DE10153919A1 - Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises cooling the heat exchange fluid downstream of the high pressure column sump vaporizer and upstream of a pressure relieving device - Google Patents
Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises cooling the heat exchange fluid downstream of the high pressure column sump vaporizer and upstream of a pressure relieving deviceInfo
- Publication number
- DE10153919A1 DE10153919A1 DE10153919A DE10153919A DE10153919A1 DE 10153919 A1 DE10153919 A1 DE 10153919A1 DE 10153919 A DE10153919 A DE 10153919A DE 10153919 A DE10153919 A DE 10153919A DE 10153919 A1 DE10153919 A1 DE 10153919A1
- Authority
- DE
- Germany
- Prior art keywords
- pressure column
- heat exchanger
- transfer fluid
- heat transfer
- low
- 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.)
- Withdrawn
Links
Classifications
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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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
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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
- F25J3/04006—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
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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
- F25J3/04006—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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- 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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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
- F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
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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
- F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
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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
- F25J3/04248—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
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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
- F25J3/04248—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
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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
- F25J3/04436—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
- F25J3/04454—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 a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
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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
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- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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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
- F25J3/04763—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
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same 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
- F25J2200/00—Processes or apparatus using separation by rectification
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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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- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/42—One fluid being nitrogen
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/40—Quasi-closed internal or closed external air refrigeration cycle
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
-
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/50—Quasi-closed internal or closed external oxygen refrigeration cycle
-
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/12—Particular process parameters like pressure, temperature, ratios
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
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Abstract
Description
Die Erfindung betrifft ein Verfahren zur Gewinnung hoch reinen Sauerstoffs aus weniger reinem Sauerstoff in einem Destilliersystem, das eine Hochdrucksäule und eine Niederdrucksäule aufweist, wobei eine Einsatzfraktion aus weniger reinem Sauerstoff in die Hochdrucksäule eingeleitet wird, eine vorgereinigte Sauerstofffraktion aus der Hochdrucksäule in die Niederdrucksäule eingeleitet wird und aus der Niederdrucksäule ein hoch reines Sauerstoffprodukt abgezogen wird, und wobei bei dem Verfahren ferner ein erster Strom eines Wärmeträger-Fluids in einem Hochdrucksäulen-Sumpfverdampfer durch indirekten Wärmeaustausch mit einer verdampfenden Flüssigkeit aus der Hochdrucksäule mindestens teilweise kondensiert, anschließend mindestens zum Teil entspannt und in einem Niederdrucksäulen- Kopfkondensator durch indirekten Wärmeaustausch mit einem kondensierenden Gas aus der Niederdrucksäule mindestens teilweise verdampft wird.The invention relates to a method for obtaining high-purity oxygen from less pure oxygen in a still system that has a high pressure column and having a low pressure column, with a feed fraction from less pure Oxygen is introduced into the high pressure column, a pre-cleaned oxygen fraction is introduced from the high pressure column into the low pressure column and from the Low pressure column a highly pure oxygen product is withdrawn, and with the method further comprises a first stream of a heat transfer fluid in one High pressure column sump evaporator through indirect heat exchange with a evaporating liquid from the high pressure column at least partially condensed, then at least partially relaxed and in a low-pressure column Top condenser through indirect heat exchange with a condensing gas is at least partially evaporated from the low pressure column.
Unter "weniger reinem Sauerstoff" wird hier eine Fraktion verstanden, die
hauptsächlich aus Sauerstoff besteht, aber noch verschiedene Verunreinigungen
enthält, die leichter und schwerer als Sauerstoff sieden. Es kann sich beispielsweise
um Sauerstoff technischer Reinheit, insbesondere einer Reinheit von etwa 99,5 mol%,
handeln. Das hoch reine Sauerstoffprodukt enthält weniger Verunreinigungen als das
Einsatzgemisch. Es kann beispielsweise noch die folgenden Verunreinigungen
aufweisen:
"Less pure oxygen" is understood here to mean a fraction which consists mainly of oxygen but still contains various impurities that boil more easily and heavily than oxygen. It can be, for example, technical-grade oxygen, in particular a purity of about 99.5 mol%. The highly pure oxygen product contains fewer impurities than the feed mixture. For example, it can still contain the following impurities:
Ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung sind aus JP 04139004 bekannt. Das Destilliersystem zur Sauerstoff-Reinigung wird hier mittels eines Kreislaufs beheizt und gekühlt, der vermutlich mit Stickstoff betrieben wird. Zwischen Hochdrucksäule und Niederdrucksäule ist ein weiterer Kondensator- Verdampfer (Hauptkondensator) angeordnet, in dem Sumpfflüssigkeit der Niederdrucksäule gegen kondensierendes Kopfgas der Hochdrucksäule verdampft wird.A method of the type mentioned and a corresponding device are known from JP 04139004. The distillation system for oxygen purification is here heated and cooled by means of a circuit, which is presumably operated with nitrogen will. Between the high pressure column and the low pressure column there is another condenser Evaporator (main condenser) arranged in the sump liquid of the Low pressure column evaporated against condensing head gas of the high pressure column will.
Der Erfindung liegt die Aufgabe zugrunde, ein derartiges System anzugeben, das besonders effizient arbeitet.The invention is based on the object of specifying such a system that works particularly efficiently.
Diese Aufgabe wird dadurch gelöst, dass das Wärmeträger-Fluid stromabwärts des Hochdrucksäulen-Sumpfverdampfers und stromaufwärts der Entspannung in einem Unterkühlungs-Wärmetauscher durch indirekten Wärmeaustausch abgekühlt wird.This object is achieved in that the heat transfer fluid downstream of the High pressure column sump evaporator and upstream of the expansion in one Subcooling heat exchanger is cooled by indirect heat exchange.
Durch den Wärmeaustausch in dem Unterkühlungs-Wärmetauscher wird das in dem Hochdrucksäulen-Sumpfverdampfer verflüssigte Wärmeträger-Fluid unterkühlt, also auf eine Temperatur unterhalb seines Siedepunkts gebracht. Bei der anschließenden Entspannung (vorzugsweise in einem Drosselventil) entsteht dadurch weniger Flashgas. Entsprechend mehr Flüssigkeit steht zur Kühlung des Niederdrucksäulen- Kopfkondensators zur Verfügung. Dadurch wird die Effizienz des Verfahrens verbessert, indem entweder die Rücklaufmenge und damit die Trennwirkung in der Niederdrucksäule erhöht wird, oder indem - bei gleichbleibender Kühlleistung des Niederdrucksäulen-Kopfkondensators die Menge an Wärmeträger-Fluid und damit der Energieverbrauch verringert wird. (Selbstverständlich können diese beiden Effekte auch kombiniert werden.)Due to the heat exchange in the subcooling heat exchanger, this is achieved in the High-pressure column sump evaporator liquefied heat transfer fluid is supercooled, ie brought to a temperature below its boiling point. In the subsequent There is less relaxation (preferably in a throttle valve) Flash gas. Correspondingly more liquid is available for cooling the low-pressure column Head capacitor available. This increases the efficiency of the procedure improved by either the return flow and thus the separation effect in the Low-pressure column is increased, or by - with the cooling capacity of the Low pressure column top condenser the amount of heat transfer fluid and thus the Energy consumption is reduced. (Of course, these two effects can can also be combined.)
Die beiden Kondensator-Verdampfer (Hochdrucksäulen-Sumpfverdampfer und Niederdrucksäulen-Kopfkondensator) können unmittelbar im Sumpf beziehungsweise am Kopf der entsprechenden Säulen angeordnet sein. Alternativ kann eine oder jeder der beiden Kondensator-Verdampfer getrennt von den Säulen in einem separaten Behälter angeordnet sein.The two condenser-evaporators (high pressure column sump evaporator and Low-pressure column top condenser) can be placed directly in the sump respectively be arranged at the head of the corresponding pillars. Alternatively, one or each the two condenser-evaporators separated from the columns in a separate one Be arranged container.
Das Wärmeträger-Fluid kann bei der Erfindung beispielsweise durch Stickstoff, Sauerstoff, Luft oder jedes andere Gemisch aus Luftkomponenten gebildet werden. Das im Niederdrucksäulen-Kopfkondensator verdampfte Wärmeträger-Fluid wird (gegebenenfalls nach Anwärmung) in die Atmosphäre abgeblasen und/oder in einem Kreislaufverdichter rückverdichtet und wieder dem Hochdrucksäulen-Sumpfverdampfer zugeführt. In the invention, the heat transfer fluid can be, for example, nitrogen, Oxygen, air or any other mixture of air components can be formed. The heat transfer fluid evaporated in the low-pressure column top condenser is (if necessary after warming up) blown into the atmosphere and / or in one Recompressed cycle compressor and back to the high pressure column sump evaporator fed.
Bevorzugte Wertebereiche für die Drücke bei dem erfindungsgemäßen Verfahren sind:
Hochdrucksäule (im Sumpf):
beispielsweise 2,0 bis 3,0 bar, vorzugsweise etwa 2,5 bar
Niederdrucksäule (im Sumpf):
beispielsweise 1,1 bis 1,9 bar, vorzugsweise etwa 1,5 bar
Wärmeträger-Fluid im Hochdrucksäulen-Sumpfverdampfer (Verflüssigungsraum):
beispielsweise 5 bis 9 bar, vorzugsweise etwa 7 bar
Wärmeträger-Fluid im Niederdrucksäulen-Kopfkondensator (Verdampfungsraum):
beispielsweise 2 bis 4 bar, vorzugsweise etwa 3 barPreferred ranges of values for the pressures in the process according to the invention are:
High pressure column (in the sump):
for example 2.0 to 3.0 bar, preferably about 2.5 bar
Low pressure column (in the sump):
for example 1.1 to 1.9 bar, preferably about 1.5 bar
Heat transfer fluid in the high pressure column sump evaporator (liquefaction chamber):
for example 5 to 9 bar, preferably about 7 bar
Heat transfer fluid in the low-pressure column top condenser (evaporation chamber):
for example 2 to 4 bar, preferably about 3 bar
Vorzugsweise wird gasförmiges Wärmeträger-Fluid, das aus dem Niederdrucksäulen- Kopfkondensator abgezogen wurde, in dem Unterkühlungs-Wärmetauscher angewärmt. Dieser Dampf stellt die kälteste Fraktion in dem Destilliersystem dar und bewirkt damit eine besonders starke Unterkühlung des flüssigen Wärmeträger-Fluids.Preferably, gaseous heat transfer fluid, which from the low pressure column Top condenser was withdrawn in the subcooling heat exchanger warmed up. This vapor represents the coldest fraction in the still system and thus causes a particularly strong subcooling of the liquid heat transfer fluid.
Der Unterkühlungs-Wärmetauscher wird bei der Erfindung durch einen Wärmetauscherblock gebildet, der von den beiden Kondensator-Verdampfern (Hochdrucksäulen-Sumpfverdampfer und Niederdrucksäulen-Kopfkondensator) getrennt ist. Er kann vollständig separat ausgeführt sein. Es ist jedoch günstig, ihn mit einem anderen Wärmeaustauschvorgang zu kombinieren. Wenn zum Beispiel das Wärmeträger-Fluid stromaufwärts des Hochdrucksäulen-Sumpfverdampfers in einem Hauptwärmetauscher abgekühlt wird, ist es vorteilhaft, wenn der Hauptwärmetauscher und der Unterkühlungs-Wärmetauscher durch einen integrierten Wärmetauscherblock gebildet werden. Dies gilt insbesondere dann, wenn ein Strom, der sowohl im Unterkühlungs-Wärmetauscher, als auch im Hauptwärmetauscher angewärmt wird, durch die gleiche Fraktion gebildet wird, beispielsweise durch gasförmiges Wärmeträger-Fluid, das aus dem Niederdrucksäulen-Kopfkondensator abgezogen wurde. Dieses kann dann nacheinander den Unterkühlungs-Wärmetauscher- und den Hauptwärmetauscher-Abschnitt des integrierten Wärmetauschers in derselben Passage durchströmen.The subcooling heat exchanger is in the invention by a Heat exchanger block formed by the two condenser-evaporators (High pressure column sump evaporator and low pressure column top condenser) is separated. It can be carried out completely separately. However, it is convenient to have him with you combine with another heat exchange process. For example if that Heat transfer fluid upstream of the high pressure column sump evaporator in one Main heat exchanger is cooled, it is advantageous if the main heat exchanger and the subcooling heat exchanger through an integrated heat exchanger block are formed. This is especially true when a current that is both im Subcooling heat exchanger, as well as being heated in the main heat exchanger, is formed by the same fraction, for example by gaseous Heat transfer fluid withdrawn from the low pressure column top condenser became. This can then successively the subcooling heat exchanger and the Main heat exchanger section of the integrated heat exchanger in the same Flow through passage.
Die Wirkung der Erfindung kann weiter verbessert werden, indem das Wärmeträger- Fluid stromabwärts des Hochdrucksäulen-Sumpfverdampfers und stromaufwärts der Entspannung in einem weiteren Unterkühlungs-Wärmetauscher durch indirekten Wärmeaustausch abgekühlt wird. Unter dem "weiteren Unterkühlungs-Wärmetauscher" ist ein vom bisher beschriebenen, ersten Unterkühlungs-Wärmetauscher getrennter Wärmetauscher zu verstehen, indem insbesondere eine andere Fraktion als in dem ersten Unterkühlungs-Wärmetauscher angewärmt wird.The effect of the invention can be further improved by the heat transfer medium Fluid downstream of the high pressure column sump evaporator and upstream of the Relaxation in another supercooling heat exchanger through indirect Heat exchange is cooled. Under the "further subcooling heat exchanger" is a separate from the first supercooling heat exchanger described so far To understand heat exchangers, in particular by a different fraction than in that first supercooling heat exchanger is heated.
Vorzugsweise wird in dem weiteren Unterkühlungs-Wärmetauscher eine flüssige Fraktion aus der Niederdrucksäule angewärmt, wobei insbesondere stromaufwärts des weiteren Unterkühlungs-Wärmetauschers eine Druckerhöhung in der flüssigen Fraktion durchgeführt wird. Dabei kann es sich beispielsweise um hoch reines Sauerstoffprodukt handeln, das flüssig aus der Niederdrucksäule abgezogen, in einer Pumpe auf über Niederdrucksäulen-Druck gebracht und anschließend in den weiteren Unterkühlungs-Wärmetauscher eingeführt wird.A liquid heat exchanger is preferably used in the further subcooling heat exchanger Fraction from the low pressure column warmed, in particular upstream of the Another supercooling heat exchanger increases the pressure in the liquid fraction is carried out. It can be, for example, highly pure Act oxygen product, the liquid withdrawn from the low pressure column, in a Pump brought to over low pressure column pressure and then in the other Subcooling heat exchanger is introduced.
Der erste Strom des Wärmeträger-Fluids kann in dem Hochdrucksäulen- Sumpfverdampfer vollständig oder im Wesentlichen vollständig kondensiert werden. Falls das Wärmeträger-Fluid durch ein Mehrkomponenten-Gemisch gebildet wird, kann es jedoch vorteilhaft sein, das Wärmeträger-Fluid in dem in dem Hochdrucksäulen- Sumpfverdampfer nur teilweise zu verflüssigen, beispielsweise zu 10 bis 50 mol%. Dadurch wird die Verdampfungstemperatur erhöht beziehungsweise umgekehrt genügt ein geringerer Druck im Wärmeträger-Fluid.The first stream of the heat transfer fluid can be in the high pressure column Bottom evaporator are completely or essentially completely condensed. If the heat transfer fluid is formed by a multi-component mixture, can however, it may be advantageous to use the heat transfer fluid in the high-pressure column To liquefy bottom evaporator only partially, for example to 10 to 50 mol%. This increases the evaporation temperature or, conversely, is sufficient a lower pressure in the heat transfer fluid.
Der gasförmig verbliebene Teil des ersten Stroms des Wärmeträger-Fluids kann in einem anderen Kondensator verflüssigt werden, beispielsweise in einem Hauptkondensator, über den Hochdrucksäule und Niederdrucksäule in wärmetauschender Verbindung stehen. Der separat verflüssigte Teil des ersten Stroms des Wärmeträger-Fluids kann ebenfalls dem Niederdrucksäulen-Kopfkondensator zugeführt werden. Vorzugsweise werden die beiden kondensierten Teile des Wärmeträger-Fluids vorher gemeinsam unterkühlt.The part of the first stream of the heat transfer fluid remaining in gaseous form can be used in be liquefied in another condenser, for example in one Main condenser, above the high pressure column and low pressure column in heat-exchanging connection. The separately liquefied part of the first stream of the heat transfer fluid can also go to the low-pressure column top condenser are fed. Preferably, the two condensed parts of the Heat transfer fluids previously supercooled together.
In einer anderen Variante des erfindungsgemäßen Verfahrens wird das Wärmeträger- Fluid stromaufwärts des Hochdrucksäulen-Sumpfverdampfers in den ersten Strom und in einen zweiten Strom aufgeteilt, wobei der zweite Strom in einem weiteren Kondensator-Verdampfer verflüssigt wird, in dem eine Fraktion aus der Niederdrucksäule verdampft wird. Dadurch wird die Heizleistung des Wärmeträger- Fluids nicht ausschließlich auf die Hochdrucksäule übertragen, sondern zwischen Hochdrucksäule und Niederdrucksäule aufgeteilt. Die Hochdrucksäule kann somit zum einen einen geringeren Durchmesser aufweisen; zum anderen ist es möglich, über die Aufteilung des Wärmeträger-Fluids die Konzentration an schwererflüchtigen Komponenten (zum Beispiel Kohlenwasserstoffe und/oder Argon) in den Säulensümpfen gezielt einzustellen. Beide Ströme können stromabwärts ihrer Kondensation in den Niederdrucksäulen-Kopfkondensator eingeführt werden; vorzugsweise werden sie auch gemeinsam unterkühlt.In another variant of the method according to the invention, the heat transfer medium Fluid upstream of the high pressure column sump evaporator in the first stream and divided into a second stream, the second stream in a further Condenser-evaporator is liquefied, in which a fraction from the Low pressure column is evaporated. This increases the heating capacity of the heat transfer medium Fluids are not only transferred to the high-pressure column, but between Split high pressure column and low pressure column. The high pressure column can thus to have a smaller diameter; on the other hand, it is possible to use the Distribution of the heat transfer fluid, the concentration of less volatile Components (for example hydrocarbons and / or argon) in the Targeted adjustment of column sumps. Both streams can be downstream of their Introducing condensation into the low pressure column top condenser; preferably they are also supercooled together.
Die Verfahrensweisen der Ansprüche 6 und 7 sowie die Verwendung eines weniger als 90% Stickstoff enthaltenden stellen Merkmale dar, die auch ohne den in Anspruch 1 beschriebenen Unterkühlungsschritt vorteilhaft sind.The procedures of claims 6 and 7 as well as the use of a less than 90% nitrogen-containing are features that would also be possible without the claim 1 supercooling step described are advantageous.
Insbesondere dann, wenn das erfindungsgemäße Verfahren in eine Anlage zur Tieftemperatur-Zerlegung von Luft eingebunden ist, kann es günstig sein, wenn gasförmiges Wärmeträger-Fluid, das aus dem Niederdrucksäulen-Kopfkondensator abgezogen wurde, arbeitsleistend entspannt wird, gegebenenfalls stromabwärts seiner Anwärmung in Unterkühlungs-Wärmetauscher. Vor seiner arbeitsleistenden Entspannung kann das verdampfte Wärmeträger-Fluid beispielsweise mit einer Restfraktion aus der Luftzerlegung im engeren Sinne vermischt werden. Auf diese Weise kann der verbleibende Druck des Wärmeträger-Fluids ausgenutzt werden, vorzugsweise mit Hilfe einer ohnehin vorhandenen Maschine.In particular, when the inventive method in a plant for If low-temperature decomposition of air is involved, it can be beneficial if gaseous heat transfer fluid emerging from the low-pressure column top condenser was withdrawn, is relaxed to perform work, possibly downstream of his Warming up in subcooling heat exchangers. Before his job The evaporated heat transfer fluid can, for example, be expanded with a Residual fraction from the air separation in the narrower sense are mixed. To this Way, the remaining pressure of the heat transfer fluid can be used, preferably with the help of an already existing machine.
Die Erfindung betrifft außerdem eine Vorrichtung zur Tieftemperaturzerlegung von Luft gemäß Patentanspruch 9.The invention also relates to a device for the cryogenic separation of air according to claim 9.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand von in den Zeichnungen schematisch dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:The invention and further details of the invention are based on the following of exemplary embodiments shown schematically in the drawings explained. Here show:
Fig. 1 ein erstes Ausführungsbeispiel der Erfindung, Fig. 1 shows a first embodiment of the invention,
Fig. 2 ein weiteres Ausführungsbeispiel mit zwei Unterkühlungs- Wärmetauschern, Fig. 2 shows a further embodiment with two supercooling heat exchangers,
Fig. 3 eine Variante mit nur partieller Kondensation des Wärmeträger-Fluids, Fig. 3 shows a variant with only partial condensation of the heat transfer fluid,
Fig. 4 eine andere Variante mit Aufteilung des Wärmeträger-Fluids vor dem Hochdrucksäulen-Sumpfverdampfer und Fig. 4 shows another variant with division of the heat transfer fluid before the high-pressure column bottom reboiler and
Fig. 5 ein Beispiel für die Einbindung des erfindungsgemäßen Systems gemäß Fig. 1 in einer Tieftemperatur-Luftzerlegungsanlage. FIG. 5 shows an example of the integration of the system according to the invention according to FIG. 1 in a low-temperature air separation plant.
In dem Verfahren von Fig. 1 wird über Leitung 1 flüssiger Sauerstoff einer Reinheit von beispielsweise 99,5 mol% in eine Hochdrucksäule 2 eingeführt, vorzugsweise an einer Zwischenstelle unterhalb der Mitte der Hochdrucksäule. Die Hochdrucksäule 2 ist Teil eines Destilliersystems, das außerdem eine Niederdrucksäule 3, einen Hochdrucksäulen-Sumpfverdampfer 4, einen Niederdrucksäulen-Kopfkondensator 6 und einen weiteren Kondensator-Verdampfer (Hauptkondensator) 5 umfasst. Im Hochdrucksäulen-Sumpfverdampfer 4 wird durch indirekten Wärmeaustausch aufsteigender Dampf erzeugt. Kontinuierlich oder intermittierend wird über Leitung 7 Spülflüssigkeit abgezogen. Mit ihr werden schwererflüchtige Verunreinigungen aus dem Verfahren entfernt. Das Kopfgas 8 enthält praktisch keine schwererflüchtigen Komponenten mehr und wird im Hauptkondensator 5 mindestens teilweise, vorzugsweise vollständig gegen verdampfende Sumpfflüssigkeit der Niederdrucksäule verflüssigt. Dabei gebildetes Kondensat 9 wird zu einem ersten Teil 10 als Rücklauf auf die Hochdrucksäule 2 aufgegeben. Der Rest wird als vorgereinigte Sauerstofffraktion 11 über ein Drosselventil 12 in die Niederdrucksäule 3 eingeführt, und zwar vorzugsweise an einer Zwischenstelle oberhalb der Mitte der Niederdrucksäule.In the process of FIG. 1, liquid oxygen with a purity of, for example, 99.5 mol% is introduced into a high-pressure column 2 via line 1 , preferably at an intermediate point below the center of the high-pressure column. The high-pressure column 2 is part of a distillation system which also comprises a low-pressure column 3 , a high- pressure column bottom evaporator 4 , a low-pressure column top condenser 6 and a further condenser-evaporator (main condenser) 5. In the high-pressure column sump evaporator 4 , rising steam is generated by indirect heat exchange. Rinsing liquid is drawn off continuously or intermittently via line 7. It removes less volatile impurities from the process. The top gas 8 practically no longer contains any less volatile components and is at least partially, preferably completely, liquefied in the main condenser 5 against the evaporating bottom liquid of the low-pressure column. The condensate 9 formed in the process is fed to a first part 10 as a return to the high-pressure column 2 . The remainder is introduced into the low-pressure column 3 as a pre-cleaned oxygen fraction 11 via a throttle valve 12 , specifically preferably at an intermediate point above the center of the low-pressure column.
Das Kopfgas 13 der Niederdrucksäule wird in dem Niederdrucksäulen- Kopfkondensator 6 zum großen Teil kondensiert. Das Kondensat 14 wird zum Niederdrucksäulen-Kopf zurückgeleitet, während der gasförmige verbliebene Anteil 15, der die leichterflüchtigen Verunreinigungen enthält, als Restdampf abgezogen wird. Aus dem Sumpf der Niederdrucksäule 3 wird über Leitung 16 hoch reines Sauerstoffprodukt HLOX flüssig abgezogen, gegebenenfalls gefördert mittels eine Pumpe 17.The top gas 13 of the low-pressure column is largely condensed in the low-pressure column top condenser 6. The condensate 14 is returned to the low-pressure column head, while the gaseous remaining portion 15 , which contains the more volatile impurities, is drawn off as residual vapor. Highly pure oxygen product HLOX is withdrawn in liquid form from the bottom of the low-pressure column 3 via line 16 , if necessary conveyed by means of a pump 17 .
Über Leitung 101 wird ein Wärmeträger-Fluid herangeführt und über Leitung 102 zu einem Hauptwärmetauscher 104 geleitet, der Teil eines integrierten Wärmeaustauschers 103 ist. Dort wird das Wärmeträger-Fluid 102 in indirektem Wärmeaustausch gegen Wärmeträger-Fluid 111 vom Niederdrucksäulen- Kopfkondensator und gegen Restdampf 15 angewärmt. (Letzterer wird nach seiner Anwärmung über Leitung 117 in die Atmosphäre abgeblasen.) Vom kalten Ende des Hauptwärmetauschers 104 strömt das Wärmeträger-Fluid über Leitung 106 zum Hochdrucksäulen-Sumpfverdampfer 4 und wird dort vollständig verflüssigt. Das kondensiert Wärmeträger-Fluid 107, 108 wird in einem Drosselventil 109 entspannt und in den Verdampfungsraum des Niederdrucksäulen-Kopfkondensators 6 eingespeist. Dort verdampft es vollständig oder zum größten Teil. (Nicht verdampfte Anteile können kontinuierlich oder intermittierend über eine Spülleitung 110 abgezogen werden.) Das in dem Niederdrucksäulen-Kopfkondensator gebildete gasförmige Wärmeträger-Fluid 111 wird in dem integrierten Wärmeaustauscher 103 auf etwa Umgebungstemperatur angewärmt und über die Leitungen 112 und 113 in die Atmosphäre abgeblasen. Alternativ kann das gesamte warme gasförmige Wärmeträger-Fluid 112 oder ein Teil davon über Leitung 114 im Kreislauf geführt werden. Zumindest in diesem Fall ist zusätzlich ein Kreislaufverdichter 115 mit Nachkühler 116 notwendig.A heat transfer fluid is brought in via line 101 and passed via line 102 to a main heat exchanger 104 , which is part of an integrated heat exchanger 103 . There, the heat transfer fluid 102 is heated in an indirect heat exchange against heat transfer fluid 111 from the low-pressure column top condenser and against residual steam 15. (The latter is blown off into the atmosphere via line 117 after it has been heated.) From the cold end of the main heat exchanger 104 , the heat transfer fluid flows via line 106 to the high-pressure column sump evaporator 4 and is completely liquefied there. The condensed heat transfer fluid 107 , 108 is expanded in a throttle valve 109 and fed into the evaporation chamber of the low-pressure column top condenser 6. There it evaporates completely or for the most part. (Non-evaporated portions can be withdrawn continuously or intermittently via a flushing line 110. ) The gaseous heat transfer fluid 111 formed in the low-pressure column top condenser is warmed to approximately ambient temperature in the integrated heat exchanger 103 and vented into the atmosphere via the lines 112 and 113. Alternatively, the entire warm gaseous heat transfer fluid 112 or a part thereof can be circulated via line 114. At least in this case, a circulation compressor 115 with an aftercooler 116 is also necessary.
Erfindungsgemäß wird das verflüssigte Wärmeträger-Fluid 107 vor seiner Entspannung 109 in einem Unterkühlungs-Wärmetauscher 105 unterkühlt. Die Kälte liefert das gasförmige Wärmeträger-Fluid 111 vom Niederdrucksäulen-Kopfkondensator 6. Der Unterkühlungs-Wärmetauscher 105 ist in dem Ausführungsbeispiel Teil des integrierten Wärmeaustauschers 103. Alternativ könnten Hauptwärmetauscher 104 und Unterkühlungs-Wärmetauscher 105 durch zwei getrennte Wärmeaustauscherblöcke realisiert sein.According to the invention, the liquefied heat transfer fluid 107 is supercooled in a supercooling heat exchanger 105 before it is expanded 109. The cold supplies the gaseous heat transfer fluid 111 from the low-pressure column top condenser 6 . The supercooling heat exchanger 105 is part of the integrated heat exchanger 103 in the exemplary embodiment. Alternatively, the main heat exchanger 104 and subcooling heat exchanger 105 could be implemented by two separate heat exchanger blocks.
Das Wärmeträger-Fluid 101 wird bei dem Verfahren von Fig. 1 beispielsweise durch Luft, Stickstoff oder Sauerstoff gebildet, oder aber durch eine beliebige Mischung dieser Einzelkomponenten.In the method of FIG. 1, the heat transfer fluid 101 is formed, for example, by air, nitrogen or oxygen, or by any desired mixture of these individual components.
Die Flashgasmenge wird bei dem Ausführungsbeispiel der Fig. 1 durch die erfindungsgemäße Unterkühlung des Wärmeträger-Fluids um 4% verringert.In the exemplary embodiment of FIG. 1, the amount of flash gas is reduced by 4% as a result of the subcooling of the heat transfer fluid according to the invention.
Fig. 2 unterscheidet sich von Fig. 1 durch einen weiteren Unterkühlungs- Wärmetauscher 240, der stromaufwärts des bisher beschriebenen ersten Unterkühlungs-Wärmetauschers 105 angeordnet ist und die Unterkühlung des flüssigen Wärmeträger-Fluids 107 verstärkt. In ihm wird flüssiger hoch reiner Sauerstoff 241, der aus der Niederdrucksäule abgezogen (16) und flüssig auf Druck gebracht (217) wurde, angewärmt. Die angewärmte Flüssigkeit wird schließlich über eine Produktleitung 242 abgeführt. FIG. 2 differs from FIG. 1 by a further subcooling heat exchanger 240 , which is arranged upstream of the first subcooling heat exchanger 105 described so far and which increases the subcooling of the liquid heat transfer fluid 107 . In it, liquid, highly pure oxygen 241 , which has been drawn off from the low-pressure column ( 16 ) and pressurized as a liquid ( 217 ), is heated. The heated liquid is finally discharged via a product line 242.
Fig. 3 basiert ebenfalls auf Fig. 1. Allerdings ist der Prozess von Fig. 3 gezielt auf die Verwendung eines Mehrkomponenten-Gemischs wie zum Beispiel Luft als Wärmeträger-Fluid ausgelegt. Hierbei wird das Wärmeträger-Fluid 106 im Hochdrucksäulen-Sumpfverdampfer 4 nur teilweise kondensiert (beispielsweise zu 10 bis 50 mol%). Der gasförmig verbliebene Anteil wird über Leitung 350 zum Hauptkondensator 305 geleitet. Dieser enthält zusätzliche Passagen, in den das Gas 350 gegen verdampfende Sumpfflüssigkeit der Niederdrucksäule kondensiert wird. Die entstandene Flüssigkeit 351 wird mit dem Kondensat 352 aus dem Hochdrucksäulen- Sumpfverdampfer 4 vermischt und strömt wie in Fig. 1 über Leitung 107 zum Unterkühlungs-Wärmetauscher 105 und weiter (108, 109) zum Niederdrucksäulen- Kopfkondensator 6. FIG. 3 is also based on FIG. 1. However, the process of FIG. 3 is specifically designed for the use of a multicomponent mixture such as, for example, air as the heat transfer fluid. Here, the heat transfer fluid 106 is only partially condensed in the high pressure column bottom evaporator 4 (for example 10 to 50 mol%). The portion remaining in gaseous form is passed via line 350 to the main condenser 305 . This contains additional passages in which the gas 350 is condensed against the evaporating bottom liquid of the low-pressure column. The resulting liquid 351 is mixed with the condensate 352 from the Hochdrucksäulen- bottom vaporizer 4 flows as in FIG. 1 via line 107 for super-cooling heat exchanger 105 and further (108, 109) for Niederdrucksäulen- head condenser 6.
Eine weitere Abwandlung von Fig. 1 zeigt Fig. 4. Das Wärmeträger-Fluid aus dem Hauptwärmetauscher 104 wird hier in einen ersten Strom 460 und einen zweiten Strom 461 aufgeteilt. Das Mengenverhältnis zwischen erstem und zweitem Strom wird über ein Ventil 462 eingestellt. Beispielsweise 10 bis 40 mol% des Wärmeträger-Fluids 406 werden über die Leitung 461 geführt. Der zweite Strom 461 wird zum Hauptkondensator 405 geleitet. Dieser enthält gegenüber Fig. 1 zusätzliche Passagen, in denen der zweite Strom 461 gegen verdampfende Sumpfflüssigkeit der Niederdrucksäule kondensiert wird. Die entstandene Flüssigkeit 463 wird mit dem Kondensat 464 aus dem Hochdrucksäulen-Sumpfverdampfer 4 vermischt und strömt wie in Fig. 1 über Leitung 107 zum Unterkühlungs-Wärmetauscher 105 und weiter (108, 109) zum Niederdrucksäulen-Kopfkondensator 6.A further modification of FIG. 1 is shown in FIG. 4. The heat transfer fluid from the main heat exchanger 104 is divided into a first stream 460 and a second stream 461 here . The quantitative ratio between the first and second stream is set via a valve 462 . For example, 10 to 40 mol% of the heat transfer fluid 406 are conducted via the line 461 . The second stream 461 is directed to the main capacitor 405 . Compared to FIG. 1, this contains additional passages in which the second stream 461 is condensed against the evaporating bottom liquid of the low-pressure column. The resulting liquid 463 is mixed with the condensate 464 from the high-pressure column bottom evaporator 4 and, as in FIG. 1, flows via line 107 to the supercooling heat exchanger 105 and further ( 108 , 109 ) to the low-pressure column top condenser 6 .
Das Verfahren und die Vorrichtung der Erfindung können beispielweise im Anschluss an eine Tieftemperatur-Luftzerlegungsanlage betrieben werden, indem deren Sauerstoffprodukt als weniger reiner Sauerstoff in die Hochdrucksäule eingeführt wird, in Gas- und/oder in Flüssigform. Besonders interessant ist die Erfindung jedoch im Zusammenhang mit der Aufrechterhaltung einer Notversorgung an einer Luftzerlegungsanlage, die im Normalbetrieb den hoch reinen Sauerstoff selbst erzeugt. Fällt die Luftzerlegungsanlage aus, kann das hoch reine Produkt in der Regel nicht oder nur unter hohem Aufwand über Tankwagen oder Rohrleitungen herangeführt werden. In diesem Fall ist es günstig, leicht verfügbaren weniger reinen Sauerstoff technischer Qualität heranzuführen und vor Ort erfindungsgemäß zu reinigen. Dazu wird er beispielsweise aus einem Flüssigtank entnommen und flüssig in die Hochdrucksäule eingespeist. Das erfindungsgemäße Verfahren kommt dabei weitgehend ohne äußere Energiezufuhr, rotierende Maschinen und komplizierte Regelung aus, lediglich der Druck des Wärmeträger-Fluids muss ausreichen, um den Betrieb des Hochdrucksäulen-Sumpfverdampfers sicherzustellen. Dies kann beispielsweise durch die Verwendung von Stickstoff aus einem als Wärmeträger-Fluid bewerkstelligt werden, wenn dieser flüssig aus dem Tank entnommen und anschließend verdampft wird. Wegen der hohen Anforderungen an die Verfügbarkeit des hoch reinen Sauerstoffs ist die Erfindung insbesondere für Onsite-Anlagen zur Belieferung von Einrichtungen zur Halbleiter-Produktion geeignet.The method and the device of the invention can, for example, subsequently operated to a cryogenic air separation plant by its Oxygen product is introduced into the high pressure column as less pure oxygen, in gas and / or in liquid form. However, the invention is particularly interesting in Relation to the maintenance of emergency care at a Air separation plant that generates the high-purity oxygen itself during normal operation. If the air separation plant fails, the highly pure product usually cannot or only brought in with great effort via tank trucks or pipelines will. In this case it is beneficial to have less pure oxygen readily available of technical quality and to be cleaned on site according to the invention. In addition For example, if it is removed from a liquid tank and poured into the High pressure column fed. The method according to the invention comes here largely without external energy supply, rotating machines and complicated Regulation off, only the pressure of the heat transfer fluid must be sufficient to Ensure operation of the high pressure column sump evaporator. This can for example through the use of nitrogen from a heat transfer fluid be accomplished when this liquid is removed from the tank and is then evaporated. Because of the high demands on availability of the highly pure oxygen, the invention is particularly suitable for on-site systems Supply of facilities for semiconductor production suitable.
Die Einbindung des erfindungsgemäßen Systems in eine Tieftemperatur- Luftzerlegungsanlage ist in Fig. 5 dargestellt. Rechts in der Zeichnung ist das Destilliersystem 2, 3, 4, 5, 6 der Fig. 1 abgebildet. Alternativ könnten auch die in den Fig. 2 bis 4 beschriebenen Varianten um Zusammenhang mit der Luftzerlegungsanlage (LZA) im engeren Sinne eingesetzt werden, die im Folgenden näher erläutert wird.The integration of the system according to the invention in a low-temperature air separation plant is shown in FIG . The distillation system 2 , 3 , 4 , 5 , 6 of FIG. 1 is shown on the right in the drawing. Alternatively, the variants described in FIGS. 2 to 4 could also be used in connection with the air separation plant (LZA) in the narrower sense, which is explained in more detail below.
Verdichtete und gereinigte Luft 540 wird in einem Hauptwärmetauscher 541 auf etwa Taupunkt abgekühlt und strömt über die Leitungen 542, 543 teilweise in die LZA- Hochdrucksäule 544 eines Zwei-Säulen-Luftzerlegers 544/545. Gasförmiger Kopfstickstoff 546 der LZA-Hochdrucksäule 544 wird zu einem ersten Teil 547 in einem LZA-Hauptkondensator 548 und zu einem zweiten Teil 549 in einem Nebenkondensator 550 verflüssigt. Das dabei erzeugte Kondensat 551 wird zu einem ersten Teil 552 als Rücklauf auf die LZA-Hochdrucksäule 544 aufgegeben. Der Rest 553 wird in einem integrierten Unterkühlungs-Wärmetauscher 554 abgekühlt und über Leitung 555 in den Kopf der LZA-Niederdrucksäule 545 eingedrosselt. Als Sumpfprodukt verlässt flüssiger Rohsauerstoff 556 die LZA-Hochdrucksäule 544, wird in zwei Strömen 557, 559 unterschiedlich stark unterkühlt (in 554) und schließlich in die LZA-Niederdrucksäule 545 (über Leitung 558) beziehungsweise in den Verdampfungsraum eines LZA-Niederdrucksäulen-Kopfkondensators 561 eingespeist. Compressed and purified air 540 is cooled in a main heat exchanger 541 to about dew point and flows through the lines 542, 543 partially into the LTA high pressure column 544 of a two-column air separation plant 544/545. Gaseous overhead nitrogen 546 of the LZA high pressure column 544 is liquefied to a first part 547 in an LZA main condenser 548 and to a second part 549 in a secondary condenser 550. The condensate 551 generated in this way is fed to a first part 552 as a return to the LZA high-pressure column 544 . The remainder 553 is cooled in an integrated supercooling heat exchanger 554 and throttled into the top of the LZA low-pressure column 545 via line 555. As a bottom product, liquid crude oxygen 556 leaves the LZA high pressure column 544 , is supercooled to different degrees in two streams 557 , 559 (in 554) and finally into the LZA low pressure column 545 (via line 558 ) or into the evaporation chamber of an LZA low pressure column top condenser 561 fed in.
Der LZA-Niederdrucksäule 545 werden flüssiger Sauerstoff 565 am Sumpf und flüssiger Stickstoff 564 einige Böden unterhalb des Kopfs entnommen. Der flüssige Stickstoff 564 wird in einer Pumpe 566 auf einen erhöhten Druck gebracht, im integrierten Unterkühlungs-Wärmetauscher 554 angewärmt und über Leitung 567 in den Verdampfungsraum des Nebenkondensators 550 geleitet. Dampf 568 aus dem Nebenkondensator 550 wird im Hauptwärmetauscher 541 auf etwa Umgebungstemperatur gebracht und über Leitung 569 als gasförmiges hoch reines Stickstoffprodukt (GAN) abgezogen. Flüssig verbliebener Stickstoff 582 fließt in die LZA-Hochdrucksäule 544 zurück.The LZA low pressure column 545 is taken from liquid oxygen 565 at the bottom and liquid nitrogen 564 a few floors below the top. The liquid nitrogen 564 is brought to an increased pressure in a pump 566 , warmed in the integrated supercooling heat exchanger 554 and passed via line 567 into the evaporation chamber of the secondary condenser 550. Vapor 568 from the secondary condenser 550 is brought to approximately ambient temperature in the main heat exchanger 541 and withdrawn via line 569 as a gaseous high-purity nitrogen product (GAN). Nitrogen 582 that remained liquid flows back into the LZA high-pressure column 544 .
Vom LZA-Niederdrucksäulen-Kopfkondensator 561 werden ein gasförmiger (562) und ein flüssiger (563) Spülstrom sowie Restgas 590 abgezogen. Letzteres wird in den Wärmeaustauschern 554 und 541 angewärmt und bei 591 aus dem Verfahren entfernt. Außerdem wird der LZA-Niederdrucksäule 545 über Leitung 592 Unrein-Stickstoff als Restfraktion gasförmig entnommen, im integrierten Unterkühlungs-Wärmetauscher 554 angewärmt und über Leitung 593 zum kalten Ende des Hauptwärmetauschers 541 geführt. Bei einer Zwischentemperatur wird die Restfraktion 594 einer Entspannungsmaschine (Restgasturbine) 595 zugeleitet und dort auf etwa Atmosphärendruck arbeitsleistend entspannt. Die Niederdruck-Restfraktion 596 wird auf etwa Umgebungstemperatur angewärmt (541) und schließlich über Leitung 597 abgezogen. Die Leitung 598 ist optional und dient der Regelung des aufsteigenden Dampfs.A gaseous ( 562 ) and a liquid ( 563 ) flushing stream and residual gas 590 are drawn off from the LZA low-pressure column top condenser 561. The latter is heated in heat exchangers 554 and 541 and removed from the process at 591. In addition, impure nitrogen is removed in gaseous form as a residual fraction from the LZA low-pressure column 545 via line 592 , heated in the integrated supercooling heat exchanger 554 and fed via line 593 to the cold end of the main heat exchanger 541 . At an intermediate temperature, the residual fraction 594 is fed to an expansion machine (residual gas turbine) 595 and expanded there to approximately atmospheric pressure to perform work. The low-pressure residual fraction 596 is warmed to approximately ambient temperature ( 541 ) and finally drawn off via line 597 . Line 598 is optional and is used to regulate the rising steam.
Ein erster Strom 583-584 des flüssigen Sauerstoffs 565 wird mittels einer Pumpe 585 in den Verdampfungsraum des LZA-Hauptkondensators 548 gefördert und verdampft dort teilweise. Verdampfter Sauerstoff und verbliebene Flüssigkeit werden gemeinsam über Leitung 586 in die LZA-Niederdrucksäule 545 zurückgeleitet. Ein zweiter Strom 583-587 wird in einer Pumpe 588 auf den gewünschten Produktdruck gebracht (so genannte Innenverdichtung) und im Hauptwärmetauscher 541 verdampft und angewärmt. Über Leitung 589 wird schließlich gasförmiger Drucksauerstoff mit Standard-Reinheit (S-GOX) abgegeben.A first stream 583-584 of the liquid oxygen 565 is conveyed by means of a pump 585 into the evaporation space of the LZA main condenser 548 and partially evaporates there. Evaporated oxygen and remaining liquid are fed back together via line 586 into the LZA low-pressure column 545 . A second stream 583-587 is brought to the desired product pressure in a pump 588 (so-called internal compression) and evaporated and heated in the main heat exchanger 541. Finally, gaseous pressurized oxygen with standard purity (S-GOX) is released via line 589.
Die Betriebsdrücke in der Luftzerlegungsanlage im engeren Sinne betragen etwa 10 bar in der LZA-Hochdrucksäule und etwa 3 bar in der LZA-Niederdrucksäule. The operating pressures in the air separation plant in the narrower sense are approximately 10 bar in the LZA high pressure column and about 3 bar in the LZA low pressure column.
Abweichend von der in Fig. 5 gezeichneten Darstellung können diese beiden Säulen auch als Doppelsäule übereinander angeordnet sein.In a departure from the illustration shown in FIG. 5, these two columns can also be arranged one above the other as a double column.
Ein dritter Strom 1 des flüssigen Sauerstoffs aus der LZA-Niederdrucksäule 545 stellt den "weniger reinen Sauerstoff" im Sinne der Erfindung dar, der als Einsatz in die Hochdrucksäule 2 eingeleitet wird. Der Restdampf 15 vom Kopf der Niederdrucksäule 3 wird mit dem Restgas 590 vom LZA-Niederdrucksäulen-Kopfkondensator 561 vereinigt.A third stream 1 of the liquid oxygen from the LZA low-pressure column 545 represents the “less pure oxygen” in the sense of the invention, which is introduced into the high -pressure column 2 as an input. The residual steam 15 from the top of the low-pressure column 3 is combined with the residual gas 590 from the LZA low-pressure column top condenser 561 .
Als Wärmeträger-Fluid 106 wird ein Teil der abgekühlten Einsatzluft 542 verwendet, der stromaufwärts der LZA-Hochdrucksäule 544 von der Gesamtluft 542 abgenommen und dem Verflüssigungsraum des Hochdrucksäulen-Sumpfverdampfers 4 zugeleitet wird. Im Niederdrucksäulen-Kopfkondensator 6 verdampftes Wärmeträger-Fluid 111 wird mit Unrein-Stickstoff 592 aus der LZA-Niederdrucksäule 545 vermischt und gemeinsam mit diesem arbeitsleistend entspannt (595), was eine weitere Energieeinsparung bewirkt. Der erste Unterkühlungs-Wärmetauscher 105 im Sinne der Erfindung wird durch einen Abschnitt des integrierten Unterkühlungs- Wärmetauschers 554 gebildet, in dem flüssiges Wärmeträger-Fluid 107 aus dem Hochdrucksäulen-Sumpfverdampfer 4 abgekühlt wird. Diese Abkühlung wird hier durch indirekten Wärmeaustausch nicht nur mit Wärmeträger-Fluid-Dampf 111 aus dem Verdampfungsraum des Niederdrucksäulen-Kopfkondensators 6, sondern auch mit gasförmigen Rückströmen aus der Luftzerlegungsanlage im engeren Sinn bewirkt. (In Fig. 5 werden der erste Unterkühlungs-Wärmetauscher der Erfindung und der Unterkühlungs-Gegenströmer des Luftzerlegers durch einen gemeinsamen Block gebildet, den integrierten Unterkühlungs-Wärmetauscher 554.)A portion of the cooled feed air 542 is used as the heat transfer fluid 106 , which is taken from the total air 542 upstream of the LZA high-pressure column 544 and fed to the liquefaction space of the high-pressure column sump evaporator 4. Heat transfer fluid 111 evaporated in the low-pressure column top condenser 6 is mixed with impure nitrogen 592 from the LZA low-pressure column 545 and expanded together with this to perform work ( 595 ), which results in further energy savings. The first subcooling heat exchanger 105 within the meaning of the invention is formed by a section of the integrated subcooling heat exchanger 554 in which the liquid heat transfer fluid 107 from the high-pressure column sump evaporator 4 is cooled. This cooling is brought about here by indirect heat exchange not only with heat transfer fluid vapor 111 from the evaporation chamber of the low-pressure column top condenser 6 , but also with gaseous return flows from the air separation plant in the narrower sense. (In Fig. 5, the first subcooling heat exchanger of the invention and the subcooling countercurrent of the air separator are formed by a common block, the integrated subcooling heat exchanger 554. )
Der flüssige hoch reine Sauerstoff 16 aus der Niederdrucksäule 3 wird in einer Pumpe 517 auf den gewünschten Produktdruck gebracht (innenverdichtet), über Leitung 599 zum Hauptwärmetauscher 541 geleitet, dort verdampft und angewärmt und schließlich über Leitung 600 als gasförmiges hoch reines Produkt (P-GOX) abgeführt. Ein Teil 601 des in 517 gepumpten Sauerstoffs kann auch als hoch reines Flüssigprodukt (P-LOX) gewonnen werden.The liquid, highly pure oxygen 16 from the low-pressure column 3 is brought to the desired product pressure in a pump 517 (internally compressed), passed via line 599 to the main heat exchanger 541 , where it is evaporated and warmed and finally via line 600 as a gaseous, highly pure product (P-GOX ) discharged. A portion 601 of the oxygen pumped into 517 can also be obtained as a highly pure liquid product (P-LOX).
Claims (9)
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
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DE10153919A DE10153919A1 (en) | 2001-11-02 | 2001-11-02 | Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises cooling the heat exchange fluid downstream of the high pressure column sump vaporizer and upstream of a pressure relieving device |
DE10205095A DE10205095A1 (en) | 2001-11-02 | 2002-02-07 | Method and device for producing a high-purity air component |
DE10205096A DE10205096A1 (en) | 2001-11-02 | 2002-02-07 | Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises feeding the less pure oxygen into high pressure column, feeding fraction into a low pressure column and withdrawing highly pure oxygen |
EP02024271A EP1308681A1 (en) | 2001-11-02 | 2002-10-31 | Process and device for the production of an ultra high purity air component |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
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DE10153919A DE10153919A1 (en) | 2001-11-02 | 2001-11-02 | Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises cooling the heat exchange fluid downstream of the high pressure column sump vaporizer and upstream of a pressure relieving device |
Publications (1)
Publication Number | Publication Date |
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DE10153919A1 true DE10153919A1 (en) | 2002-05-08 |
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Family Applications (3)
Application Number | Title | Priority Date | Filing Date |
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DE10153919A Withdrawn DE10153919A1 (en) | 2001-11-02 | 2001-11-02 | Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises cooling the heat exchange fluid downstream of the high pressure column sump vaporizer and upstream of a pressure relieving device |
DE10205096A Withdrawn DE10205096A1 (en) | 2001-11-02 | 2002-02-07 | Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises feeding the less pure oxygen into high pressure column, feeding fraction into a low pressure column and withdrawing highly pure oxygen |
DE10205095A Withdrawn DE10205095A1 (en) | 2001-11-02 | 2002-02-07 | Method and device for producing a high-purity air component |
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Application Number | Title | Priority Date | Filing Date |
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DE10205096A Withdrawn DE10205096A1 (en) | 2001-11-02 | 2002-02-07 | Process for recovering highly pure oxygen from less pure oxygen in a distillation system comprises feeding the less pure oxygen into high pressure column, feeding fraction into a low pressure column and withdrawing highly pure oxygen |
DE10205095A Withdrawn DE10205095A1 (en) | 2001-11-02 | 2002-02-07 | Method and device for producing a high-purity air component |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1363092A1 (en) * | 2002-05-17 | 2003-11-19 | Linde Aktiengesellschaft | Cryogenic air separation process and apparatus |
CN107684828A (en) * | 2017-10-20 | 2018-02-13 | 江苏华益科技有限公司 | A kind of rectifier unit of high pure oxygen 16 |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102007024168A1 (en) * | 2007-05-24 | 2008-11-27 | Linde Ag | Method and apparatus for cryogenic air separation |
DE102007051182A1 (en) * | 2007-10-25 | 2009-04-30 | Linde Aktiengesellschaft | An electronic industrial plant and method for operating an electronic industrial plant |
DE102007051184A1 (en) * | 2007-10-25 | 2009-04-30 | Linde Aktiengesellschaft | Method and apparatus for cryogenic air separation |
DE102007051183A1 (en) * | 2007-10-25 | 2009-04-30 | Linde Aktiengesellschaft | Method for cryogenic air separation |
DE102011113262A1 (en) * | 2011-09-13 | 2013-03-14 | Linde Aktiengesellschaft | Process and apparatus for recovering pressure oxygen by cryogenic separation of air |
KR20220156848A (en) * | 2020-03-23 | 2022-11-28 | 린데 게엠베하 | Processes and plants for cryogenic separation of air |
-
2001
- 2001-11-02 DE DE10153919A patent/DE10153919A1/en not_active Withdrawn
-
2002
- 2002-02-07 DE DE10205096A patent/DE10205096A1/en not_active Withdrawn
- 2002-02-07 DE DE10205095A patent/DE10205095A1/en not_active Withdrawn
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1363092A1 (en) * | 2002-05-17 | 2003-11-19 | Linde Aktiengesellschaft | Cryogenic air separation process and apparatus |
CN107684828A (en) * | 2017-10-20 | 2018-02-13 | 江苏华益科技有限公司 | A kind of rectifier unit of high pure oxygen 16 |
Also Published As
Publication number | Publication date |
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DE10205095A1 (en) | 2003-05-15 |
DE10205096A1 (en) | 2003-05-15 |
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