EP1199532A1 - Drei-Säulen-System zur Tieftemperatur-Zerlegung von Luft - Google Patents
Drei-Säulen-System zur Tieftemperatur-Zerlegung von Luft Download PDFInfo
- Publication number
- EP1199532A1 EP1199532A1 EP01103828A EP01103828A EP1199532A1 EP 1199532 A1 EP1199532 A1 EP 1199532A1 EP 01103828 A EP01103828 A EP 01103828A EP 01103828 A EP01103828 A EP 01103828A EP 1199532 A1 EP1199532 A1 EP 1199532A1
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- EP
- European Patent Office
- Prior art keywords
- pressure column
- oxygen
- medium
- column
- gas turbine
- Prior art date
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
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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
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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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
- 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
- F25J3/04109—Arrangements of compressors and /or their drivers
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
- F25J3/04121—Steam turbine as the prime mechanical driver
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
- F25J3/04127—Gas turbine as the prime mechanical driver
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
- F25J3/04133—Electrical motor as the prime mechanical driver
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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
- F25J3/04151—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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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
- 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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
- F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
- F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04593—The air gas consuming unit is also fed by an air stream
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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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- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/62—Purifying more than one feed stream in multiple adsorption vessels, e.g. for two feed streams at different pressures
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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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- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/54—Oxygen production with multiple pressure O2
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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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- 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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- 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
-
- 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
- F25J2250/50—One fluid being oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
Definitions
- the invention relates to a method for the low-temperature decomposition of air and Power generation.
- the air separation is carried out in a three-pillar system.
- a gas turbine system which is a gas turbine, is used to generate energy (Gas turbine expander), a gas turbine compressor driven by the gas turbine and has a combustion chamber.
- one or more Air separation products used in the energy generation system for example, oxygen generated in the air separator can be used to generate a Fuel gas can be used with which the combustion chamber is loaded, in particular as an oxidizing agent in a coal or heavy oil gasification.
- nitrogen from the air separator can be used to extract coal and / or used in the gas turbine stream; in the latter case Nitrogen is fed into the combustion chamber or into the gas turbine or with the Gas turbine exhaust gas between the combustion chamber and the gas turbine of the combustion chamber mixed.
- the basics of low temperature air separation in general are in the Monograph "Low Temperature Technology” by Hausen / Linde (2nd edition, 1985) and in one Article by Latimer in Chemical Engineering Progress (Vol. 63, No.2, 1967, page 35) described.
- the three-pillar system is preferably one Triple column, in which the head of the high pressure column and the bottom of the Medium pressure column and on the other hand the head of the medium pressure column and the sump of the Low pressure column are in heat-exchanging connection.
- triple columns are also from DE 1041989 or from Springmann, Chem.-Ing.-Techn., 46 (1974), 881 known.
- the invention is also with other column arrangements and / or others Capacitor configurations applicable (see for example EP 768503 A2, DE 2920270 or EP 572962 A or EP 634617 A).
- Capacitor configurations applicable (see for example EP 768503 A2, DE 2920270 or EP 572962 A or EP 634617 A).
- Devices for extracting other air components, in particular from Noble gases can be provided, for example argon extraction.
- the gas turbine compressor brings air to a very high pressure of over about 7 bar, for example of 17 bar.
- This air usually serves as a part Combustion air for the combustion chamber of the gas turbine system.
- Another part is the first feed air stream to be led into air separation.
- a second feed air flow independent of the first in a separate air compressor compressed, preferably to a pressure lower than that Outlet pressure of the gas turbine compressor; this is in itself from EP 717249 A2 known.
- the air compressor is not driven by the gas turbine, but rather for example from an engine or a steam turbine. (The term “not from the However, gas turbine driven "does not exclude that generated in the gas turbine electrical energy is transmitted to an electric motor, which in turn the drives a separate air compressor.)
- such a double column system is based on three columns reduced, which preserves its essential advantages, but the expenditure on equipment greatly reduced.
- the medium-pressure column of the three-column system simultaneously the low pressure part of the double column for the air under the higher pressure as well represents the high pressure part of the double column for the air under the lower pressure So the first feed air flow is introduced into the high pressure column, and the Medium pressure column is both with oxygen-enriched liquid from the High pressure column as well as the second feed air flow.
- Return for the Low pressure column can come from one or more of the following sources: im first condenser formed condensate, in the second main condenser condensate formed, liquid nitrogen flow from an intermediate point of High pressure column, liquid nitrogen flow from an intermediate point of the medium pressure column.
- a liquid nitrogen stream has at least one theoretical bottom below the head of the medium pressure column and the Low pressure column is fed. This is particularly advantageous if in the Low pressure column no pure nitrogen is generated. Between the medium pressure column head and the liquid nitrogen discharge to the low pressure column are, for example, 5 to 20, preferably 10 to 15 practical floors.
- the second oxygen-enriched fraction which is in the Low pressure column is initiated, withdrawn from the high pressure column.
- the first oxygen-enriched fraction (insert for the medium pressure column) and the second oxygen-enriched fraction (insert for the low pressure column) preferably withdrawn together from the bottom of the high pressure column and before their introduction into the medium pressure column or low pressure column.
- an oxygen fraction 1 is generated in the low pressure column is, at least part of the oxygen fraction liquid from the low pressure column removed, brought to an increased pressure in the liquid state and into the Medium pressure column is introduced and that the medium pressure column is an oxygen product is removed.
- the oxygen product is therefore already in the process of being removed from the three-pillar system at an increased pressure. The effort for Further compression on the product pressure is noticeably reduced or can even drop completely.
- the pressurized liquid oxygen fraction from the Low pressure column at least one theoretical floor (for example one to five practical trays) is introduced into the medium pressure column above the sump. This can result in a lower purity in the bottom of the low pressure column than in Medium pressure column sump prevail. With thermal coupling of low pressure column and medium pressure column this enables a relatively high pressure in the low pressure column or a particularly low operating air pressure.
- the oxygen product is liquid from the Stripped medium pressure column, introduced into a secondary condenser and through there indirect heat exchange with a heating medium, especially with nitrogen the high pressure column is at least partially evaporated.
- the oxygen product is often required under a pressure higher than that Operating pressure of the medium pressure column.
- a pressure higher than that Operating pressure of the medium pressure column for example be compressed outside by being gaseous from the medium pressure column or a Secondary condenser, which is operated under medium-pressure column pressure, removed, warmed to about ambient temperature and in an oxygen compressor is compressed.
- the oxygen product or part of it compress inside by flowing it out of the medium pressure column or out of the Secondary condenser is removed, brought to a pressure in the liquid state, which is higher than the operating pressure of the medium pressure column, and under this pressure indirect heat exchange is evaporated.
- the evaporation of the liquid under pressure brought oxygen product can be carried out in the main heat exchanger in which the cooling of the feed air for the high pressure column and the Heating of other products takes place; alternatively, this can be indirect Heat exchange step take place in a separate heat exchanger.
- the heat of vaporization is available through a high pressure flow provided, either by a correspondingly highly compressed part of the feed air or is formed by circulating nitrogen. Because the inner compression also on supercritical pressures, the term "evaporation" is here in another To understand the meaning that also includes pseudo-evaporation.
- a nitrogen fraction can be drawn directly from the high pressure column and / or the Medium pressure column removed, warmed up and obtained as a pressure nitrogen product become.
- the high-pressure column nitrogen can also be internally compressed if necessary, by making the nitrogen fraction liquid from the high pressure column or their Head condenser removed, is brought to a pressure in the liquid state, the is higher than the operating pressure of the high pressure column, and under this pressure indirect heat exchange is evaporated.
- the indirect heat exchange will preferably carried out in the main heat exchanger with high pressure air as the heating fluid.
- the second Feed air flow separate from the first feed air flow only to approximately Operating pressure of the medium pressure column (plus line losses) compressed and without further pressure-changing measures are introduced into the medium pressure column.
- (only) part of the separation air from a gas turbine compressor is delivered (for example the first feed air flow), this saves How energy works.
- a third feed air stream can be compressed to generate process cold, cleaned, cooled, relieved of work and into the low pressure column or in the Medium pressure column are introduced.
- Work relaxation Mechanical energy generated can be used to recompress the third feed air flow be used, for example by using a turbine-booster combination.
- the invention also relates to a combined device for cryogenic decomposition of air and for energy generation according to claim 14.
- An air stream 10 is brought to a pressure in a gas turbine compressor 11, which is at least equal to the operating pressure of the high pressure column 1.
- the gas turbine compressor 11 is part of a gas turbine system. (Part of the air compressed in 11 is branched off as combustion air to the combustion chamber of the gas turbine unit, what is not shown in the drawing).
- a cleaning device 13 preferably a molecular sieve station.
- a first feed air stream 15 is branched off from the cleaned high-pressure air 14, in a main heat exchanger 40 cooled and via line 16 of the high pressure column 1 fed.
- a partial air flow (not shown here) has to be described in detail higher pressure further compressed and downstream of the main heat exchanger 40 be throttled.
- a second feed air stream 20, 24 is through an air compressor 21, a Aftercooler 22 and a separate cleaning device 23 performed, also in Main heat exchanger 40 cooled, but then led into the medium pressure column 2 (25), without throttling or other pressure-changing measures downstream of the second air compressor.
- the second feed air flow needs in the second Air compressor 21 only compresses to approximately the operating pressure of the medium pressure column 2 become.
- the air compressor is not driven by the gas turbine, but rather preferably by means of external energy, for example by an electric motor.
- This is in a post-compressor 31 further compresses and occurs after post-cooling 32 in the Main heat exchanger 40. After cooling to an intermediate temperature, it becomes led out of the main heat exchanger 40 via line 33, in one Turbine 34 relaxed while working and blown into the low-pressure column 3 (35).
- the turbine 34 is mechanically coupled to the post-compressor 31.
- Gaseous nitrogen 41 is generated at the top of the high-pressure column 1. He's going to liquefied a first part 42 in the first main condenser 4. The one won Liquid nitrogen 43 is returned to the high pressure column 1 (line 44) or abandoned to the medium pressure column 2 (line 45). The Liquid nitrogen 45 is in one before the feed 46 into the medium pressure column Supercooling counterflow 47 supercooled. A second part 48 of the top nitrogen 41 the high pressure column is at least partially in a secondary condenser 49 condenses and flows back via line 50 to the high pressure column 1. A third Part 51 of the high pressure column nitrogen 41 is in the main heat exchanger 40 warmed up and obtained via line 52 as a pressure nitrogen product GAN.
- Liquid crude oxygen is obtained in the sump of the high-pressure column 1. This is called deducted oxygen-enriched fraction 53 and - after hypothermia 47 - to one first part 54 as the first oxygen-enriched fraction in the medium pressure column 2 initiated. A second part 56, 57 is after further supercooling 55 in the Throttled low pressure column.
- a second part 61 of the top nitrogen 58 of the medium pressure column is in the Main heat exchanger 40 warmed up and via line 62 - if necessary after Further compression 63 with after-cooling 64 - as a further pressure nitrogen product PGAN won.
- Liquid oxygen of 95% purity is generated in the bottom of the low pressure column. That part of the bottom liquid that is not in the second main condenser 5 is evaporated, flows as an oxygen fraction 67 to a pump 68 and is in there brought liquid state to about medium pressure column pressure. The oxygen fraction 69 is heated under this increased pressure in the supercooling counterflow 47 and introduced into the medium pressure column 2 via line 70. The feed is here immediately above the sump of the medium pressure column. In the swamp, the represents the evaporation space of the first main condenser 4, the Oxygen fraction 70 from the low pressure column with that within the medium pressure column flowing down liquid mixed. The mixture is liquid as line 71 Oxygen product taken, slightly throttled (72), in the Evaporation chamber of the secondary condenser 49 initiated and there partially evaporated.
- a first part 73 of the oxygen product 71 is gaseous from the Auxiliary condenser removed, warmed up in the main heat exchanger and finally delivered via line 74 as a product (GOX). If product printing is desired, which is higher than the medium pressure column pressure, the warmed oxygen product be further compressed in a product compressor 75 (with aftercooler 78) (Outer compression).
- the liquid portion of the oxygen product 71 is discharged via line 79 deducted the evaporation space of the secondary condenser 49 and one Subjected to internal compression. To do this, it is pumped to product pressure in a pump 80 brought about the same as the product pressure of the outer compression or different of this is.
- the high pressure oxygen product 81 is in the main heat exchanger evaporates (or pseudo-evaporates if the product pressure is above the critical pressure lies) and warmed to ambient temperature. This leaves via line 76 internally compressed oxygen product (GOX-IC) the plant. If desired, he can be combined with the oxygen product 74, which is compressed in 75.
- impure nitrogen 82 Another product of the low pressure column 3 is impure nitrogen 82 from the head deducted, in the supercooling countercurrent 55 and 47 and in Main heat exchanger 40 warmed up.
- the warm impure nitrogen 83 (UN2) can be used as unpressurized by-product used as regeneration gas for the cleaning devices 13 and / or 23 used and / or released into the atmosphere.
- Figure 2 is largely identical to Figure 1. However, here is the third Feed air flow 230, 233 in the expansion machine 234 only approximately Medium pressure column pressure relaxed. The relaxed third feed airflow 235 will via line 236 together with the second feed air flow 225 downstream of the Main heat exchanger 40 fed into the medium pressure column 2. A direct air introduction there is no low pressure column 3 in this process variant.
- the cleaning of the two air streams 10, 20 can in principle also be carried out in one be carried out common device. For example, it is possible to Compress the total air initially only to approximately medium pressure column pressure, below this medium pressure, and then the first (and possibly the third) to further compress the air flow from the medium pressure.
- the for the Processes also require cold from work-relieving nitrogen the medium pressure column 2 can be obtained.
- the relaxed medium pressure column nitrogen can then be mixed with the impure nitrogen from the low pressure column 3 and be heated together with this in the main heat exchanger 40.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Power Engineering (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
- Figur 1
- ein erstes Ausführungsbeispiel der Erfindung mit Einblasung von Turbinenluft in die Niederdrucksäule,
- Figur 2
- eine Abwandlung dieses Prozesses mit Einblasung von Turbinenluft in die Mitteldrucksäule und
- Figur 3
- eine weiteres Ausführungsbeispiel der Erfindung mit Einspeisung von gepumptem Niederdrucksäule-Sauerstoff an einer Zwischenstelle der Mitteldrucksäule.
Claims (14)
- Verfahren zur Tieftemperatur-Zerlegung von Luft in einem Drei-Säulen-System, das eine Hochdrucksäule (1), eine Mitteldrucksäule (2) und eine Niederdrucksäule (3) aufweist, und zur Energie-Erzeugung in einem Gasturbinen-System, das eine Gasturbine, einen von der Gasturbine angetriebenen Gasturbinen-Verdichter (11) und eine Brennkammer aufweist, bei dem(a) ein erster Einsatzluftstrom (10, 14, 15, 16) im Gasturbinen-Verdichter (11) verdichtet, gereinigt (13), abgekühlt (40) und in die Hochdrucksäule (1) eingeleitet wird,(b) ein zweiter Einsatzluftstrom (20, 24, 25, 225) in einem nicht von der Gasturbine angetriebenen Luftverdichter (21) verdichtet, gereinigt (23), abgekühlt (40) und in die Mitteldrucksäule (2) eingeführt wird,(c) in der Hochdrucksäule (1) eine erste sauerstoffangereicherte Fraktion (53, 54) erzeugt wird,(d) die erste sauerstoffangereicherte Fraktion (53, 54) in die Mitteldrucksäule (2) eingeleitet wird und bei dem(e) eine zweite sauerstoffangereicherte Fraktion (53, 57) in die Niederdrucksäule (3) eingeleitet wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass gasförmiger Stickstoff (41, 42) aus der Hochdrucksäule (1) in einem ersten Hauptkondensator (4) durch indirekten Wärmeaustausch mit einer sauerstoffreichen Fraktion aus der Niederdrucksäule (3) kondensiert wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass gasförmiger Stickstoff (58, 59) aus der Mitteldrucksäule (2) in einem zweiten Hauptkondensator (5) durch indirekten Wärmeaustausch mit einer sauerstoffreichen Fraktion aus der Niederdrucksäule (3) kondensiert wird.
- Verfahren nach Anspruch 2 oder 3, dadurch gekennzeichnet, dass im ersten Hauptkondensator (4) und/oder im zweiten Hauptkondensator (5) gebildetes Kondensat (43; 60) und/oder eine oder mehrere Flüssigstickstoff-Ströme (65) von einer Zwischenstelle der Hochdrucksäule oder der Mitteldrucksäule der Niederdrucksäule (3) zugeleitet (66) werden.
- Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass ein Flüssigstickstoff-Strom (65) mindestens einen theoretischen Boden unterhalb des Kopfs der Mitteldrucksäule (2) entnommen und der Niederdrucksäule (3) zugeleitet (66) wird.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass die zweite sauerstoffangereicherte Fraktion (53, 57), die in die Niederdrucksäule (3) eingeleitet wird, aus der Hochdrucksäule (1) abgezogen wird.
- Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, dass in der Niederdrucksäule (3) eine Sauerstoff-Fraktion (67) erzeugt wird, mindestens ein Teil der Sauerstoff-Fraktion (67) flüssig aus der Niederdrucksäule (3) entnommen, in flüssigem Zustand auf einen erhöhten Druck gebracht (68) und in die Mitteldrucksäule (2) eingeleitet (69, 70, 370) wird und dass der Mitteldrucksäule (2) ein Sauerstoff-Produkt (71) entnommen wird.
- Verfahren nach Anspruch 7, dadurch gekennzeichnet, dass die flüssig auf Druck gebrachte Sauerstoff-Fraktion (370) aus der Niederdrucksäule mindestens einen theoretischen Boden oberhalb des Sumpfs in die Mitteldrucksäule (2) eingeleitet wird.
- Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, dass ein Sauerstoff-Produkt (71) flüssig aus der Mitteldrucksäule (2) abgezogen, in einen Nebenkondensator (49) eingeleitet und dort durch indirekten Wärmeaustausch mit einem Heizmedium, insbesondere mit Stickstoff (48) aus der Hochdrucksäule (1), mindestens teilweise verdampft wird.
- Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, dass mindestens ein Teil (79) des Sauerstoff-Produkts (71) flüssig aus der Mitteldrucksäule (2) oder aus dem Nebenkondensator (49) abgezogen, in flüssigem Zustand auf einen Druck gebracht (80) wird, der höher als der Betriebsdruck der Mitteldrucksäule (2) ist, und unter diesem Druck durch indirekten Wärmeaustausch (40) verdampft wird.
- Verfahren nach einem der Ansprüche 1 bis 10, dadurch gekennzeichnet, dass eine Stickstoff-Fraktion (51) aus der Hochdrucksäule (1) und/oder Stickstoff-Fraktion (61) aus der Mitteldrucksäule (2) angewärmt (40) und als Druckstickstoff-Produkt (52, 62) gewonnen wird.
- Verfahren nach Anspruch 11, dadurch gekennzeichnet, dass die Stickstoff-Fraktion flüssig aus der Hochdrucksäule (1) entnommen, in flüssigem Zustand auf einen Druck gebracht wird, der höher als der Betriebsdruck der Hochdrucksäule (1) ist, und unter diesem Druck durch indirekten Wärmeaustausch verdampft wird.
- Verfahren nach einem der Ansprüche 1 bis 12, dadurch gekennzeichnet, dass der zweite Einsatzluftstrom (20) in dem Luftverdichter (21) auf etwa den Betriebsdruck der Mitteldrucksäule (2) verdichtet und ohne weitere druckverändernde Maßnahmen in die Mitteldrucksäule (2) eingeleitet (24, 25, 225, 236) wird.
- Kombinierte Vorrichtung zur Tieftemperatur-Zerlegung von Luft und zur Energie-Erzeugung mit einem Drei-Säulen-System, das eine Hochdrucksäule (1), eine Mitteldrucksäule (2) und eine Niederdrucksäule (3) aufweist, und mit einem Gasturbinen-System, das eine Gasturbine, einen von der Gasturbine angetriebenen Gasturbinen-Verdichter (11) und eine Brennkammer aufweist, und mit(a) einer ersten Einsatzluftleitung (10, 14, 15, 16), die vom Austritt des Gasturbinen-Verdichters (11) in die Hochdrucksäule (1) führt, mit(b) einem mit von der Gasturbine gekoppelten Luftverdichter (21) und einer zweiten Einsatzluftleitung (25, 225, 236), die vom Austritt des Luftverdichters (21) in die Mitteldrucksäule (2) führt, mit(c) einer ersten Rohsauerstoffleitung (53, 54) zur Einleitung einer ersten sauerstoffangereicherten Fraktion aus der Hochdrucksäule (1) in die Mitteldrucksäule (2), und mit(d) einer zweiten Rohsauerstoffleitung (53, 57) zur Einleitung einer zweiten sauerstoffangereicherten Fraktion in die Niederdrucksäule (3).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10052180A DE10052180A1 (de) | 2000-10-20 | 2000-10-20 | Drei-Säulen-System zur Tieftemperatur-Zerlegung von Luft |
DE10052180 | 2000-10-20 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1199532A1 true EP1199532A1 (de) | 2002-04-24 |
EP1199532B1 EP1199532B1 (de) | 2005-08-03 |
Family
ID=7660531
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP01103828A Expired - Lifetime EP1199532B1 (de) | 2000-10-20 | 2001-02-15 | Drei-Säulen-System zur Tieftemperatur-Zerlegung von Luft |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP1199532B1 (de) |
AT (1) | ATE301271T1 (de) |
DE (2) | DE10052180A1 (de) |
ES (1) | ES2246945T3 (de) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1120617A2 (de) * | 2000-01-28 | 2001-08-01 | The BOC Group plc | Verfahren zur Luftzerlegung |
EP1120616A2 (de) * | 2000-01-28 | 2001-08-01 | The BOC Group plc | Verfahren zur Luftzerlegung |
EP2634517A1 (de) * | 2012-02-29 | 2013-09-04 | L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Verfahren und Vorrichtung zur Trennung von Luft durch kryogenische Destillation |
US20130340476A1 (en) * | 2011-03-18 | 2013-12-26 | L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Apparatus and method for separating air by cryogenic distillation |
CN104067079B (zh) * | 2011-03-18 | 2016-11-30 | 乔治洛德方法研究和开发液化空气有限公司 | 用于通过低温蒸馏分离空气的设备和方法 |
US20220090855A1 (en) * | 2020-09-18 | 2022-03-24 | L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude | Method and apparatus for producing high-purity nitrogen and low-purity oxygen |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102009023900A1 (de) | 2009-06-04 | 2010-12-09 | Linde Aktiengesellschaft | Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft |
EP3438585A3 (de) * | 2017-08-03 | 2019-04-17 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Enteisungsverfahren eines geräts zur trennung von luft durch kryogene destillation, und entsprechend angepasstes gerät, um mit diesem verfahren enteist zu werden |
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EP0476989A1 (de) * | 1990-09-20 | 1992-03-25 | Air Products And Chemicals, Inc. | Stickstoffgasgenerator bestehend aus einer Dreifachdistillationskolonne mit mehreren Verdampfern/Kondensoren |
EP0694745A1 (de) * | 1994-07-25 | 1996-01-31 | The BOC Group plc | Lufttrennung |
EP0717249A2 (de) * | 1994-12-16 | 1996-06-19 | The BOC Group plc | Lufttrennung |
JPH11132652A (ja) * | 1997-10-27 | 1999-05-21 | Nippon Sanso Kk | 低純度酸素の製造方法及び装置 |
DE19936962A1 (de) * | 1999-08-05 | 2000-09-28 | Linde Tech Gase Gmbh | Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft |
-
2000
- 2000-10-20 DE DE10052180A patent/DE10052180A1/de not_active Withdrawn
-
2001
- 2001-02-15 DE DE50106958T patent/DE50106958D1/de not_active Expired - Lifetime
- 2001-02-15 ES ES01103828T patent/ES2246945T3/es not_active Expired - Lifetime
- 2001-02-15 EP EP01103828A patent/EP1199532B1/de not_active Expired - Lifetime
- 2001-02-15 AT AT01103828T patent/ATE301271T1/de not_active IP Right Cessation
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Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1120617A2 (de) * | 2000-01-28 | 2001-08-01 | The BOC Group plc | Verfahren zur Luftzerlegung |
EP1120616A2 (de) * | 2000-01-28 | 2001-08-01 | The BOC Group plc | Verfahren zur Luftzerlegung |
EP1120617A3 (de) * | 2000-01-28 | 2002-08-28 | The BOC Group plc | Verfahren zur Luftzerlegung |
EP1120616A3 (de) * | 2000-01-28 | 2002-08-28 | The BOC Group plc | Verfahren zur Luftzerlegung |
US20130340476A1 (en) * | 2011-03-18 | 2013-12-26 | L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Apparatus and method for separating air by cryogenic distillation |
CN104067079A (zh) * | 2011-03-18 | 2014-09-24 | 乔治洛德方法研究和开发液化空气有限公司 | 用于通过低温蒸馏分离空气的设备和方法 |
CN104067079B (zh) * | 2011-03-18 | 2016-11-30 | 乔治洛德方法研究和开发液化空气有限公司 | 用于通过低温蒸馏分离空气的设备和方法 |
AU2012230171B2 (en) * | 2011-03-18 | 2017-03-30 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device and method for separating air by cryogenic distillation |
EP2634517A1 (de) * | 2012-02-29 | 2013-09-04 | L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Verfahren und Vorrichtung zur Trennung von Luft durch kryogenische Destillation |
US9360250B2 (en) | 2012-02-29 | 2016-06-07 | L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
US20220090855A1 (en) * | 2020-09-18 | 2022-03-24 | L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude | Method and apparatus for producing high-purity nitrogen and low-purity oxygen |
US11988446B2 (en) * | 2020-09-18 | 2024-05-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for producing high-purity nitrogen and low-purity oxygen |
Also Published As
Publication number | Publication date |
---|---|
ATE301271T1 (de) | 2005-08-15 |
ES2246945T3 (es) | 2006-03-01 |
DE50106958D1 (de) | 2005-09-08 |
EP1199532B1 (de) | 2005-08-03 |
DE10052180A1 (de) | 2002-05-02 |
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