluft; gelegentlich wird dieser Strom auch Drosselstrom genannt, obwohl er anstelle eines Drosselventils auch in einer Flüssigturbine (DFE = "dense fluid expander") entspannt werden kann.Against the (pseudo) evaporating product stream, a high-pressure heat carrier is liquefied (or pseudo-liquefied when it is under supercritical pressure). The heat carrier is often formed by a part of the air, in the present case of the "second partial flow" of the compressed feed air; Occasionally, this flow is also called throttle flow, although it can be relaxed in a liquid turbine (DFE = dense fluid expander) instead of a throttle valve.

Innenverdichtungsverfahren sind zum Beispiel bekannt aus DE 830805 , DE 901542 (= US 2712738 / US 2784572 ), DE 952908 , DE 1103363 (= US 3083544 ), DE 1112997 (= US 3214925 ), DE 1124529 , DE 1117616 (= US 3280574 ), DE 1226616 (= US 3216206 ), DE 1229561 (= US 3222878 ), DE 1199293 , DE 1187248 (= US 3371496 ), DE 1235347 , DE 1258882 (= US 3426543 ), DE 1263037 (= US 3401531 ), DE 1501722 (= US 3416323 ), DE 1501723 (= US 3500651 ), DE 253132 (= US 4279631 ), DE 2646690 , EP 93448 B1 (= US 4555256 ), EP 384483 B1 (= US 5036672 ), EP 505812 B1 (= US 5263328 ), EP 716280 B1 (= US 5644934 ), EP 842385 B1 (= US 5953937 ), EP 758733 B1 (= US 5845517 ), EP 895045 B1 (= US 6038885 ), DE 19803437 A1 , EP 949471 B1 (= US 6185960 B1 ), EP 955509 A1 (= US 6196022 B1 ), EP 1031804 A1 (= US 6314755 ), DE 19909744 A1 , EP 1067345 A1 (= US 6336345 ), EP 1074805 A1 (= US 6332337 ), DE 19954593 A1 , EP 1134525 A1 (= US 6477860 ), DE 10013073 A1 , EP 1139046 A1 , EP 1146301 A1 , EP 1150082 A1 , EP 1213552 A1 , DE 10115258 A1 , EP 1284404 A1 (= US 2003051504 A1 ), EP 1308680 A1 (= US 6612129 B2 ), DE 10213212 A1 , DE 10213211 A1 , EP 1357342 A1 oder DE 10238282 A1 DE 10302389 A1 , DE 10334559 A1 , DE 10334560 A1 , DE 10332863 A1 , EP 1544559 A1 , EP 1585926 A1 , DE 102005029274 A1 EP 1666824 A1 , EP 1672301 A1 , DE 102005028012 A1 , WO 2007033838 A1 , WO 2007104449 A1 , EP 1845324 A1 , DE 102006032731 A1 , EP 1892490 A1 , DE 102007014643 A1, A1 , EP 2015012 A2 , EP 2015013 A2 , EP 2026024 A1 , WO 2009095188 A2 oder DE 102008016355 A1 .Internal compression methods are known, for example DE 830805 . DE 901542 (= US 2712738 / US 2784572 ) DE 952908 . DE 1103363 (= US 3,083,544 ) DE 1112997 (= US 3214925 ) DE 1124529 . DE 1117616 (= US 3280574 ) DE 1226616 (= US 3216206 ) DE 1229561 (= US 3222878 ) DE 1199293 . DE 1187248 (= US 3371496 ) DE 1235347 . DE 1258882 (= US 3426543 ) DE 1263037 (= US 3401531 ) DE 1501722 (= US 3,416,323 ) DE 1501723 (= US 3,500,651 ) DE 253132 (= US 4279631 ) DE 2646690 . EP 93448 B1 (= US 4555256 ) EP 384483 B1 (= US 5036672 ) EP 505812 B1 (= US 5263328 ) EP 716280 B1 (= US 5644934 ) EP 842385 B1 (= US 5953937 ) EP 758733 B1 (= US 5845517 ) EP 895045 B1 (= US 6038885 ) DE 19803437 A1 . EP 949471 B1 (= US 6,189,960 B1 ) EP 955509 A1 (= US 6196022 B1 ) EP 1031804 A1 (= US 6314755 ) DE 19909744 A1 . EP 1067345 A1 (= US 6336345 ) EP 1074805 A1 (= US 6332337 ) DE 19954593 A1 . EP 1134525 A1 (= US 6477860 ) DE 10013073 A1 . EP 1139046 A1 . EP 1146301 A1 . EP 1150082 A1 . EP 1213552 A1 . DE 10115258 A1 . EP 1284404 A1 (= US 2003051504 A1 ) EP 1308680 A1 (= US 6612129 B2 ) DE 10213212 A1 . DE 10213211 A1 . EP 1357342 A1 or DE 10238282 A1 DE 10302389 A1 . DE 10334559 A1 . DE 10334560 A1 . DE 10332863 A1 . EP 1544559 A1 . EP 1585926 A1 . DE 102005029274 A1 EP 1666824 A1 . EP 1672301 A1 . DE 102005028012 A1 . WO 2007033838 A1 . WO 2007104449 A1 . EP 1845324 A1 . DE 102006032731 A1 . EP 1892490 A1 . DE 102007014643 A1, A1 . EP 2015012 A2 . EP 2015013 A2 . EP 2026024 A1 . WO 2009095188 A2 or DE 102008016355 A1 ,

Vielfach zwingt ein schwankender Sauerstoffbedarf dazu, eine Luftzerlegungsanlage auf variablen Betrieb mit variabler Sauerstoffproduktion auszulegen. Umgekehrt kann es sinnvoll sein, eine Luftzerlegungsanlage trotz konstanter oder im Wesentlichen konstanter Produktion variabel zu betreiben, indem verschiedene Betriebsweisen vorgesehen sind, die unterschiedlich hohen Energieverbrauch aufweisen.In many cases, fluctuating oxygen demand forces an air separation plant to be designed for variable operation with variable oxygen production. Conversely, it may be useful to operate an air separation plant variable despite constant or substantially constant production by different modes of operation are provided, which have different levels of energy consumption.

Gegeben durch unterschiedliche Faktoren (nicht zuletzt durch immer größer werdenden Anteil erneuerbarer Energien an der Stromerzeugung) werden die Stromtarif-Schwankungen im Bereich Industrieanlagen immer größer. Beeinflusst von den gewissen Saisonschwankungen, wird die Schwankungsbreite des Stromtarifs auch durch den Tag-Nacht-Zyklus bestimmt.Given different factors (not least due to the increasing share of renewable energies in power generation), electricity tariff fluctuations in the field of industrial plants are becoming ever greater. Influenced by the certain seasonal fluctuations, the fluctuation range of the electricity tariff is also determined by the day-night cycle.

Bei niedrigem Strombedarf im Netz (zum Beispiel in der Nacht) kann einen Überschuss an Strom vorliegen. Dieser Überschuss soll aber abgenommen werden und wird daher für einen niedrigeren Preis angeboten. Steigt der Strombedarf im Netz (zum Beispiel tagsüber), steigt auch der Strompreis. Je nach Region und speziellen Rahmenbedingungen können die Strompreise an einem Ort um den Faktor fünf oder auch stärker variieren.When there is a low power requirement in the grid (for example at night), there may be an excess of electricity. However, this surplus is to be reduced and is therefore offered for a lower price. If the electricity demand in the grid increases (for example, during the day), the price of electricity also increases. Depending on the region and specific conditions, electricity prices in one location can vary by a factor of five or even more.

Es besteht also ein Bedarf, Luftzerlegungsanlagen mit einer schnellen und effizienten Lastanpassung auszustatten. Das kurzzeitige Abstellen solcher Anlage ist regelmäßig aufgrund einer stets aufrechtzuerhaltenden Lieferung an gasförmigem Drucksauerstoff nicht möglich.Thus, there is a need to provide air separation plants with a fast and efficient load adjustment. The temporary shutdown of such plant is regularly due to a constant supply of gaseous pressure oxygen not possible.

Bereits seit über 30 Jahren ist es bekannt, Wechselspeicherverfahren einzusetzen, um ein schwankendes Energieangebot zu kompensieren (Springmann, "Energieeinsparung", Linde-Symposium "Luftzerlegungsanlagen", 4. Arbeitstagung der Linde AG vom 15.-17.10.1980, Artikel H). Diese benötigen jedoch einen relativ hohen apparativen und regelungstechnischen Aufwand. Außerdem ist aus US 7272954 bekannt, bei hohem Strompreis, tiefkalte Flüssigkeit in das Destillationssäulen-System einzuleiten und die überschüssige Kälte mittels eines Kaltverdichters zu verbrauchen; auch hier wird allerdings zusätzlicher apparativen Aufwand notwendig.For over 30 years, it has been known to use removable storage methods to compensate for a fluctuating energy supply (Springmann, "Energy Saving", Linde Symposium "Air separation plants", 4th Workshop of Linde AG 15.-17.10.1980, Article H). However, these require a relatively high apparatus and control engineering effort. Besides, it is off US 7272954 known, at high electricity price, to introduce cryogenic liquid into the distillation column system and to use the excess cold by means of a cold compressor; however, additional equipment is necessary here as well.

Ein Verfahren gemäß dem Oberbegriff des Patentanspruchs 1 ist aus US20060010912 A1 bekannt.A method according to the preamble of claim 1 is made US20060010912 A1 known.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die einen vergleichsweise niedrigen apparativen Aufwand erfordern, trotzdem einen in einem besonders weiten Bereich variablen Betrieb der Anlage hinsichtlich ihres Energieverbrauchs ermöglichen und dabei besonders effizient arbeiten.The invention has for its object to provide a method of the type mentioned above and a corresponding device that require a relatively low cost of equipment, yet allow variable in a particularly wide range operation of the system in terms of energy consumption and work very efficiently.

Diese Aufgabe wird durch die Merkmale des kennzeichnenden Teils der Patentansprüche 1 und 8 gelöst.This object is solved by the features of the characterizing part of claims 1 and 8.

Bei geringem Energieangebot und hohem Strompreis wird die Anlage in der zweiten Betriebsweise gefahren. Dabei wird durch die Einspeisung von flüssigem Sauerstoff sowohl Kälte in die Anlage eingebracht als auch bereits geleistete Trennarbeit. Der Sauerstoff, der von außen zugeführt wird, braucht nicht mehr in der Anlage erzeugt zu werden. Entsprechend kann die Gesamtluftmenge, die in die Anlage eingeführt wird, vermindert werden. Verringert werden kann auch die Kälteproduktion, im Extremfall auf Null. Der Turbinenstrom (zweiter Teilstrom) wird also verringert oder sogar ganz abgeschaltet. Dabei bleibt die Menge an gasförmigem Drucksauerstoffprodukt gleich oder im Wesentlichen gleich. Unter "im Wesentlichen gleich" wird hier eine Veränderung um weniger als 3 %, vorzugsweise weniger als 2 % verstanden.With low energy supply and high electricity price, the system is operated in the second mode. It is by the supply of liquid oxygen Both cold introduced into the system as well as already performed separation work. The oxygen, which is supplied from outside, no longer needs to be generated in the system. Accordingly, the total amount of air introduced into the plant can be reduced. It is also possible to reduce the production of refrigeration, in extreme cases to zero. The turbine flow (second partial flow) is thus reduced or even completely switched off. The amount of gaseous pressure oxygen product remains the same or substantially the same. By "substantially the same" is meant a change of less than 3%, preferably less than 2%.

Bei der Erfindung werden zwei parallelgeschaltete Nachverdichter (auch BAC genannt - "booster air compressor") für den zweiten und den dritten Teilstrom der Luft eingesetzt; anders ausgedrückt ist der entsprechende Nachverdichter zweisträngig ausgebildet. Dies bewirkt eine besondere große Bandbreite, in der die Gesamtmenge der Einsatzluft und damit der Energieverbrauch der Anlage variiert werden kann. Gegenüber einer ersten Betriebsweise, die als Designfall mit hoher Flüssigproduktion ausgestaltet ist, der Energieverbrauch in einer zweiten Betriebsweise auf 50 % reduziert werden, in dem einer der beiden Nachverdichter abgeschaltet und der andere in Unterlast (etwa 0 % betrieben wird. Der Hauptluftverdichter, in dem der Gesamtluftstrom zunächst verdichtet wird, kann dabei ebenfalls mehrsträngig oder gegebenenfalls einsträngig ausgebildet sein. Die beiden Nachverdichter weisen beispielsweise 2 bis 5 Stufen auf, insbesondere 3 bis 4 Stufen. Selbstverständlich können bei der Erfindung auch drei oder mehr parallelgeschaltete Nachverdichter für den zweiten und den dritten Teilstrom der Luft eingesetzt werden; der Nachverdichter ist dann drei- oder mehrsträngig ausgebildet. Stromaufwärts oder stromabwärts des mehrsträngigen Nachverdichters können weitere Nachverdichter eingesetzt werden, die den zweiten und dritten Teilstrom einzeln oder gemeinsam verdichten.In the invention, two parallel-connected booster (also called BAC called "booster air compressor") for the second and the third partial flow of air used; In other words, the corresponding after-compressor is designed to be double-stranded. This causes a particularly wide range in which the total amount of feed air and thus the energy consumption of the system can be varied. Compared to a first mode of operation designed as a high liquid production design case, second mode energy consumption is reduced to 50% by shutting off one of the two boosters and operating the other in underload (about 0%) The two secondary compressors may have, for example, 2 to 5 stages, in particular 3 to 4. Of course, three or more parallel-connected boosters for the second and the third can also be used in the invention The secondary compressor is then designed with three or more strands upstream or downstream of the multistage compressor additional compressor can be used, which compress the second and third partial flow individually or together.

Im Rahmen der Erfindung können der erste Druck (erster Teilstrom, so genannter Drosselstrom) und der zweite hohe Druck (zweiter Teilstrom, so genannter Turbinenstrom) gleich oder unterschiedlich sein. Es kann auch die Gesamtluft auf den ersten oder zweiten hohen Druck verdichtet werden; alternativ wird die Gesamtluft auf einen niedrigeren Druck verdichtet, beispielsweise auf den Hochdrucksäulendruck plus Leitungsverlusten, und der erste und/oder der zweite Teilstrom der Luft werden nachverdichtet. Der zweite Teilstrom wird nach seiner arbeitsleistenden Entspannung in der Regel mindestens teilweise, vorzugsweise vollständig oder im Wesentlichen vollständig in die Hochdrucksäule eingeführt.In the context of the invention, the first pressure (first partial flow, so-called throttle flow) and the second high pressure (second partial flow, so-called turbine flow) may be the same or different. It is also possible to compress the total air to the first or second high pressure; Alternatively, the total air is compressed to a lower pressure, for example, the high pressure column pressure plus line losses, and the first and / or the second partial flow of the air are recompressed. The second partial flow is after his work-performing relaxation usually at least partially, preferably completely or substantially completely introduced into the high-pressure column.

Unter dem "Gesamtluftstrom" wird hier die Menge an Luft verstanden, die im Endeffekt in das Destillationssäulen-System eingeleitet wird. Das geschieht auf unterschiedlichen Wegen, in Form von zwei, drei oder mehr Teilströmen, die den Hauptwärmetauscher auf mindestens einem Teilstück durchströmen.By "total airflow" is meant the amount of air that is ultimately introduced into the distillation column system. This is done in different ways, in the form of two, three or more part streams, which flow through the main heat exchanger on at least one section.

Der in der zweiten Betriebsweise einzuspeisende Flüssigsauerstoff (zweiter Sauerstoffstrom) kann während der ersten Betriebsweise in der Anlage selbst produziert werden ("dritter Sauerstoffstrom" des Patentanspruchs 3); die "externe Quelle außerhalb des Destillationssäulen-Systems" wird dann von einem Flüssigsauerstofftank gebildet, in den während des Normalbetriebs mindestens ein Teil des dritten Sauerstoffstroms eingeleitet wird. Alternativ kann der zweite Sauerstoffstrom vollständig, teilweise oder zeitweise aus einer anderen Quelle entnommen werden, beispielsweise aus einem Flüssigtank, der nicht aus dem Destillationssäulen-System der Anlage, sondern aus dem einer benachbarten Luftzerlegungsanlage oder aus Tankfahrzeugen befüllt wird.The liquid oxygen to be fed in the second mode of operation (second oxygen stream) can be produced during the first mode of operation in the system itself ("third oxygen stream" of patent claim 3); the "external source outside the distillation column system" is then formed by a liquid oxygen tank into which at least part of the third oxygen stream is introduced during normal operation. Alternatively, the second oxygen stream may be withdrawn completely, partially or temporarily from another source, for example from a liquid tank which is not filled from the distillation column system of the plant but from an adjacent air separation plant or tank trucks.

Im Normalbetrieb der Anlage können in dem Destillationssäulen-System neben dem Flüssigsauerstoff weitere Flüssigprodukte wie Flüssigstickstoff und/oder Flüssigargon erzeugt werden.In normal operation of the plant, liquid products such as liquid nitrogen and / or liquid argon can be produced in the distillation column system in addition to the liquid oxygen.

Es ist günstig, wenn bei der Erfindung mindestens eine, vorzugsweise alle der in Patentanspruch 2 genannten Bedingungen erfüllt sind. Bevorzugt werden die Ströme in der zweiten Betriebsweise (Betrieb bei reduziertem Energieangebot) relativ zur ersten Betriebsweise (Normalbetrieb mit Flüssigproduktion) um einen Wert reduziert, der in den folgenden Zahlenbereichen liegt: Gesamtluftmenge 5 mol-% bis 30 mol-% Turbinenmenge (Turbinenstrom) 10 mol-% bis 100 mol-% It is advantageous if in the invention at least one, preferably all of the conditions mentioned in claim 2 are met. Preferably, in the second mode of operation (operation with reduced energy supply), the currents are reduced relative to the first mode of operation (normal mode with liquid production) by a value which lies in the following numerical ranges: Total air volume 5 mol% to 30 mol% Turbine quantity (turbine stream) 10 mol% to 100 mol%

Regelmäßig wird in der zweiten Betriebsweise kein Flüssigprodukt erzeugt, beziehungsweise, falls eine Argongewinnung vorgesehen ist, kein Flüssigprodukt außer Argon.Regularly no liquid product is produced in the second mode of operation, or, if an argon recovery is provided, no liquid product other than argon.

Eine besonders wirksame Anpassung an ein schwankendes Energieangebot lässt sich bei einem Verfahren nach Patentanspruch 3 erreichen, bei dem in der ersten Betriebsweise (im Normalbetrieb) ein dritter Sauerstoffstrom aus der Niederdrucksäule als Flüssigprodukt abgezogen wird. In der zweiten Betriebsweise (Stromsparbetrieb) wird weniger Sauerstoff als Flüssigprodukt gewonnen, vorzugsweise überhaupt keiner. Die zweite Flüssigsauerstoffmenge (an LOX-Produkt) ist vorzugsweise um 50 mol-% bis 100 mol-% niedriger als die erste Flüssigsauerstoffmenge.A particularly effective adaptation to a fluctuating energy supply can be achieved in a method according to claim 3, wherein in the first mode of operation (in normal operation), a third oxygen stream is withdrawn from the low-pressure column as a liquid product. In the second mode of operation (power saving mode) less oxygen is obtained as a liquid product, preferably none at all. The second amount of liquid oxygen (on LOX product) is preferably from 50 mole% to 100 mole% lower than the first amount of liquid oxygen.

In der zweiten Betriebsweise wird vorzugsweise keiner der Prozessströme des Destillationssäulen-Systems einer Kaltverdichtung unterzogen. Insbesondere werden in der zweiten Betriebsweise keinerlei rotierenden Maschinen eingesetzt, die nicht auch in der ersten Betriebsweise genutzt werden. Der Hardware-Aufwand für den variablen Betrieb ist damit denkbar gering.In the second mode of operation, preferably none of the process streams of the distillation column system is subjected to cold compaction. In particular, no rotating machines are used in the second mode of operation, which are not used in the first mode of operation. The hardware outlay for variable operation is thus very low.

Unter "Kaltverdichtung" wird hier ein Gasverdichtungsvorgang verstanden, bei dem das Gas der Verdichtung bei einer Temperatur zugefĂĽhrt wird, die deutlich unterhalb der Umgebungstemperatur liegt, insbesondere unterhalb von 240 K.By "cold compression" is meant here a gas compression process in which the gas is supplied to the compression at a temperature which is well below the ambient temperature, in particular below 240 K.

Dadurch kann das erfindungsgemäße Verfahren besonders effizient durchgeführt werden. Die gesamte Kälte, die über die Flüssigkeitszuspeisung zugeführt wird, kann genutzt werden, um die Turbinenluftmenge zu reduzieren. Indem entsprechend weniger Luft nachverdichtet werden muss oder indem - bei Verfahren mit Verdichtung der Gesamtluft auf einen hohen Druck - die Gesamtluft auf einen deutlich niedrigeren Druck verdichtet wird.As a result, the method according to the invention can be carried out particularly efficiently. All the cold that is supplied via the liquid feed can be used to reduce the amount of turbine air. By correspondingly less air must be recompressed or by - in processes with compression of the total air to a high pressure - the total air is compressed to a much lower pressure.

Vorzugsweise wird in der zweiten Betriebsweise die arbeitsleistende Entspannung des zweiten Teilstroms gänzlich eingestellt, das heißt die zweite Turbinenmenge ist null.Preferably, in the second mode of operation, the work-performing expansion of the second partial flow is set completely, that is, the second turbine quantity is zero.

Die beiden Nachverdichter können jeweils einen separaten Nachkühler aufweisen; alternativ wird ihre Kompressionswärme in einem gemeinsamen Nachkühler entfernt.The two booster can each have a separate aftercooler; Alternatively, their heat of compression is removed in a common aftercooler.

Grundsätzlich kann der Gesamtluftstrom nur aus dem ersten Teilstrom (Turbinenstrom) und dem zweiten Teilstrom (Drosselstrom) bestehen. Der Gesamtluftstrom kann auch weitere Luftteilströme umfassen, darunter einen ersten Teil (Direktluft), der ohne Turbinenentspannung und in im Wesentlichen gasförmigem Zustand in das Destillationssäulen-System, insbesondere in die Hochdrucksäule eingespeist wird. Als "im Wesentlichen gasförmig" wird hier ein Strom bezeichneten, der vollständig gasförmig ist oder weniger als 1-2 mol-% Flüssigkeit enthält. Vorzugsweise wird der Gesamtluftstrom in genau drei Luftströme aufgeteilt, wie es im Patentanspruch 7 beschrieben ist.In principle, the total air flow can only consist of the first partial flow (turbine flow) and the second partial flow (throttle flow). The total air flow may also include other partial air streams, including a first part (direct air), which is fed without Turbinenentspannung and in a substantially gaseous state in the distillation column system, in particular in the high-pressure column. As "substantially gaseous" here is meant a stream which is completely gaseous or contains less than 1-2 mol% of liquid. Preferably, the total air flow is divided into exactly three air streams, as described in claim 7.

Die Erfindung betrifft außerdem eine Vorrichtung gemäß Patentanspruch 8. Die erfindungsgemäße Vorrichtung kann durch Vorrichtungsmerkmale ergänzt werden, die den Merkmalen der abhängigen Verfahrensansprüche entsprechen.The invention also relates to a device according to claim 8. The device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.

Die erfindungsgemäße variable Betriebsweise kann nicht nur auf Anlagen angewendet werden, die von Vorneherein auf einen solchen variablen Betrieb ausgelegt sind. Vielmehr betrifft die Erfindung außerdem ein Verfahren zum Nachrüsten einer bestehenden Tieftemperatur-Luftzerlegungsanlage gemäß den Patentansprüchen 9 bis 11.The variable operation according to the invention can be applied not only to systems that are designed from the outset to such a variable operation. Rather, the invention also relates to a method for retrofitting an existing cryogenic air separation plant according to the claims 9 to 11.

Dabei muss kaum in die Hardware des bestehenden Destillationssäulen-Systems eingegriffen werden. Fehlt eine Leitung zum Einspeisen von Flüssigsauerstoff in die Niederdrucksäule, muss diese natürlich nachgerüstet werden. Unter Umständen kann auch eine vorhandene Leitung genutzt werden; dann müssen lediglich Armaturen und gegebenenfalls eine Pumpe ergänzt werden. Im Übrigen ist es mit einer Anpassung der Regelung getan, das heißt der Software des Betriebsleitsystems. Insbesondere müssen keinerlei rotierende Maschinen nachgerüstet werden. Eine Ausnahme kann der zweite Nachverdichter sein, wenn die bestehende Anlage nur einen einsträngigen Nachverdichter aufweist.It hardly has to interfere with the hardware of the existing distillation column system. If a line for feeding liquid oxygen into the low-pressure column is missing, it must of course be retrofitted. Under certain circumstances, an existing line can be used; then only fittings and possibly a pump must be added. Incidentally, it is done with an adjustment of the scheme, that is the software of the operations control system. In particular, no rotating machines need to be retrofitted. An exception may be the second after-compressor, if the existing system has only one single-stranded secondary compressor.

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

Figur 1
ein erstes AusfĂĽhrungsbeispiel ohne Argongewinnung und
Figur 2
ein zweites AusfĂĽhrungsbeispiel mit Argongewinnung.
The invention and further details of the invention are explained below with reference to embodiments schematically illustrated in the drawings. Hereby show:
FIG. 1
a first embodiment without argon recovery and
FIG. 2
a second embodiment with argon recovery.

Der Hauptluftverdichter, die Vorkühlung der Luft und die Luftreinigung sind in Figur 1 nicht dargestellt. Der gereinigte Gesamtluft 1 tritt in der ersten Betriebsweise (Normalbetrieb/Auslegungsfall) unter einem Druck von 5,8 bar ein. Ein erster Teil 2 wird unter diesem Druck in einen Hauptwärmetauscher 3 auf etwa Taupunkt abgekühlt und über Leitung 4 in die Hochdrucksäule 5 eines Destillationssäulen-Systems eingeleitet, das außerdem eine Niederdrucksäule 6 und einen Hauptkondensator 7 aufweist. Die beiden Säulen weisen an ihrem Kopf einen Betriebsdruck von 5,0 bis 5,5 bar beziehungsweise 1,3 bis 1,4 bar auf. Alternativ können die Drücke in beiden Säulen etwa proportional auf ein höheres Niveau angehoben werden.The main air compressor, the pre-cooling of the air and the air purification are in FIG. 1 not shown. The purified total air 1 occurs in the first mode (normal operation / design case) under a pressure of 5.8 bar. A first part 2 is cooled under this pressure in a main heat exchanger 3 to about dew point and introduced via line 4 in the high pressure column 5 of a distillation column system, which also has a low pressure column 6 and a main capacitor 7. The two columns have at their top an operating pressure of 5.0 to 5.5 bar or 1.3 to 1.4 bar. Alternatively, the pressures in both columns may be raised approximately proportionally to a higher level.

Ein zweiter Teil 8 der Gesamtluft 1 wird in einem Paar von parallel geschalteten Nachverdichtern 9, 10 mit Nachkühler 11 auf 58 bar nachverdichtet und als "erster Teilstrom" 13 und "zweiter Teilstrom" 16 dem Hauptwärmetauscher 3 zugeführt. Der erste Teilstrom wird bis zum kalten Ende des Hauptwärmetauschers geführt und dabei pseudo-verflüssigt. Nach Entspannung in einem Drosselventil 15 wird er in überwiegend flüssigem Zustand in die Hochdrucksäule 5 eingeleitet. Der zweite Teilstrom wird bei einer Zwischentemperatur über Leitung 16 aus dem Hauptwärmetauscher 3 entnommen, in einer Expansionsturbine 17 arbeitsleistend auf etwa Hochdrucksäulendruck entspannt. Nach Abtrennung eines kleinen Flüssiganteils in einem Abscheider (Phasentrenner) 18 wird der zweite Teilstrom gemeinsam mit dem ersten Teil der Einsatzluft über Leitung 4 der Hochdrucksäule zugeführt. Die Turbine 17 wird von einem elektrischen Generator G gebremst.A second part 8 of the total air 1 is recompressed in a pair of parallel-connected booster 9, 10 with aftercooler 11 to 58 bar and fed to the main heat exchanger 3 as "first partial flow" 13 and "second partial flow" 16. The first partial flow is led to the cold end of the main heat exchanger and thereby pseudo-liquefied. After relaxation in a throttle valve 15, it is introduced into the high-pressure column 5 in a predominantly liquid state. The second partial flow is removed at an intermediate temperature via line 16 from the main heat exchanger 3, expanded in an expansion turbine 17 work to approximately high-pressure column pressure. After separation of a small proportion of liquid in a separator (phase separator) 18, the second partial stream is supplied together with the first part of the feed air via line 4 of the high-pressure column. The turbine 17 is braked by an electric generator G.

Die sauerstoffangereicherte Sumpfflüssigkeit 19 der Hochdrucksäule wird in einem Unterkühlungs-Gegenströmers 20 abgekühlt und über Leitung 21 der Niederdrucksäule 6 an einer Zwischenstelle zugeführt. Über die Leitungen 22 und 23 wird mindestens ein Teil der in die Hochdrucksäule eingespeisten Luft gleich wieder entnommen und nach Unterkühlung 20 der Niederdrucksäule 6 zugespeist. Unreiner Flüssigstickstoff 24 wird ebenfalls unterkühlt (20) und dann über Leitung 25 als Rücklauf auf den Kopf der Niederdrucksäule 6 aufgegeben.The oxygen-enriched bottoms liquid 19 of the high-pressure column is cooled in a subcooling countercurrent 20 and fed via line 21 to the low-pressure column 6 at an intermediate point. About the lines 22 and 23, at least a portion of the air fed into the high-pressure column is immediately removed again and fed after supercooling 20 of the low-pressure column 6. Impure liquid nitrogen 24 is also supercooled (20) and then fed via line 25 as reflux to the top of the low-pressure column 6.

Ein erster Teil 27 des gasförmigen Kopfstickstoffs 26 der Hochdrucksäule 5 wird in dem Hauptkondensator 7 vollständig oder fast vollständig verflüssigt. Der dabei gewonnene Flüssigstickstoff 28 wird zu einem ersten Teil 29 als Rücklauf auf den Kopf der Hochdrucksäule 5 aufgegeben. Ein zweiter Teil 30, 32 kann nach Unterkühlung 20 und Flashgasabtrennung in einem Abscheider (Phasentrenner) 33 als Flüssigprodukt (LIN) gewonnen werden. Ein zweiter Teil 39 des gasförmigen Kopfstickstoffs 26 der Hochdrucksäule 5 wird im Hauptwärmetauscher angewärmt und über Leitung 40 als gasförmiges Druckstickstoffprodukt (PGAN) gewonnen.A first part 27 of the gaseous top nitrogen 26 of the high-pressure column 5 is completely or almost completely liquefied in the main condenser 7. The case obtained liquid nitrogen 28 is fed to a first part 29 as reflux to the head of the high-pressure column 5. A second part 30, 32 can be obtained after supercooling 20 and flash gas separation in a separator (phase separator) 33 as a liquid product (LIN). A second part 39 of the gaseous nitrogen head 26 of the high-pressure column 5 is warmed in the main heat exchanger and recovered via line 40 as gaseous pressure nitrogen product (PGAN).

Vom Sumpf der Niederdrucksäule (genauer: aus dem Verdampfungsraum des Hauptkondensators 7) wird flüssiger Sauerstoff 34 abgezogen. Ein erster Teil davon strömt als "erster Sauerstoffstrom" 35 zu einer Pumpe 36 und wird dort in flüssigem Zustand auf einen erhöhten Druck von 30 bar gebracht. Der (in dem Beispiel unterkritische) Sauerstoffstrom 37 wird zum kalten Ende des Hauptwärmetauschers geführt. Im Hauptwärmetauscher 3 wird er verdampft und auf etwa Umgebungstemperatur angewärmt. Über Leitung 38 wird der erste Sauerstoffstrom schließlich als gasförmiges Drucksauerstoffprodukt (GOX IC) gewonnen.From the bottom of the low-pressure column (more precisely: from the evaporation space of the main condenser 7) liquid oxygen 34 is withdrawn. A first part of this flows as "first oxygen stream" 35 to a pump 36 and is brought there in the liquid state to an elevated pressure of 30 bar. The oxygen stream 37 (subcritical in the example) is fed to the cold end of the main heat exchanger. In the main heat exchanger 3 it is vaporized and warmed to about ambient temperature. Via line 38, the first oxygen stream is finally recovered as gaseous pressure oxygen product (GOX IC).

Ein zweiter Teil 44/45 des flĂĽssigen Sauerstoffs 34 wird - gegebenenfalls nach UnterkĂĽhlung 20 - ĂĽber Leitung 45 als "dritter Sauerstoffstrom" abgezogen und als FlĂĽssigprodukt gewonnen. Er wird insbesondere in einen FlĂĽssigsauerstofftank (nicht dargestellt) eingeleitet (LOX to tank).A second part 44/45 of the liquid oxygen 34 is - optionally after subcooling 20 - withdrawn via line 45 as a "third oxygen stream" and recovered as a liquid product. In particular, it is introduced into a liquid oxygen tank (not shown) (LOX to tank).

Eine Leitung 46 dient zur Einspeisung eines "zweiten Sauerstoffstroms" aus dem Flüssigsauerstofftank in den Sumpf der Niederdrucksäule; sie ist in der ersten Betriebsweise jedoch außer Betrieb.A conduit 46 serves to feed a "second oxygen stream" from the liquid oxygen tank into the bottom of the low-pressure column; However, it is in the first mode of operation but out of service.

Gasförmiger Unreinstickstoff 41 vom Kopf der Niederdrucksäule 6 wird im Unterkühlungs-Gegenströmer 20 und weiter im Hauptwärmetauscher 3 angewärmt und über Leitung 42 in die Atmosphäre abgeblasen oder als Regeneriergas in der nicht dargestellten Einrichtung zur Luftreinigung eingesetzt.Gaseous impure nitrogen 41 from the top of the low-pressure column 6 is warmed in the supercooling countercurrent 20 and further in the main heat exchanger 3 and blown off via line 42 into the atmosphere or used as a regeneration gas in the device for air purification, not shown.

In der ersten Betriebsweise ist die Luftturbine 17 in Betrieb, die Bypass-Leitung 43 wird nicht durchströmt. Ebenso wird über Leitung 45 flüssiger Sauerstoff aus dem Destillationssäulen-System abgezogen. Zusätzlich kann Stickstoff als Flüssigprodukt (LIN) gewonnen werden sowie reiner gasförmiger Stickstoff aus der Niederdrucksäule (nicht dargestellt).In the first mode of operation, the air turbine 17 is in operation, the bypass line 43 is not flowed through. Also, via line 45, liquid oxygen is withdrawn from the distillation column system. In addition, nitrogen can be recovered as a liquid product (LIN) and pure gaseous nitrogen from the low pressure column (not shown).

In einer zweiten Betriebsweise (Stromsparbetrieb) wird die Leitung 45 geschlossen, vorzugsweise wird auch kein Flüssigstickstoff (LIN) produziert. Umgekehrt wird über Leitung 46 Flüssigsauerstoff von außerhalb des Destillationssäulen-Systems in die Niederdrucksäule eingespeist. Die Produktmenge an gasförmigem Drucksauerstoff 38/GOX IC bleibt dabei gleich. Die Gesamtluftmenge 1 ist gegenüber der ersten Betriebsweise um etwa 32 mol-% vermindert, der zweite Teil 8/12 sogar um 65 mol-%; vorzugsweise ist einer der beiden Nachverdichter 9, 10 außer Betrieb, der andere wird mit reduzierter Leistung gefahren. Die Turbine 17 steht still, der Bypass 43 ist offen und wird von einem kleinen Strom durchflossen, der die entsprechenden Passagen des Hauptwärmetauschers spült. Der Gesamtluftdruck beträgt nur noch 5,3 bar, der Luftdruck stromabwärts der Nachverdichter 9, 10 nur noch 53 bar. Dabei wird in der zweiten Betriebsweise gleich viel gasförmiges Drucksauerstoffprodukt (GOX IC) unter gleichem Druck geliefert wie in der ersten Betriebsweise. Diese Zahlen gelten für den Fall, dass in der ersten Betriebsweise etwa 25 mol-% des Gesamtsauerstoffprodukts als Flüssigprodukt und etwa 75 mol-% als gasförmiges (innenverdichtetes) Druckprodukt unter ca. 30 bar gewonnen werden. Außerdem wird dabei etwa gleich viel an flüssigem Stickstoff wie an flüssigem Sauerstoff produziert. Hier verstärken sich zwei Effekte und ermöglichen damit eine besonders hohe Verringerung des Energieverbrauchs am Hauptluftverdichter (Gesamtluftmenge) und beim Nachverdichten (erster und zweiter Teilstrom): Zum Einen wird die Gesamtluftmenge verringert, indem flüssiger Sauerstoff von außen eingespeist wird (und damit nicht mehr aus der eingespeisten Luftmenge erzeugt werden muss); zum Anderen verringern die nicht produzierten LOX- und LIN-Produkte den Luft- und Kältebedarf weiter. Bei dem unten dargestellten zweiten Zahlenbeispiel für eine reine Gasanlage werden dagegen nur die Mengenänderungen beschrieben, die alleine durch Einspeisung des externen LOX in der zweiten Betriebsweise hervorgerufen sind.In a second mode of operation (power saving mode), the line 45 is closed, preferably also no liquid nitrogen (LIN) is produced. Conversely, via line 46, liquid oxygen is fed from outside the distillation column system into the low-pressure column. The amount of gaseous pressure oxygen 38 / GOX IC remains the same. The total amount of air 1 is reduced by about 32 mol% compared to the first mode of operation, the second part 8/12 even by 65 mol%; Preferably, one of the two booster 9, 10 is out of service, the other is driven with reduced power. The turbine 17 stands still, the bypass 43 is open and is traversed by a small current, which flushes the corresponding passages of the main heat exchanger. The total air pressure is only 5.3 bar, the air pressure downstream of the booster 9, 10 only 53 bar. In the second mode of operation, the same amount of gaseous pressure oxygen product (GOX IC) is supplied under the same pressure as in the first mode of operation. These figures apply to the case where, in the first mode of operation, about 25 mol% of the total oxygen product is obtained as a liquid product and about 75 mol% as a gaseous (internally compressed) pressure product below about 30 bar. It also produces about the same amount of liquid nitrogen as liquid oxygen. Here, two effects are amplified, thus enabling a particularly high reduction in energy consumption at the main air compressor (total air volume) and at the recompression (first and second partial flow): On the one hand, the total amount of air is reduced by supplying liquid oxygen from the outside (and thus no longer from the supplied amount of air must be generated); On the other hand, the non-produced LOX and LIN products further reduce the demand for air and refrigeration. By contrast, in the second numerical example for a pure gas installation shown below, only the changes in quantity that are caused solely by feeding the external LOX in the second operating mode are described.

Im Rahmen der Erfindung kann aus der Anlage zur Erzeugung von Flüssigprodukten (erste Betriebsweise) eine reine Gasanlage (zweite Betriebsweise) gemacht und dabei in Zeiten mit hohen Strompreisen viel Energie gespart werden. Das Verfahren bleibt dabei effizient, da keiner der Verdichter im Bypass betrieben wird und die Verluste bei der Drosselung des Turbinenstromes wegen der kleinen (überwiegend für das Durchspülen von Wärmetauscherpassagen benötigten) Menge und der niedrigen Eintrittstemperatur (diese Temperatur liegt in der zweiten Betriebsweise wesentlich niedriger als in der ersten) relativ gering sind. Es wird praktisch ein effektiver Betriebsmodus ohne Flüssigproduktion ermöglicht. Zusätzliche Energieeinsparung kommt von der reduzierten Gesamtluftmenge (entsprechend verringerte Antriebsenergie am nicht dargestellten Hauptluftverdichter). Wegen nicht benötigter Kälteleistung wird außerdem Antriebsenergie beim Nachverdichten 9/10 eingespart.In the context of the invention can be made from the plant for the production of liquid products (first mode of operation) a pure gas system (second mode) while saving energy in times of high electricity prices. The process remains efficient because none of the compressors are operated in bypass and the losses in the throttling of the turbine flow because of the small (mainly required for the flushing of heat exchanger passages) amount and the low inlet temperature (this temperature is essential in the second mode lower than in the first) are relatively low. It is practically an effective mode of operation without liquid production allows. Additional energy savings comes from the reduced total amount of air (correspondingly reduced drive energy at the main air compressor, not shown). Because cooling capacity is not required, drive energy is also saved when re-compacting 9/10.

Im Rahmen der Erfindung kann auch eine bestehende FlĂĽssiganlage nach Figur 1, aber ohne Leitung 46 entsprechend nachgerĂĽstet werden. Dazu ist lediglich der Einbau dieser Leitung 46 erforderlich, ansonsten bleiben alle Bauteile gleich.In the context of the invention may also be an existing liquid plant after FIG. 1 but be retrofitted without line 46 accordingly. For this purpose, only the installation of this line 46 is required, otherwise all components remain the same.

Die Erfindung kann sinngemäß auch bei Verfahren ohne Nachverdichtung genutzt werden, bei denen die Gesamtluft auf deutlich über Hochdrucksäulendruck verdichtet wird (HAP - high air pressure). Unabhängig davon kann die Turbine 17 anstelle des Generators von einem Nachverdichter für Turbinenluft gebremst werden. Auch eine Anwendung der Erfindung auf Verfahren mit so genannter Einblaseturbine (die Luft vom Hauptluftverdichter wird nach Entspannung nicht in die Drucksäule sondern in die Niederdrucksäule geleitet) oder mit mehr als einer Turbine sowie auf solche mit Stickstoffkreislauf ist möglich.The invention can be used mutatis mutandis in processes without recompression, in which the total air is compressed to significantly high-pressure column pressure (HAP - high air pressure). Independently of this, the turbine 17 can be braked instead of the generator by a compressor for turbine air. An application of the invention to methods with so-called injection turbine (the air from the main air compressor is not led to relaxation in the pressure column but in the low pressure column) or with more than one turbine and those with nitrogen cycle is possible.

Figur 2 unterscheidet sich von Figur 1 lediglich durch eine hinzugefügte Argongewinnung, die hier nur schematisch dargestellt ist (Argon Box). Diese ist auf die übliche Weise mit Hochdrucksäule und Niederdrucksäule verbunden. FIG. 2 differs from FIG. 1 only by an added Argon recovery, which is shown here only schematically (argon box). This is connected in the usual way with high pressure column and low pressure column.

In einem ersten Zahlenbeispiel kann die Anlage nach Figur 2 wie bei Figur 1 betrieben werden. Dabei wird in der zweiten Betriebsweise wird eine Menge an flĂĽssigem Argon LAR gewonnen, die proportional zur Gesamtluftmenge reduziert ist.In a first numerical example, the system can after FIG. 2 as in FIG. 1 operate. In this case, in the second mode, an amount of liquid argon LAR is obtained, which is reduced in proportion to the total amount of air.

Ein zweites Zahlenbeispiel weicht hiervon ab, indem (auch) in der ersten Betriebsweise kein Flüssigsauerstoffprodukt gewonnen wird (und vorzugsweise auch kein Flüssigstickstoffprodukt LIN). Auch in diesem Fall ist die Produktmenge an gasförmigem Drucksauerstoff 38/GOX IC in der zweiten Betriebsweise gleich derjenigen in der ersten Betriebsweise. Die Gesamtluftmenge wird gegenüber der ersten Betriebsweise um 10 mol-% vermindert, der zweite Teil 8/12 um 25 mol-%. Dies kann auch mit einem einzigen Nachverdichter (statt der in den Zeichnungen dargestellten zwei parallel geschalteten) bewerkstelligt werden.A second numerical example deviates therefrom in that (also) in the first mode of operation no liquid oxygen product is obtained (and preferably also no liquid nitrogen product LIN). Also in this case, the product amount of gaseous pressure oxygen 38 / GOX IC in the second mode is the same as that in the first mode. The total amount of air is reduced compared to the first mode by 10 mol%, the second part 8/12 by 25 mol%. This can also be accomplished with a single post-compressor (instead of the two parallel ones shown in the drawings).

Abweichend von der Darstellung in den Zeichnungen kann der Turbinenstrom 16 auch an einem Zwischenabzug der beiden Nachverdichter 9, 10 abgezogen werden, also mit einem geringeren Druck als der Drosselstrom 13, der dann vom Austritt der Nachverdichter 9, 10 abgenommen wird. Grundsätzlich kann die Turbine 17 auch mit einer Nachverdichterstufe gebremst werden, die eine der Ströme 13 und 16 oder beide weiter nachverdichtet.Notwithstanding the representation in the drawings, the turbine stream 16 can also be withdrawn at an intermediate take-off of the two booster 9, 10, ie with a lower pressure than the throttle flow 13, which is then removed from the outlet of the booster 9, 10. In principle, the turbine 17 can also be braked with a post-compressor stage, which further compresses one of the streams 13 and 16 or both.

Claims (10)

  1. Method for producing gaseous compressed oxygen having variable power consumption by low temperature separation of air in a distillation column system that has a high-pressure column (5) and a low-pressure column (6), in which
    - feed air in the form of a total air stream (1) is cooled in a main heat exchanger (3),
    - at least a part of the cooled feed air is introduced into the high-pressure column (5),
    - a first oxygen stream (35) from the low-pressure column (6) is pressurized (36) in the liquid state,
    - the pressurized first oxygen stream (37) is vaporized or pseudo-vaporized and warmed in the main heat exchanger (3),
    - the warmed first oxygen stream (38) is obtained as a gaseous compressed oxygen product,
    - a first substream (13) of the feed air, before entry thereof into the main heat exchanger (3), is brought to a first high pressure which is at least 4 bar higher than the operating pressure of the high-pressure column (5),
    - the first substream is liquefied or pseudo-liquefied at the first high pressure in the main heat exchanger (3) and subsequently introduced (14) into the distillation column system,
    - a second substream (16) of the feed air is brought to a second high pressure (9, 10) that is at least 4 bar higher than the operating pressure of the high-pressure column (5),
    - the second substream is cooled in the main heat exchanger (3) only to an intermediate temperature,
    - the second substream (16) that is cooled to the intermediate temperature is work-producingly expanded (17) and subsequently introduced into the distillation column system (4),
    - wherein, in a first mode of operation
    - a first total air amount is cooled in the main heat exchanger (3),
    - a first turbine amount, as second substream (16), is fed to the work-producing expansion,
    - and wherein, in a second mode of operation
    - a second total air amount is cooled in the main heat exchanger (3), which second total air amount is less than the first total air amount and,
    - a second turbine amount is fed as second substream to the work-producing expansion (17) which second turbine amount is less than the first turbine amount
    - and wherein
    - the total air stream (1), upstream of its cooling the the main heat exchanger (3), is compressed in a main air compressor,
    - in the second mode of operation, a second oxygen stream (46) is introduced from an external source outside the distillation column system into the low-pressure column (6) in the liquid state, characterized in that
    - in the first mode of operation, the first and second substreams (13, 16) are together (8, 12) boosted in a pair of parallel-connected boosters (9, 10).
  2. Method according to Claim 1, characterized in that at least one of the following conditions is met:
    - the second total air amount is at least 5 mol% lower than the first total air amount,
    - a second turbine amount is at least 10 mol% lower, in particular at least 30 mol% lower, than the first turbine amount.
  3. Method according to Claim 1 or 2, characterized in that
    - in the first mode of operation, a third oxygen stream is taken off as liquid product from the low-pressure column in the scope of a first liquid oxygen amount and
    - in the second mode of operation, the third oxygen stream is taken off as liquid product in the scope of a second liquid oxygen amount which is lower than the first liquid oxygen amount,
    - wherein the second liquid oxygen amount is lower than the first liquid oxygen amount, in particular by at least 50 mol%, in particular by 100 mol%.
  4. Method according to any one of Claims 1 to 3, characterized in that, in the second mode of operation, none of the process streams of the distillation column system is subjected to a cold compression.
  5. Method according to any one of Claims 1 to 4, characterized in that the second turbine amount is zero.
  6. Method according to any one of Claims 1 to 5, characterized in that the two boosters (9, 10) have a shared aftercooler (11) or have one aftercooler each.
  7. Method according to any one of Claims 1 to 6, characterized in that the total air stream consists of a first part (2) and a second part (8), wherein the second part (8) consists of the first substream (13) and the second substream (16), and in particular the first part (2) is fed without turbine expansion substantially in the gaseous state into the distillation column system, in particular into the high-pressure column (5).
  8. Device for producing gaseous compressed oxygen having variable energy consumption by low-temperature separation of air
    - having a distillation column system that has a high-pressure column (5) and a low-pressure column (6),
    - having a main heat exchanger (3) for cooling feed air in the form of a total air stream (1),
    - having means for introducing at least a part of the cooled feed air into the high-pressure column (5),
    - having means (36) for pressurizing a first oxygen stream (35) from the low-pressure column (6) in the liquid state,
    - having means for vaporizing or pseudo-vaporizing and warming in the main heat exchanger (3) the pressurized first oxygen stream (37),
    - having means for producing the warmed first oxygen stream (38) as a gaseous compressed oxygen product,
    - having means (9, 10) for bringing a first substream (13) of the feed air, before entry thereof into the main heat exchanger (3), to a first high pressure which is at least 4 bar higher than the operating pressure of the high-pressure column (5),
    - having means for liquefying or pseudo-liquefying the first substream at the first high pressure in the main heat exchanger (3),
    - having means (14) for introducing the (pseudo-)liquefied first substream into the distillation column system,
    - having means (9, 10) for bringing a second substream (16) of the feed air to a second high pressure which is at least 4 bar higher than the operating pressure of the high-pressure column (5),
    - having means for withdrawing the second substream in the main heat exchanger (3) at an intermediate temperature,
    - having means (17) for the work-producing expansion of the second substream (16) that is cooled to the intermediate temperature,
    - having means (4) for introducing the work-producingly expanded first substream into the distillation column system introduced (4),
    - having a main air compressor for compressing the total air stream (1) upstream of its cooling in the main heat exchanger (3),
    - having a means for introducing a second oxygen stream (46) in the liquid state from an external source outside the distillation column system into the low-pressure column (6)
    - having a control device, by which the following process parameters are set:
    - in a first mode of operation
    - a first total air amount which is cooled in the main heat exchanger (3),
    - a first turbine amount which is fed as first substream (16) to the work-producing expansion,
    - and in a second mode of operation
    - a second total air amount is cooled in the main heat exchanger (3) which is less than the first total air amount,
    - a second turbine amount is fed as first substream to the work-producing expansion (17), which second turbine amount is less than the first turbine amount
    - an amount of the second oxygen stream which is fed to the low-pressure column (6) in the liquid state, which amount is greater than the amount in the first mode of operation, characterized by a pair of boosters (9, 10) connected in parallel for jointly boosting the first and second substream (13,16).
  9. Method for retrofitting a low-temperature air separation plant for an operation according to the method according to any one of claims 1 to 7, characterized in that means are added for introducing the second oxygen stream into the low-pressure column.
  10. Method according to Claim 9, characterized in that, apart from the means for introducing the second oxygen stream into the low-pressure column and optionally apart from the further booster (10), no, or substantially no, changes to the low-temperature air separation plant are made.
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US10281207B2 (en) * 2016-06-30 2019-05-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of air gases by the cryogenic separation of air with variable liquid production and power usage
US10281206B2 (en) * 2016-06-30 2019-05-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus for the production of air gases by the cryogenic separation of air with variable liquid production and power usage
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CN105143801A (en) 2015-12-09
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