EP2989400B1 - Method for obtaining an air product in an air separating system with temporary storage, and air separating system - Google Patents
Method for obtaining an air product in an air separating system with temporary storage, and air separating system Download PDFInfo
- Publication number
- EP2989400B1 EP2989400B1 EP14716757.1A EP14716757A EP2989400B1 EP 2989400 B1 EP2989400 B1 EP 2989400B1 EP 14716757 A EP14716757 A EP 14716757A EP 2989400 B1 EP2989400 B1 EP 2989400B1
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- EP
- European Patent Office
- Prior art keywords
- air
- liquid fraction
- pressure
- gox
- tank
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- 238000000034 method Methods 0.000 title claims description 23
- 239000007788 liquid Substances 0.000 claims description 78
- 238000000926 separation method Methods 0.000 claims description 59
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 42
- 239000012530 fluid Substances 0.000 claims description 29
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 12
- 238000000605 extraction Methods 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims 2
- 238000009834 vaporization Methods 0.000 claims 2
- 230000008016 vaporization Effects 0.000 claims 2
- 238000007906 compression Methods 0.000 description 22
- 230000006835 compression Effects 0.000 description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000001704 evaporation Methods 0.000 description 14
- 230000008020 evaporation Effects 0.000 description 12
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 229910052786 argon Inorganic materials 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 238000012432 intermediate storage Methods 0.000 description 5
- 238000004821 distillation Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000011109 contamination Methods 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000001228 spectrum Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 102000017795 Perilipin-1 Human genes 0.000 description 1
- 108010067162 Perilipin-1 Proteins 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229910052743 krypton Inorganic materials 0.000 description 1
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052754 neon Inorganic materials 0.000 description 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 1
- QJGQUHMNIGDVPM-OUBTZVSYSA-N nitrogen-15 Chemical compound [15N] QJGQUHMNIGDVPM-OUBTZVSYSA-N 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
Images
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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
- F17C7/02—Discharging liquefied gases
- F17C7/04—Discharging liquefied gases with change of state, e.g. vaporisation
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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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
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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
- F25J3/04078—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
- F25J3/04103—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 using solely hydrostatic liquid head
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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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
- F25J3/04763—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.
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2221/00—Handled fluid, in particular type of fluid
- F17C2221/01—Pure fluids
- F17C2221/011—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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
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- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/04—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pressure accumulator
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
Definitions
- the present invention relates to a method for obtaining an air product in an air separation plant and an air separation plant set up to carry out such a method.
- distillation column systems These can be designed, for example, as single or two-column systems, in particular as classic double-column systems, but also as three-column or multi-column systems.
- a distillation column system is used in particular, which comprises a nitrogen column in the form of a single-column apparatus with an additional column for generating oxygen.
- devices for example columns, for obtaining further air components, in particular the noble gases krypton, xenon and / or argon, can be provided in the mentioned distillation column systems.
- Compressed oxygen is required for a number of industrial applications, and air separation systems with so-called internal compression can be used to extract it.
- a liquid, pressurized liquid fraction in particular liquid oxygen
- the internal compression has, among other things, energetic advantages compared to a subsequent compression of an oxygen product stream that is already in gaseous form.
- the liquid fraction is "pseudo-evaporated".
- the heat transfer medium under high pressure is liquefied (or possibly pseudo-liquefied if it is under supercritical pressure).
- the heat transfer medium is often formed by part of the air supplied to the air separation plant.
- EP 0 716 280 B1 U.S. 5,644,934 A
- EP 0 842 385 B1 U.S. 5,953,937 A
- EP 0 758 733 B1 U.S. 5,845,517 A
- EP 0 895 045 B1 U.S.
- present explanations also apply in a corresponding manner to other air products such as nitrogen or argon, which can also be obtained in a gaseous state using internal compression and are previously present as liquid fractions.
- the invention is also suitable for all others, and in particular, which are present in liquid form in a corresponding air separation plant liquid pressurized or liquid pressurized fractions. These can also be taken from the system in liquid form.
- an air product can also be pressurized by means of a partial flow of compressed feed air in a tank arrangement.
- air products e.g. pressurized oxygen
- pressurized oxygen with a high and especially with a specified degree of purity are required.
- These requirements can only be met with considerable effort or not at all, especially in conventional air separation plants with internal compression.
- the present invention proposes a method for obtaining an air product in an air separation plant and an air separation plant set up to carry out such a method with the features of the independent claims.
- Preferred configurations are the subject of the dependent claims and the description below.
- the invention is based on a known method for obtaining air products.
- the invention can be used for the internal compression explained at the outset, but it is generally suitable for all processes for the production of air products in which these are at least temporarily in liquid form and can be temporarily stored in corresponding tanks.
- a liquid fraction is obtained from the feed air, which increases the pressure in liquid form to a target pressure, then against a heat transfer medium evaporates, and is finally given off as an air product in a gaseous state.
- the air product corresponds to the liquid fraction; in the case of internal compression, the liquid fraction is evaporated to form the air product.
- the liquid fraction is fed into and removed from the at least two tanks in alternating operation.
- “Alternating operation" of the at least two tanks means here that the liquid fraction is fed to at least one of the tanks and removed from at least one of the tanks and not fed to any of the tanks at the same time and, at least not to provide the air product, is removed.
- the feed and the withdrawal from one tank are never carried out at the same time if the corresponding liquid fraction is then to be released as an air product (e.g. after evaporation).
- the tank is therefore always either filled or emptied or neither filled nor emptied in a production plant (i.e. the liquid fraction is always either fed into the tank or removed from it).
- the liquid fraction can be fed to a first tank and removed from a second tank, or vice versa.
- the liquid fraction can also be removed from or fed to one of the tanks, while it is not fed to or removed from the other tank.
- the liquid fraction can also be supplied to both tanks at the same time, but not withdrawn at the same time, or withdrawn from both tanks at the same time, but not supplied at the same time. This also applies mutatis mutandis to more than two tanks.
- the invention it is provided and, thanks to the alternating operation, possible to determine its composition, for example a content of at least one component, in the respective tank before the liquid fraction is removed to provide the air product. Since, due to the intermediate storage, a corresponding liquid fraction is never sent directly to Providing the air product is used, this can always be made available with a verified composition, for example with a defined purity. The usually desired gas product itself cannot usually be continuously checked for its purity; however, this enables the intermediate storage proposed here.
- the method proposed according to the invention develops particular advantages when the liquid fraction for providing the air product in the liquid state is increased in pressure to a target pressure, then evaporated against a heat transfer medium, and finally released as the air product in the gaseous state, i.e. in so-called internal compression processes.
- the evaporation takes place here in particular in the main heat exchanger of the air separation plant.
- Internal compression is used as an alternative to gaseous product compression (external compression) when the gaseous product is to be obtained under pressure.
- the continuously accumulating liquid fraction is conventionally dispensed in the at least two tanks without the intermediate storage according to the invention.
- the release of possibly contaminated air products that do not meet the respective requirements can therefore only be prevented with considerable additional effort.
- main heat exchanger is mentioned in the context of this application, this is preferably understood to mean a single heat exchanger block. In the case of larger systems, however, it can also be advantageous to implement the main heat exchanger by means of several strands connected in parallel with regard to their temperature profile, which are formed by components that are separate from one another. In principle, it is possible to design the main heat exchanger, or each of its branches, by means of two or more heat exchanger blocks connected in series.
- the term “evaporation” here includes pseudo-evaporation under supercritical pressure.
- the pressure under which the liquid fraction, for example pure oxygen, is introduced into a heat exchanger for evaporation can therefore also be above the critical pressure.
- the liquid fraction for example pure oxygen (but also for example argon, helium and / or neon), as in conventional air separation plants with internal compression, is brought to an increased pressure ("pressure increased") in the liquid state.
- pressure increased a warm compressor for a corresponding air product can be dispensed with or at least made relatively small.
- the purity of the gaseous air product obtained is usually improved because contamination by diffusion through seals etc. is avoided.
- the pressure build-up evaporation does not exclude the use of pumps, these can be provided before or after a corresponding tank arrangement.
- the invention is also particularly suitable for pressureless intermediate storage in the tank arrangement, in particular when the Liquid fraction of the system is taken without pressure as an air product or is only pressure increased downstream of the tank arrangement. Usually, however, pressures, for example up to 5 bar, are used, which allow the air product to be withdrawn even without a pump. In this context, it can also be advantageous to return the gas (so-called blow-off gas) that has been released before the refilling of a corresponding tank to reduce the pressure into a suitable column of the distillation column system used.
- the liquid fraction is only used to provide the air product if its composition determined in the tank arrangement corresponds to a specified value, for example a minimum purity of a maximum of 10 ppm residual argon or preferably a maximum of 500 ppm nitrogen. If this is not the case, the liquid fraction can be discarded or returned to the air separation plant at a suitable point, for example a pure oxygen column.
- composition of the liquid fraction is advantageously determined continuously or at intervals. This can be done at least before the removal to provide the air product, but also repeatedly, in particular if a tank is only partially filled in order to avoid excessive production of a non-specification liquid fraction.
- Gas chromatography is particularly suitable for determining the composition of the liquid fraction because it has particularly low detection limits.
- a separation column can have a top condenser in which steam from the upper region of the separation column can be at least partially condensed. This is a nitrogen product that can then be removed from the system in liquid form. At least part of the condensate obtained in the top condenser can also be fed back to the separation column as return.
- a fluid is removed from the separation column and heated in the top condenser against the fluid to be condensed.
- the fluid can be taken from the separation column in the form of one or two fluid streams or only after it has been heated into two fluid streams be divided. Fluid streams withdrawn separately from the separation column are preferably withdrawn from it at different withdrawal heights and therefore have different compositions.
- One of the two fluid streams can preferably be drawn off at the bottom of the separation column.
- the second fluid stream is withdrawn from an intermediate point of the first separation column which is arranged above the sump, in particular above the point at which the first fluid flow is withdrawn.
- One of the two fluid flows is further heated, e.g. in the main heat exchanger of the air separation plant, and expanded in an expansion machine.
- the other fluid flow can be (back) compressed in a compressor coupled to the expansion machine to the pressure of the corresponding separation column and then cooled to a corresponding temperature in the main heat exchanger. It is particularly advantageous to use a cold compressor for recompression.
- a “cold compressor” is understood here to mean a compressor which can be operated at an inlet temperature of less than 200 K, in particular less than 150 K, preferably between 90 and 120 K.
- the SPECTRA process is particularly favorable in terms of energy, because the relaxation in the explained relaxation machine takes place in a work-performing manner.
- the mechanical energy generated in this way can at least partially be used for recompression, as explained above.
- the mechanical energy is transferred directly from the expansion machine to the recompressor mechanically, for example via a common shaft of the expansion machine and the recompressor.
- the recompressor is designed as a cold compressor, preferably only part of the mechanical energy generated by the expansion machine is transferred to the recompressor, the rest is "destroyed" in a warm braking device, e.g. a brake fan, a generator or a dissipative brake. .
- the basic concept of the present invention is therefore not to release the liquid fraction continuously and without further control as an air product, but to store it temporarily in at least two tanks. This makes it possible to use the Check the tank contents for their chemical composition, especially for residual impurities. This can be done discontinuously, for example every ten minutes. Only if the product it contains meets the specified purity requirements is it evaporated in the main heat exchanger, for example, and given off as a gaseous air product.
- the present invention is particularly suitable for a method in which the feed air is cooled in a main heat exchanger and fed into a first separation column.
- pure oxygen is obtained as the liquid fraction from an oxygen-enriched stream from the first separation column in a second separation column. After the intermediate storage and pressure increase in the main heat exchanger, the pure oxygen is evaporated against at least part of the feed air as a heat carrier.
- the invention relates in the same way to an air separation plant which is set up to carry out a method explained above and which has corresponding means.
- the air separation plant benefits from the advantages explained above in the same way. Reference is made to this.
- Extraction or feed means e.g. valves or pumps
- means for heating or cooling e.g. heater or heat exchanger
- means for compression or expansion e.g. compressors or expansion valves or machines
- a particularly advantageously designed air separation system has a separation system from which the liquid fraction can be removed at an extraction point which is geodetically above a feed point in the tank arrangement.
- the liquid fraction can flow off into the tank arrangement in an energy-saving manner.
- this is usually supported by the application of pressure.
- "Geodetically above” means that there is a difference in height between the extraction point from the separating column system and the feed point into the tank arrangement, but not that they have to be arranged one above the other in a fall line. A There can therefore be a lateral offset.
- the tanks are usually at a height that ensures that the air product is provided under sufficient pressure.
- Figure 1 is an air separation plant with internal compression according to the state of the art, for example from the EP 1 995 537 A2 is known, shown schematically in the form of a system diagram.
- the air separation plant set up for internal compression is designated as a whole by 110.
- the invention is also suitable for use in air separation plants without internal compression.
- Atmospheric air 1 is sucked in via a filter 2 by an air compressor 3 and compressed there to an absolute pressure of 6 to 20 bar, preferably about 9 bar.
- the compressed air 6 is cleaned in a cleaning device 7 which has a pair of containers filled with adsorption material, preferably molecular sieve.
- the cleaned air 8 is cooled in a main heat exchanger 9 to approximately dew point and partially liquefied.
- a first part 11 of the cooled air 10 is via a throttle valve 51 into a Single column 12 initiated.
- the feed is preferably a few practical or theoretical plates above the bottom.
- the operating pressure of the individual column 12 (at the top) is 6 to 20 bar, preferably about 9 bar.
- Your top condenser 13 is cooled with a first fluid flow 14 and a second fluid flow 18.
- the first fluid stream 14 is withdrawn from the sump of the individual column 12, the second fluid stream 18 from an intermediate point a few practical or theoretical trays above the air feed or at the same level as it.
- gaseous nitrogen 15, 16 is drawn off at the top of the single column 12, warmed to approximately ambient temperature in the main heat exchanger 9 and finally drawn off via line 17 as a gaseous pressure product (PGAN). Further gaseous nitrogen is passed through the top condenser 13. A portion 53 of the condensate 52 obtained in the top condenser 13 can be obtained as a liquid nitrogen product (PLIN); the remainder 54 is given up as return to the top of the single column 12.
- PLIN liquid nitrogen product
- the first fluid stream 14 is evaporated in the top condenser 13 under a pressure of 2 to 9 bar, preferably about 4 bar, and flows in gaseous form via a line 19 to the cold end of the main heat exchanger 9 an expansion machine 21, which is designed as a turboexpander in the example, expanded to approximately 300 mbar above atmospheric pressure while performing work.
- the expansion machine 21 is mechanically coupled to a cold compressor 30 and a braking device 22, which in the exemplary embodiment is formed by an oil brake.
- the relaxed fluid flow 23 is heated in the main heat exchanger 9 to approximately ambient temperature.
- the warm fluid flow 24 is blown off into the atmosphere (ATM) (line 25) and / or used as regeneration gas 26, 27 in the cleaning device 7, optionally after being heated in the heating device 28.
- ATM atmosphere
- the second fluid stream 18 is evaporated in the top condenser 13 under a pressure of 2 to 9 bar, preferably about 4 bar, and flows in gaseous form via a line 29 to the cold compressor 30, in which it is recompressed to approximately the operating pressure of the individual column.
- the recompressed fluid flow 31 is in the main heat exchanger 9 cooled again to column temperature and finally fed back via line 32 to the individual column 12 at the bottom.
- An oxygen-enriched stream 36 which is essentially free of less volatile impurities, is withdrawn in the liquid state from an intermediate point of the individual column 12, which is arranged 5 to 25 theoretical or practical trays above the air feed.
- the oxygen-enriched stream 36 is optionally supercooled in a bottom evaporator 37 of a pure oxygen column 38 and then applied to the top of the pure oxygen column 38 via a line 39 and a throttle valve 40.
- the operating pressure of the pure oxygen column 38 (at the top) is 1.3 to 4 bar, preferably about 2.5 bar.
- the bottom evaporator 37 of the pure oxygen column 38 is also cooled by means of a second part 42 of the cooled feed air 10.
- the feed air flow 42 is at least partially, for example completely, condensed and flows via a line 43 to the individual column 12, where it is introduced approximately at the level of the feed of the remaining feed air 11.
- a highly pure oxygen product is removed as a liquid fraction 41, brought to an increased pressure of 2 to 100 bar, preferably about 12 bar, by means of a pump 55, passed via a line 56 to the cold end of the main heat exchanger 9, there under the increased Pressure evaporated and warmed to about ambient temperature and finally obtained via line 57 as a gaseous product (GOX-IC).
- a pump 55 passed via a line 56 to the cold end of the main heat exchanger 9, there under the increased Pressure evaporated and warmed to about ambient temperature and finally obtained via line 57 as a gaseous product (GOX-IC).
- An overhead gas 58 of the pure oxygen column 38 is added to the previously explained relaxed second fluid stream 23 (cf. link A). If necessary, part of the feed air to prevent the cold compressor 30 from pumping is passed via a bypass line 59 to its inlet (so-called anti-surge control).
- liquid oxygen can be withdrawn as a liquid fraction from the system upstream and / or downstream of the pump 55 (denoted by LOX in the drawing).
- an external liquid for example liquid argon, liquid nitrogen or liquid oxygen, can also be obtained from a liquid tank in the Main heat exchanger 9 are evaporated in indirect heat exchange with the feed air (not shown in the drawing).
- an air separation plant according to a particularly preferred embodiment of the invention is shown schematically and designated as a whole by 100.
- the one in the Figure 2 The air separation plant 100 shown differs from that in FIG Figure 1 illustrated air separation plant 110 essentially by a tank arrangement 70 with several, in the illustrated example two, tanks 72.
- the tank arrangement 70 comprises two tanks 72 of identical design, of which only the left tank 72 is explained in more detail here.
- the air separation plant 100 according to the invention can also be designed with more than two tanks 72.
- the tanks 72 can be arranged vertically or horizontally and can be filled, for example, from above or below.
- the tank arrangement 70 further comprises a pair of valves 71, by means of which the tanks 72 can be filled alternately or in parallel. It goes without saying that if a larger number of tanks 72 are provided, a larger number of valves are provided in a corresponding manner.
- the tank arrangement 70 can for example be arranged geodetically below a withdrawal point from the pure oxygen column 38, in this case below the lowest point of the pure oxygen column 38, in order to support the transfer of the liquid fraction 41 into the tank arrangement 70.
- the pure oxygen column 38 is operated under a pressure that ensures the transfer of the liquid fraction 41 into the tank arrangement 70, for example 3 bar.
- a pressure build-up evaporator 73 is assigned to each of the tanks 72.
- the pressure build-up evaporators 73 work in a basically known manner.
- a small amount of the oxygen product 41 present in the corresponding tank 72 is withdrawn from the bottom area of the tank 72, heated and fed into the tank at the top via a valve, which is not designated in any more detail.
- the pressure in the tanks 72 increases as a result of the evaporation.
- the tank arrangement 70 can completely replace the previously explained pump 55 due to the pressure build-up evaporation; Figure 2 not shown).
- the tanks 72 in the air separation plant 100 according to the invention are operated in alternation, wherein, as explained, the liquid fraction 41 is fed to at least one of the tanks 72 and taken from at least one of the tanks 72 but not fed to any of the tanks 72 at the same time and to provide the air product is removed.
- the tank 72 assigned to the corresponding valve is filled in this way.
- a corresponding bottom valve 74 is closed.
- the pressure in the respective tank 72 is increased by the pressure build-up evaporator 73. If the corresponding tank 72 is sufficiently filled and is under the desired pressure, the corresponding valve of the valve pair 71 is closed (and the other one is opened) and then a valve 74 at the bottom of the tank 72 is opened (and the other one is closed).
- the pure oxygen contained in the tank 72 can therefore, as already explained above, flow via the line 56 to the cold end of the main heat exchanger 9, where it is evaporated under the increased pressure and warmed to approximately ambient temperature and finally removed via the line 57. At the same time, the other tank 72 fills up.
- the air separation plant 100 according to the invention with the tank arrangement 70 proves to be particularly advantageous because the liquid oxygen present in the corresponding tanks 72 is not released directly to the system boundary, ie in particular not without further checking. Rather, it is provided to monitor the purity of the oxygen in the respective tank 72 continuously or intermittently by means of a control device 75, which in the example shown is only illustrated on the right tank 72.
- the valve 74 arranged at the bottom of the corresponding tank 72 is only opened when the oxygen in the corresponding tank 72 is of sufficient purity. If this is not the case, the tank contents of the tank 72 can be discarded or returned, for example, to the pure oxygen column 38 via a line (not shown). This ensures that oxygen is always given off at the system boundary with a high and, in particular, specifiable purity. this is not possible in conventional systems because, as explained, oxygen is continuously conveyed with a corresponding pump 55.
- a continuous supply of pressurized oxygen at the system boundary via the line 57 is nevertheless ensured because, as mentioned, the tanks 72 can be operated alternately. In this way, oxygen can always be taken from one of the two tanks 72 via the valve 74 arranged at the bottom, while the other tank 72 is filled and checked by means of the control device 75.
- Any control device 75 known from the prior art can be used to monitor the cleanliness.
- the purity monitoring is preferably carried out by means of gas chromatography.
- Another advantageous aspect of the air separation plant 100 according to the invention results from the fact that, as explained, the entry of contaminants into the tank arrangement 70 is significantly reduced compared to the compression by means of a pump 55.
- Known sources of contamination in pumps are, for example, the pump seals, which are completely omitted in the tank arrangement 70.
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Description
Die vorliegende Erfindung betrifft ein Verfahren zur Gewinnung eines Luftprodukts in einer Luftzerlegungsanlage und eine zur Durchführung eines derartigen Verfahrens eingerichtete Luftzerlegungsanlage.The present invention relates to a method for obtaining an air product in an air separation plant and an air separation plant set up to carry out such a method.
Die Herstellung von Sauerstoff oder von entsprechenden Gemischen in flüssigem oder gasförmigem Zustand erfolgt üblicherweise durch Tieftemperaturzerlegung von Luft in Luftzerlegungsanlagen mit an sich bekannten Destillationssäulensystemen. Diese können beispielsweise als Ein- oder Zweisäulensysteme, insbesondere als klassische Doppelsäulensysteme, aber auch als Drei- oder Mehrsäulensysteme ausgebildet sein. Im Rahmen dieser Erfindung kommt dabei insbesondere ein Destillationssäulensystem zum Einsatz, das eine Stickstoffsäule in Form eines Einsäulenapparats mit einer zusätzlichen Säule zum Erzeugen von Sauerstoff umfasst. Ferner können in den genannten Destillationssäulensystemen Vorrichtungen, beispielsweise Säulen, zur Gewinnung weiterer Luftkomponenten, insbesondere der Edelgase Krypton, Xenon und/oder Argon, vorgesehen sein.The production of oxygen or of corresponding mixtures in the liquid or gaseous state is usually carried out by the low-temperature decomposition of air in air separation plants with known distillation column systems. These can be designed, for example, as single or two-column systems, in particular as classic double-column systems, but also as three-column or multi-column systems. In the context of this invention, a distillation column system is used in particular, which comprises a nitrogen column in the form of a single-column apparatus with an additional column for generating oxygen. Furthermore, devices, for example columns, for obtaining further air components, in particular the noble gases krypton, xenon and / or argon, can be provided in the mentioned distillation column systems.
Für eine Reihe industrieller Anwendungen wird Drucksauerstoff benötigt, zu dessen Gewinnung Luftzerlegungsanlagen mit sogenannter Innenverdichtung zum Einsatz kommen können. In derartigen Luftzerlegungsanlagen wird eine flüssig auf Druck gebrachte Flüssigfraktion, insbesondere Flüssigsauerstoff, gegen einen Wärmeträger verdampft und schließlich als gasförmiges Druckprodukt abgegeben. Die Innenverdichtung hat, unter anderem, energetische Vorteile im Vergleich zu einer nachträglichen Verdichtung eines bereits gasförmig vorliegenden Sauerstoffproduktstroms.Compressed oxygen is required for a number of industrial applications, and air separation systems with so-called internal compression can be used to extract it. In such air separation plants, a liquid, pressurized liquid fraction, in particular liquid oxygen, is evaporated against a heat transfer medium and finally given off as a gaseous pressure product. The internal compression has, among other things, energetic advantages compared to a subsequent compression of an oxygen product stream that is already in gaseous form.
Bei überkritischem Druck findet dabei kein Phasenübergang im eigentlichen Sinne statt, die Flüssigfraktion wird "pseudoverdampft". Gegen die (pseudo-)verdampfende Flüssigfraktion wird der unter hohem Druck stehende Wärmeträger verflüssigt (oder ggf. pseudoverflüssigt, wenn er unter überkritischem Druck steht). Der Wärmeträger wird häufig durch einen Teil der der Luftzerlegungsanlage zugeführten Luft gebildet.At supercritical pressure there is no phase transition in the actual sense, the liquid fraction is "pseudo-evaporated". Against the (pseudo-) evaporating liquid fraction, the heat transfer medium under high pressure is liquefied (or possibly pseudo-liquefied if it is under supercritical pressure). The heat transfer medium is often formed by part of the air supplied to the air separation plant.
Die Innenverdichtung ist beispielsweise in folgenden Druckschriften beschrieben:
Die vorliegenden Erläuterungen gelten in entsprechender Weise auch für andere Luftprodukte wie beispielsweise Stickstoff oder Argon, die ebenfalls unter Verwendung der Innenverdichtung in gasförmigem Zustand erhalten werden können und zuvor als Flüssigfraktionen vorliegen. Die Erfindung eignet sich aber auch für alle anderen in einer entsprechenden Luftzerlegungsanlage flüssig vorliegenden und insbesondere flüssig auf Druck gebrachten oder flüssig auf Druck zu bringenden Fraktionen. Diese können der Anlage auch flüssig entnommen werden.The present explanations also apply in a corresponding manner to other air products such as nitrogen or argon, which can also be obtained in a gaseous state using internal compression and are previously present as liquid fractions. However, the invention is also suitable for all others, and in particular, which are present in liquid form in a corresponding air separation plant liquid pressurized or liquid pressurized fractions. These can also be taken from the system in liquid form.
Zur Erhöhung des Drucks von Luftprodukten in Luftzerlegungsanlagen ist die sogenannte Druckaufbauverdichtung bekannt und beispielsweise in der
Für bestimmte industrielle Anwendungen werden Luftprodukte, z.B. Drucksauerstoff, mit hohem und insbesondere mit spezifiziertem Reinheitsgrad benötigt. Diese Anforderungen können insbesondere in herkömmlichen Luftzerlegungsanlagen mit Innenverdichtung nur unter beträchtlichem Aufwand oder gar nicht erfüllt werden.For certain industrial applications, air products, e.g. pressurized oxygen, with a high and especially with a specified degree of purity are required. These requirements can only be met with considerable effort or not at all, especially in conventional air separation plants with internal compression.
Es besteht daher der Bedarf nach verbesserten Möglichkeiten zur Erzeugung von entsprechenden Luftprodukten, insbesondere mit spezifiziertem Reinheitsgrad, in Luftzerlegungsanlagen, insbesondere in Luftzerlegungsanlagen mit Innenverdichtung.There is therefore a need for improved possibilities for generating corresponding air products, in particular with a specified degree of purity, in air separation plants, in particular in air separation plants with internal compression.
Die vorliegende Erfindung schlägt vor diesem Hintergrund ein Verfahren zur Gewinnung eines Luftprodukts in einer Luftzerlegungsanlage und eine zur Durchführung eines derartigen Verfahrens eingerichtete Luftzerlegungsanlage mit den Merkmalen der unabhängigen Patentansprüche vor. Bevorzugte Ausgestaltungen sind Gegenstand der abhängigen Patentansprüche sowie der nachfolgenden Beschreibung.Against this background, the present invention proposes a method for obtaining an air product in an air separation plant and an air separation plant set up to carry out such a method with the features of the independent claims. Preferred configurations are the subject of the dependent claims and the description below.
Die Erfindung geht von einem bekannten Verfahren zur Gewinnung von Luftprodukten aus. Beispielsweise kann die Erfindung bei der eingangs erläuterten Innenverdichtung zum Einsatz kommen, sie eignet sich jedoch generell für alle Verfahren zur Gewinnung von Luftprodukten, bei denen diese zumindest zeitweise flüssig vorliegen und in entsprechenden Tanks zwischengespeichert werden können. Wie erläutert, wird bei der Innenverdichtung aus Einsatzluft eine Flüssigfraktion gewonnen, die in flüssiger Form auf einen Zieldruck druckerhöht, anschließend gegen einen Wärmeträger verdampft, und schließlich als Luftprodukt in gasförmigem Zustand abgegeben wird.The invention is based on a known method for obtaining air products. For example, the invention can be used for the internal compression explained at the outset, but it is generally suitable for all processes for the production of air products in which these are at least temporarily in liquid form and can be temporarily stored in corresponding tanks. As explained, during the internal compression a liquid fraction is obtained from the feed air, which increases the pressure in liquid form to a target pressure, then against a heat transfer medium evaporates, and is finally given off as an air product in a gaseous state.
Dies entspricht im Regelfall dem Kundenwunsch. Es profitieren jedoch auch Anlagen von dem erfindungsgemäßen Verfahren, in denen ein Luftprodukt in flüssigem Zustand abgegeben wird. Im letzteren Fall entspricht das Luftprodukt der Flüssigfraktion, bei der Innenverdichtung wird die Flüssigfraktion zu dem Luftprodukt verdampft.As a rule, this corresponds to the customer's request. However, systems in which an air product is dispensed in a liquid state also benefit from the method according to the invention. In the latter case, the air product corresponds to the liquid fraction; in the case of internal compression, the liquid fraction is evaporated to form the air product.
Es ist vorgesehen, die Flüssigfraktion, insbesondere vor dem Verdampfen bei der Innenverdichtung, in einer Tankanordnung mit wenigstens zwei Tanks zwischenzuspeichern. Die Flüssigfraktion wird dabei im Wechselbetrieb in die wenigstens zwei Tanks eingespeist und aus diesen entnommen.Provision is made for the liquid fraction to be temporarily stored in a tank arrangement with at least two tanks, in particular prior to evaporation during internal compression. The liquid fraction is fed into and removed from the at least two tanks in alternating operation.
Mit einem "Wechselbetrieb" der wenigstens zwei Tanks ist hier gemeint, dass die Flüssigfraktion zumindest einem der Tanks zugeführt und zumindest einem der Tanks entnommen und dabei keinem der Tanks gleichzeitig zugeführt und, zumindest nicht zur Bereitstellung des Luftprodukts, entnommen wird. Die Einspeisung und die Entnahme aus jeweils einem Tank erfolgt damit niemals zeitgleich, wenn die entsprechende Flüssigfraktion anschließend (z.B. nach Verdampfung) als Luftprodukt abgegeben werden soll. Der Tank wird also in einem Produktionsbetrieb stets entweder befüllt oder entleert oder weder befüllt noch entleert (d.h. die Flüssigfraktion wird immer entweder in den Tank eingespeist oder aus diesem entnommen). Hieraus ergibt sich eine Reihe von Vorteilen, die im Rahmen der Erläuterung der bevorzugten Ausführungsformen noch näher erläutert werden."Alternating operation" of the at least two tanks means here that the liquid fraction is fed to at least one of the tanks and removed from at least one of the tanks and not fed to any of the tanks at the same time and, at least not to provide the air product, is removed. The feed and the withdrawal from one tank are never carried out at the same time if the corresponding liquid fraction is then to be released as an air product (e.g. after evaporation). The tank is therefore always either filled or emptied or neither filled nor emptied in a production plant (i.e. the liquid fraction is always either fed into the tank or removed from it). This results in a number of advantages, which will be explained in more detail in the context of the explanation of the preferred embodiments.
Im vereinfachten Fall von nur zwei Tanks kann dabei die Flüssigfraktion einem ersten Tank zugeführt und einem zweiten Tank entnommen werden oder umgekehrt. Die Flüssigfraktion kann jedoch auch einem der Tanks entnommen bzw. zugeführt werden, während sie dem anderen Tank nicht zugeführt bzw. entnommen wird. Die Flüssigfraktion kann auch beiden Tanks gleichzeitig zugeführt, jedoch nicht zeitgleich entnommen, oder beiden Tanks gleichzeitig entnommen, jedoch nicht zeitgleich zugeführt werden. Dies gilt jeweils sinngemäß auch für mehr als zwei Tanks.In the simplified case of only two tanks, the liquid fraction can be fed to a first tank and removed from a second tank, or vice versa. However, the liquid fraction can also be removed from or fed to one of the tanks, while it is not fed to or removed from the other tank. The liquid fraction can also be supplied to both tanks at the same time, but not withdrawn at the same time, or withdrawn from both tanks at the same time, but not supplied at the same time. This also applies mutatis mutandis to more than two tanks.
Erfindungsgemäß ist es vorgesehen und durch den Wechselbetrieb möglich, jeweils vor dem Entnehmen der Flüssigfraktion zur Bereitstellung des Luftprodukts ihre Zusammensetzung, also beispielsweise einen Gehalt an wenigstens einer Komponente, in dem jeweiligen Tank zu ermitteln. Da aufgrund der Zwischenspeicherung eine entsprechende Flüssigfraktion niemals direkt zur Bereitstellung des Luftprodukts verwendet wird, kann dieses stets mit verifizierter Zusammensetzung, beispielsweise mit definierter Reinheit, zur Verfügung gestellt werden. Das üblicherweise erwünschte Gasprodukt selbst kann i.d.R. nicht kontinuierlich auf seine Reinheit überprüft werden; dies ermöglicht jedoch die hier vorgeschlagene Zwischenspeicherung.According to the invention, it is provided and, thanks to the alternating operation, possible to determine its composition, for example a content of at least one component, in the respective tank before the liquid fraction is removed to provide the air product. Since, due to the intermediate storage, a corresponding liquid fraction is never sent directly to Providing the air product is used, this can always be made available with a verified composition, for example with a defined purity. The usually desired gas product itself cannot usually be continuously checked for its purity; however, this enables the intermediate storage proposed here.
Das erfindungsgemäß vorgeschlagene Verfahren entfaltet besondere Vorteile, wenn die Flüssigfraktion zur Bereitstellung des Luftprodukts in flüssigem Zustand auf einen Zieldruck druckerhöht, anschließend gegen einen Wärmeträger verdampft, und schließlich als das Luftprodukt in gasförmigem Zustand abgegeben wird, also bei sogenannten Innenverdichtungsverfahren. Die Verdampfung erfolgt hier insbesondere im Hauptwärmetauscher der Luftzerlegungsanlage. Die Innenverdichtung wird als Alternative zur gasförmigen Produktverdichtung (Außenverdichtung) angewendet, wenn das gasförmige Produkt unter Druck gewonnen werden soll. Hierbei wird die kontinuierlich anfallende Flüssigfraktion allerdings herkömmlicherweise ohne die erfindungsgemäße Zwischenspeicherung in den wenigstens zwei Tanks abgegeben. Die Abgabe ggf. verunreinigter Luftprodukte, die nicht den jeweiligen Anforderungen entsprechen, kann daher nur mit beträchtlichem Zusatzaufwand verhindert werden. Erfindungsgemäß ist hingegen stets die Abgabe eines Luftprodukts mit definierter und spezifizierbarer Zusammensetzung möglich.The method proposed according to the invention develops particular advantages when the liquid fraction for providing the air product in the liquid state is increased in pressure to a target pressure, then evaporated against a heat transfer medium, and finally released as the air product in the gaseous state, i.e. in so-called internal compression processes. The evaporation takes place here in particular in the main heat exchanger of the air separation plant. Internal compression is used as an alternative to gaseous product compression (external compression) when the gaseous product is to be obtained under pressure. In this case, however, the continuously accumulating liquid fraction is conventionally dispensed in the at least two tanks without the intermediate storage according to the invention. The release of possibly contaminated air products that do not meet the respective requirements can therefore only be prevented with considerable additional effort. According to the invention, however, it is always possible to dispense an air product with a defined and specifiable composition.
Ist im Rahmen dieser Anmeldung von einem "Hauptwärmetauscher" die Rede, wird hierunter vorzugsweise ein einziger Wärmetauscherblock verstanden. Bei größeren Anlagen kann es jedoch auch vorteilhaft sein, den Hauptwärmetauscher durch mehrere hinsichtlich ihres Temperaturverlaufs parallel geschaltete Stränge zu realisieren, die durch voneinander getrennte Bauelemente gebildet werden. Grundsätzlich ist es möglich, den Hauptwärmetauscher, bzw. jeden seiner Stränge, durch zwei oder mehrere seriell verbundene Wärmetauscherblöcke auszubilden.If a “main heat exchanger” is mentioned in the context of this application, this is preferably understood to mean a single heat exchanger block. In the case of larger systems, however, it can also be advantageous to implement the main heat exchanger by means of several strands connected in parallel with regard to their temperature profile, which are formed by components that are separate from one another. In principle, it is possible to design the main heat exchanger, or each of its branches, by means of two or more heat exchanger blocks connected in series.
Der Begriff "Verdampfen" schließt hier, wie eingangs erläutert, eine Pseudoverdampfung unter überkritischem Druck ein. Der Druck, unter dem die Flüssigfraktion, beispielsweise Reinsauerstoff, in einen Wärmetauscher zur Verdampfung (z.B. den Hauptwärmetauscher) eingeleitet wird, kann also auch über dem kritischen Druck liegen. Dies gilt in entsprechender Weise für den Druck des Wärmeträgers, beispielsweise die Einsatzluft, der gegen die Flüssigfraktion verflüssigt (oder pseudoverflüssigt) wird. Entscheidend kann hierbei auch sein, dass die Menge so gering ist, dass kein zusätzlicher Boosterverdichter benötigt wird.As explained at the outset, the term “evaporation” here includes pseudo-evaporation under supercritical pressure. The pressure under which the liquid fraction, for example pure oxygen, is introduced into a heat exchanger for evaporation (for example the main heat exchanger) can therefore also be above the critical pressure. This applies in a corresponding manner to the pressure of the heat transfer medium, for example the feed air, which liquefies against the liquid fraction (or pseudo-liquefied). It can also be decisive that the amount is so small that no additional booster compressor is required.
Im Rahmen der vorliegenden Erfindung wird die Flüssigfraktion, beispielsweise Reinsauerstoff (aber auch beispielsweise Argon, Helium und/oder Neon), wie in herkömmlichen Luftzerlegungsanlagen mit Innenverdichtung auch, im flüssigem Zustand auf einen erhöhten Druck gebracht ("druckerhöht") werden. Hierdurch kann ein warmer Verdichter für ein entsprechendes Luftprodukt entfallen oder zumindest relativ klein ausgeführt werden. Durch einen Wegfall einer zusätzlichen Verdichtereinheit verbessert sich i.d.R. die Reinheit des erhaltenen gasförmigen Luftprodukts, weil Kontaminationen durch Diffusion durch Dichtungen usw. vermieden werden.In the context of the present invention, the liquid fraction, for example pure oxygen (but also for example argon, helium and / or neon), as in conventional air separation plants with internal compression, is brought to an increased pressure ("pressure increased") in the liquid state. As a result, a warm compressor for a corresponding air product can be dispensed with or at least made relatively small. By eliminating an additional compressor unit, the purity of the gaseous air product obtained is usually improved because contamination by diffusion through seals etc. is avoided.
Besonders reine Luftprodukte können erhalten werden, da die Flüssigfraktion mittels der erfindungsgemäß ausgebildeten Tankanordnung durch Druckaufbauverdampfung druckerhöht wird. Die Druckaufbauverdampfung ist grundsätzlich bekannt. Hierbei wird einem entsprechenden Tank jeweils ein Teil seines Inhalts entnommen und verdampft. Durch die Expansion während der Verdampfung erhöht sich der Druck. Hierbei wird im Rahmen der vorliegenden Erfindung vorteilhafterweise ein Verfahrensdruck von 8 bis 16 bar verwendet. Die Verwendung zusätzlicher Pumpen, die ebenfalls Kontaminationen verursachen können, kann entfallen oder diese können kleiner ausgebildet werden. Eine entsprechende Anlage erweist sich damit als sehr viel wartungsärmer als herkömmliche Anlagen mit entsprechenden Pumpen. Erfindungsgemäße Anlagen ermöglichen bei Einsatz der Druckaufbauverdampfung eine Energieersparnis von ca. 0,8 bis 1 kW pro Normkubikmeter und Stunde Sauerstoffprodukt bei Reinheiten von beispielsweise unter 10 ppb Ar. Die jeweils erzielbaren Werte richten sich zu einem wesentlichen Anteil nach den Gewinnungsparametern.Particularly pure air products can be obtained since the liquid fraction is increased in pressure by means of the tank arrangement designed according to the invention by means of pressure build-up evaporation. The pressure build-up evaporation is known in principle. Here, a part of its contents is removed from a corresponding tank and evaporated. The expansion during evaporation increases the pressure. A process pressure of 8 to 16 bar is advantageously used in the context of the present invention. The use of additional pumps, which can also cause contamination, can be dispensed with or they can be made smaller. A corresponding system thus proves to be much less maintenance-friendly than conventional systems with corresponding pumps. Systems according to the invention enable energy savings of approx. 0.8 to 1 kW per standard cubic meter and hour of oxygen product with purities of, for example, below 10 ppb Ar when using pressure build-up evaporation. The values that can be achieved in each case are largely based on the extraction parameters.
Die Druckaufbauverdampfung schließt die Verwendung von Pumpen nicht aus, diese können vor oder nach einer entsprechenden Tankanordnung vorgesehen sein. Die Erfindung eignet sich insbesondere auch bei der drucklosen Zwischenspeicherung in der Tankanordnung, insbesondere dann, wenn die Flüssigfraktion der Anlage drucklos als Luftprodukt entnommen oder erst stromab der Tankanordnung druckerhöht wird. Üblicherweise werden jedoch Drücke, beispielsweise bis zu 5 bar, verwendet, die es erlauben, das Luftprodukt auch ohne Pumpe zu entnehmen. Von Vorteil kann in diesem Zusammenhang auch sein, das vor der Wiederbefüllung eines entsprechenden Tanks zum Druckabbau abgelassene Gas (sogenanntes Blowoffgas) in eine hierfür geeignete Säule des verwendeten Destillationssäulensystems zurückzuführen.The pressure build-up evaporation does not exclude the use of pumps, these can be provided before or after a corresponding tank arrangement. The invention is also particularly suitable for pressureless intermediate storage in the tank arrangement, in particular when the Liquid fraction of the system is taken without pressure as an air product or is only pressure increased downstream of the tank arrangement. Usually, however, pressures, for example up to 5 bar, are used, which allow the air product to be withdrawn even without a pump. In this context, it can also be advantageous to return the gas (so-called blow-off gas) that has been released before the refilling of a corresponding tank to reduce the pressure into a suitable column of the distillation column system used.
Im Rahmen des erfindungsgemäßen Verfahrens wird jeweils die Flüssigfraktion nur dann zur Bereitstellung des Luftprodukts verwendet, wenn ihre in der Tankanordnung bestimmte Zusammensetzung einem Vorgabewert, beispielsweise einer Mindestreinheit von maximal 10 ppm Restargon oder vorzugsweise maximal 500 ppm Stickstoff entspricht. Ist dies nicht der Fall, kann die Flüssigfraktion verworfen oder der Luftzerlegungsanlage an geeigneter Stelle, beispielsweise einer Reinsauerstoffsäule, erneut zugeführt werden.Within the scope of the method according to the invention, the liquid fraction is only used to provide the air product if its composition determined in the tank arrangement corresponds to a specified value, for example a minimum purity of a maximum of 10 ppm residual argon or preferably a maximum of 500 ppm nitrogen. If this is not the case, the liquid fraction can be discarded or returned to the air separation plant at a suitable point, for example a pure oxygen column.
Vorteilhafterweise wird die Zusammensetzung der Flüssigfraktion kontinuierlich oder in Intervallen ermittelt. Dies kann zumindest vor der Entnahme zur Bereitstellung des Luftprodukts, jedoch auch wiederholt, erfolgen, insbesondere wenn ein Tank erst teilgefüllt ist, um eine übermäßige Produktion einer nicht spezifikationsgemäßen Flüssigfraktion zu vermeiden. Die Gaschromatographie eignet sich dabei in besonderer Weise zur Ermittlung einer Zusammensetzung der Flüssigfraktion, weil sie besonders niedrige Nachweisgrenzen aufweist.The composition of the liquid fraction is advantageously determined continuously or at intervals. This can be done at least before the removal to provide the air product, but also repeatedly, in particular if a tank is only partially filled in order to avoid excessive production of a non-specification liquid fraction. Gas chromatography is particularly suitable for determining the composition of the liquid fraction because it has particularly low detection limits.
Die vorliegende Erfindung eignet sich in besonderer Weise zur Verwendung mit dem sogenannten SPECTRA-Verfahren der Anmelderin. Hierbei kann eine Trennsäule einen Kopfkondensator aufweisen, in dem Dampf aus dem oberen Bereich der Trennsäule zumindest teilweise kondensiert werden kann. Hierbei handelt es sich um ein Stickstoffprodukt, das anschließend in flüssiger Form der Anlage entnommen werden kann. Zumindest ein Teil des in dem Kopfkondensator gewonnenen Kondensats kann auch als Rücklauf auf die Trennsäule aufgegeben werden.The present invention is particularly suitable for use with the so-called SPECTRA method of the applicant. Here, a separation column can have a top condenser in which steam from the upper region of the separation column can be at least partially condensed. This is a nitrogen product that can then be removed from the system in liquid form. At least part of the condensate obtained in the top condenser can also be fed back to the separation column as return.
Ferner wird ein Fluid der Trennsäule entnommen und in dem Kopfkondensator gegen das zu kondensierende Fluid erwärmt. Das Fluid kann der Trennsäule in Form eines oder zweier Fluidströme entnommen oder erst nach der Erwärmung in zwei Fluidströme aufgeteilt werden. Getrennt der Trennsäule entnommene Fluidströme werden dieser vorzugsweise in unterschiedlicher Entnahmehöhe entnommen und weisen daher unterschiedliche Zusammensetzungen auf. Einer der zwei Fluidströme kann dabei vorzugsweise am Sumpf der Trennsäule abgezogen werden. In bestimmten Fällen kann es sich als günstig erweisen, wenn ein erster Fluidstrom einen höheren Stickstoffgehalt aufweist als ein zweiter Fluidstrom. In diesem Fall wird der zweite Fluidstrom von einer Zwischenstelle der ersten Trennsäule abgezogen, die oberhalb des Sumpfs angeordnet ist, insbesondere oberhalb der Stelle, an der der erste Fluidstrom entnommen wird.Furthermore, a fluid is removed from the separation column and heated in the top condenser against the fluid to be condensed. The fluid can be taken from the separation column in the form of one or two fluid streams or only after it has been heated into two fluid streams be divided. Fluid streams withdrawn separately from the separation column are preferably withdrawn from it at different withdrawal heights and therefore have different compositions. One of the two fluid streams can preferably be drawn off at the bottom of the separation column. In certain cases it can prove to be beneficial if a first fluid flow has a higher nitrogen content than a second fluid flow. In this case, the second fluid stream is withdrawn from an intermediate point of the first separation column which is arranged above the sump, in particular above the point at which the first fluid flow is withdrawn.
Einer der zwei Fluidströme wird, z.B. im Hauptwärmetauscher der Luftzerlegungsanlage, weiter erwärmt und in einer Entspannungsmaschine entspannt. Der andere Fluidstrom kann in einem mit der Entspannungsmaschine gekoppelten Verdichter auf den Druck der entsprechenden Trennsäule (rück)verdichtet und anschließend im Hauptwärmetauscher auf eine entsprechende Temperatur abgekühlt werden. Hierbei ist es besonders günstig, zur Rückverdichtung einen Kaltverdichter zu verwenden. Unter einem "Kaltverdichter" wird hier ein Verdichter verstanden, der bei einer Eintrittstemperatur von weniger als 200 K, insbesondere weniger als 150 K, vorzugsweise zwischen 90 und 120 K, betrieben werden kann.One of the two fluid flows is further heated, e.g. in the main heat exchanger of the air separation plant, and expanded in an expansion machine. The other fluid flow can be (back) compressed in a compressor coupled to the expansion machine to the pressure of the corresponding separation column and then cooled to a corresponding temperature in the main heat exchanger. It is particularly advantageous to use a cold compressor for recompression. A “cold compressor” is understood here to mean a compressor which can be operated at an inlet temperature of less than 200 K, in particular less than 150 K, preferably between 90 and 120 K.
Das SPECTRA-Verfahren ist energetisch besonders günstig, weil die Entspannung in der erläuterten Entspannungsmaschine arbeitsleistend erfolgt. Die hierbei erzeugte mechanische Energie kann zumindest teilweise zur Rückverdichtung, wie zuvor erläutert, genutzt werden. Die Übertragung der mechanischen Energie von der Entspannungsmaschine auf den Rückverdichter erfolgt unmittelbar mechanisch, beispielsweise über eine gemeinsame Welle der Entspannungsmaschine und des Rückverdichters. Insbesondere dann, wenn der Rückverdichter als Kaltverdichter ausgebildet ist, wird vorzugsweise nur ein Teil der von der Entspannungsmaschine erzeugten mechanischen Energie auf den Rückverdichter übertragen, der Rest wird in einer warmen Bremseinrichtung, z.B. einem Bremsgebläse, einem Generator oder einer dissipativen Bremse, "vernichtet".The SPECTRA process is particularly favorable in terms of energy, because the relaxation in the explained relaxation machine takes place in a work-performing manner. The mechanical energy generated in this way can at least partially be used for recompression, as explained above. The mechanical energy is transferred directly from the expansion machine to the recompressor mechanically, for example via a common shaft of the expansion machine and the recompressor. In particular when the recompressor is designed as a cold compressor, preferably only part of the mechanical energy generated by the expansion machine is transferred to the recompressor, the rest is "destroyed" in a warm braking device, e.g. a brake fan, a generator or a dissipative brake. .
Das Grundkonzept der vorliegenden Erfindung ist also, die Flüssigfraktion nicht kontinuierlich und ohne weitere Kontrollmöglichkeit als Luftprodukt abzugeben sondern diese in wenigstens zwei Tanks zwischenzuspeichern. Hierdurch ist es möglich, den Tankinhalt jeweils auf seine chemische Zusammensetzung, insbesondere auf Restverunreinigungen, zu überprüfen. Dies kann diskontinuierlich, beispielsweise alle zehn Minuten erfolgen. Nur wenn das enthaltene Produkt den jeweils vorgegebenen Reinheitsanforderungen entspricht, wird es beispielsweise im Hauptwärmetauscher verdampft und als gasförmiges Luftprodukt abgegeben.The basic concept of the present invention is therefore not to release the liquid fraction continuously and without further control as an air product, but to store it temporarily in at least two tanks. This makes it possible to use the Check the tank contents for their chemical composition, especially for residual impurities. This can be done discontinuously, for example every ten minutes. Only if the product it contains meets the specified purity requirements is it evaporated in the main heat exchanger, for example, and given off as a gaseous air product.
In besonderer Weise eignet sich die vorliegende Erfindung bei einem Verfahren, bei dem die Einsatzluft in einem Hauptwärmetauscher abgekühlt und in eine erste Trennsäule eingespeist wird. Hierbei wird aus einem sauerstoffangereicherten Strom aus der ersten Trennsäule in einer zweiten Trennsäule Reinsauerstoff als die Flüssigfraktion gewonnen. Der Reinsauerstoff wird nach der Zwischenspeicherung und Druckerhöhung in dem Hauptwärmetauscher gegen zumindest einen Teil der Einsatzluft als Wärmeträger verdampft.The present invention is particularly suitable for a method in which the feed air is cooled in a main heat exchanger and fed into a first separation column. Here, pure oxygen is obtained as the liquid fraction from an oxygen-enriched stream from the first separation column in a second separation column. After the intermediate storage and pressure increase in the main heat exchanger, the pure oxygen is evaporated against at least part of the feed air as a heat carrier.
Die Erfindung betrifft in gleicher Weise eine Luftzerlegungsanlage, die zur Durchführung eines zuvor erläuterten Verfahrens eingerichtet ist und über entsprechende Mittel verfügt. Die Luftzerlegungsanlage profitiert von den zuvor erläuterten Vorteilen in gleicher Weise. Auf diese wird verwiesen.The invention relates in the same way to an air separation plant which is set up to carry out a method explained above and which has corresponding means. The air separation plant benefits from the advantages explained above in the same way. Reference is made to this.
Ist hier davon die Rede, dass in einer solchen Luftzerlegungsanlage Ströme, Fraktionen, Luftprodukte usw. "entnehmbar", "einspeisbar", "erwärmbar", "abkühlbar", "verdichtbar", "entspannbar" usw. sind, bedeutet dies, dass entsprechende Entnahme- bzw. Einspeisemittel (z.B. Ventile oder Pumpen), Mittel zur Erwärmung bzw. Abkühlung (z.B. Heizer oder Wärmetauscher) und Mittel zur Verdichtung bzw. Entspannung (z.B. Verdichter bzw. Entspannungsventile oder-maschinen) usw. vorgesehen sind, die in geeigneter Weise ausgebildet sind.If it is mentioned here that in such an air separation plant streams, fractions, air products etc. are "removable", "feedable", "heatable", "coolable", "compressible", "relaxable" etc., this means that corresponding Extraction or feed means (e.g. valves or pumps), means for heating or cooling (e.g. heater or heat exchanger) and means for compression or expansion (e.g. compressors or expansion valves or machines) etc. are provided, which are provided in a suitable manner are trained.
Eine besonders vorteilhaft ausgebildete Luftzerlegungsanlage weist dabei ein Trennsystem auf, dem die Flüssigfraktion an einer Entnahmestelle entnehmbar ist, die geodätisch oberhalb einer Einspeisestelle in die Tankanordnung liegt. Die Flüssigfraktion kann auf diese Weise energiesparend in die Tankanordnung abfließen. Dies wird jedoch i.d.R. durch eine Druckbeaufschlagung unterstützt. Mit "geodätisch oberhalb" ist dabei gemeint, dass ein Höhenunterschied zwischen der Entnahmestelle aus dem Trennsäulensystem und der Einspeisestelle in die Tankanordnung besteht, nicht jedoch, dass diese in einer Falllinie übereinander angeordnet sein müssen. Ein lateraler Versatz kann also vorliegen. In größeren Anlagen befinden sich die Tanks jedoch i.d.R. auf einer Höhe, durch die sichergestellt ist, dass das Luftprodukt unter ausreichendem Druck bereitgestellt wird.A particularly advantageously designed air separation system has a separation system from which the liquid fraction can be removed at an extraction point which is geodetically above a feed point in the tank arrangement. In this way, the liquid fraction can flow off into the tank arrangement in an energy-saving manner. However, this is usually supported by the application of pressure. "Geodetically above" means that there is a difference in height between the extraction point from the separating column system and the feed point into the tank arrangement, but not that they have to be arranged one above the other in a fall line. A There can therefore be a lateral offset. In larger systems, however, the tanks are usually at a height that ensures that the air product is provided under sufficient pressure.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand eines in der Zeichnung schematisch dargestellten Ausführungsbeispiels gegenüber dem Stand der Technik näher erläutert.The invention and further details of the invention are explained in more detail below with reference to an exemplary embodiment shown schematically in the drawing, compared with the prior art.
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Figur 1 zeigt eine Luftzerlegungsanlage gemäß dem Stand der Technik undFigure 1 shows an air separation plant according to the prior art and -
Figur 2 zeigt eine Luftzerlegungsanlage gemäß einer Ausführungsform der Erfindung.Figure 2 shows an air separation plant according to an embodiment of the invention.
In den Figuren sind gleiche oder einander entsprechende Elemente mit identischen Bezugszeichen angegeben. Auf eine wiederholte Erläuterung wird der Übersichtlichkeit halber verzichtet.In the figures, identical or corresponding elements are indicated with identical reference symbols. A repeated explanation is dispensed with for the sake of clarity.
In
Atmosphärische Luft 1 (AIR) wird über ein Filter 2 von einem Luftverdichter 3 angesaugt und dort auf einen Absolutdruck von 6 bis 20 bar, vorzugsweise etwa 9 bar, verdichtet. Nach Durchströmen eines Nachkühlers 4 und eines Wasserabscheiders 5 zum Abscheiden von Wasser (H2O) wird die verdichtete Luft 6 in einer Reinigungsvorrichtung 7 gereinigt, die ein Paar von mit Adsorptionsmaterial, vorzugsweise Molekularsieb, gefüllten Behältern aufweist. Die gereinigte Luft 8 wird in einem Hauptwärmetauscher 9 auf etwa Taupunkt abgekühlt und teilweise verflüssigt. Ein erster Teil 11 der abgekühlten Luft 10 wird über ein Drosselventil 51 in eine Einzelsäule 12 eingeleitet. Die Einspeisung erfolgt vorzugsweise einige praktische oder theoretische Böden oberhalb des Sumpfs.Atmospheric air 1 (AIR) is sucked in via a
Der Betriebsdruck der Einzelsäule 12 (am Kopf) beträgt 6 bis 20 bar, vorzugsweise etwa 9 bar. Ihr Kopfkondensator 13 wird mit einem ersten Fluidstrom 14 und einem zweiten Fluidstrom 18 gekühlt. Der erste Fluidstrom 14 wird vom Sumpf der Einzelsäule 12 abgezogen, der zweite Fluidstrom 18 von_einer Zwischenstelle einige praktische oder theoretische Böden oberhalb der Luftzuspeisung oder auf gleicher Höhe wie diese.The operating pressure of the individual column 12 (at the top) is 6 to 20 bar, preferably about 9 bar. Your
Als Hauptprodukt der Einzelsäule 12 wird gasförmiger Stickstoff 15, 16 am Kopf der Einzelsäule 12 abgezogen, im Hauptwärmetauscher 9 auf etwa Umgebungstemperatur angewärmt und schließlich über Leitung 17 als gasförmiges Druckprodukt (PGAN) abgezogen. Weiterer gasförmiger Stickstoff wird durch den Kopfkondensator 13 geführt. Ein Teil 53 des in dem Kopfkondensator 13 erhaltenen Kondensats 52 kann als Flüssigstickstoffprodukt (PLIN) gewonnen werden; der Rest 54 wird als Rücklauf auf den Kopf der Einzelsäule 12 aufgegeben.As the main product of the
Der erste Fluidstrom 14 wird im Kopfkondensator 13 unter einem Druck von 2 bis 9 bar, vorzugsweise etwa 4 bar verdampft und strömt gasförmig über eine Leitung 19 zum kalten Ende des Hauptwärmetauschers 9. Aus diesem wird sie bei einer Zwischentemperatur entnommen (Leitung 20) und in einer Entspannungsmaschine 21, die in dem Beispiel als Turboexpander ausgebildet ist, arbeitsleistend auf etwa 300 mbar über Atmosphärendruck entspannt. Die Entspannungsmaschine 21 ist mechanisch mit einem Kaltverdichter 30 und einer Bremseinrichtung 22 gekoppelt, die in dem Ausführungsbeispiel durch eine Ölbremse gebildet wird. Der entspannte Fluidstrom 23 wird im Hauptwärmetauscher 9 auf etwa Umgebungstemperatur angewärmt. Der warme Fluidstrom 24 wird in die Atmosphäre (ATM) abgeblasen (Leitung 25) und/oder als Regeneriergas 26, 27 in der Reinigungsvorrichtung 7 eingesetzt, gegebenenfalls nach Erwärmung in der Heizeinrichtung 28.The
Der zweite Fluidstrom 18 wird im Kopfkondensator 13 unter einem Druck von 2 bis 9 bar, vorzugsweise etwa 4 bar verdampft und strömt gasförmig über eine Leitung 29 zu dem Kaltverdichter 30, in dem er auf etwa den Betriebsdruck der Einzelsäule rückverdichtet wird. Der rückverdichtete Fluidstrom 31 wird im Hauptwärmetauscher 9 wieder auf Säulentemperatur abgekühlt und schließlich über Leitung 32 der Einzelsäule 12 am Sumpf wieder zugeführt.The
Ein sauerstoffangereicherter Strom 36, der im Wesentlichen frei von schwerer flüchtigen Verunreinigungen ist, wird von einer Zwischenstelle der Einzelsäule 12 in flüssigem Zustand abgezogen, die 5 bis 25 theoretische oder praktische Böden oberhalb der Luftzuspeisung angeordnet ist. Der sauerstoffangereicherte Strom 36 wird gegebenenfalls in einem Sumpfverdampfer 37 einer Reinsauerstoffsäule 38 unterkühlt und anschließend über eine Leitung 39 und ein Drosselventil 40 auf den Kopf der Reinsauerstoffsäule 38 aufgegeben. Der Betriebsdruck der Reinsauerstoffsäule 38 (am Kopf) beträgt 1,3 bis 4 bar, vorzugsweise etwa 2,5 bar.An oxygen-enriched
Der Sumpfverdampfer 37 der Reinsauerstoffsäule 38 wird außerdem mittels eines zweiten Teils 42 der abgekühlten Einsatzluft 10 gekühlt. Der Einsatzluftstrom 42 wird dabei mindestens teilweise, beispielsweise vollständig, kondensiert und strömt über eine Leitung 43 zur Einzelsäule 12, wo er etwa auf Höhe der Zuspeisung der übrigen Einsatzluft 11 eingeleitet wird.The
Vom Sumpf der Reinsauerstoffsäule 38 wird ein hochreines Sauerstoffprodukt als Flüssigfraktion 41 entnommen, mittels einer Pumpe 55 auf einen erhöhten Druck von 2 bis 100 bar, vorzugsweise etwa 12 bar gebracht, über eine Leitung 56 zum kalten Ende des Hauptwärmetauschers 9 geführt, dort unter dem erhöhten Druck verdampft und auf etwa Umgebungstemperatur angewärmt und schließlich über Leitung 57 als gasförmiges Produkt (GOX-IC) gewonnen.From the bottom of the
Ein Kopfgas 58 der Reinsauerstoffsäule 38 wird dem zuvor erläuterten entspannten zweiten Fluidstrom 23 zugemischt (vgl. Verknüpfung A). Über eine Bypassleitung 59 wird gegebenenfalls ein Teil der Einsatzluft zur Pumpverhütung des Kaltverdichters 30 zu dessen Eintritt geleitet (sogenannte Anti-Surge Control).An
Bei Bedarf kann der Anlage stromauf und/oder stromab der Pumpe 55 flüssiger Sauerstoff als Flüssigfraktion entnommen werden (in der Zeichnung mit LOX bezeichnet). Zusätzlich kann eine externe Flüssigkeit, beispielsweise flüssiges Argon, flüssiger Stickstoff oder flüssiger Sauerstoff, auch aus einem Flüssigtank, in dem Hauptwärmetauscher 9 in indirektem Wärmeaustausch mit der Einsatzluft verdampft werden (in der Zeichnung nicht dargestellt).If necessary, liquid oxygen can be withdrawn as a liquid fraction from the system upstream and / or downstream of the pump 55 (denoted by LOX in the drawing). In addition, an external liquid, for example liquid argon, liquid nitrogen or liquid oxygen, can also be obtained from a liquid tank in the
In der
Die Tankanordnung 70 umfasst im dargestellten Beispiel zwei gleichartig ausgebildete Tanks 72, von denen hier nur der linke Tank 72 näher erläutert wird. Wie zuvor erwähnt, kann die erfindungsgemäße Luftzerlegungsanlage 100 auch mit mehr als zwei Tanks 72 ausgebildet sein. Die Tanks 72 können stehend oder liegend angeordnet sein und beispielsweise von oben oder unten befüllt werden. Die Tankanordnung 70 umfasst ferner im dargestellten Beispiel ein Ventilpaar 71, mittels dessen die Tanks 72 alternierend oder parallel befüllt werden können. Es versteht sich, dass, wenn eine größere Anzahl von Tanks 72 vorgesehen ist, in entsprechender Weise eine größere Anzahl von Ventilen vorgesehen ist.In the example shown, the
Die Tankanordnung 70 kann beispielsweise geodätisch unterhalb einer Entnahmestelle aus der Reinsauerstoffsäule 38, hier also unterhalb des tiefsten Punkts der Reinsauerstoffsäule 38 angeordnet sein, um die Überführung der Flüssigfraktion 41 in die Tankanordnung 70 zu unterstützen. I.d.R. wird jedoch die Reinsauerstoffsäule 38 unter einem Druck betrieben, der die Überführung der Flüssigfraktion 41 in die Tankanordnung 70 sicherstellt, beispielsweise 3 bar.The
Jedem der Tanks 72 ist im dargestellten Beispiel ein Druckaufbauverdampfer 73 zugeordnet. Die Druckaufbauverdampfer 73 arbeiten in grundsätzlich bekannter Weise. Aus dem Bodenbereich der Tanks 72 wird jeweils eine geringe Menge des im entsprechenden Tank 72 vorliegenden Sauerstoffprodukts 41, entnommen, erwärmt und kopfseitig in den Tank über ein nicht näher bezeichnetes Ventil eingespeist. Durch die Verdampfung erhöht sich der Druck in den Tanks 72. Die Tankanordnung 70 kann durch die Druckaufbauverdampfung die zuvor erläuterte Pumpe 55 vollständig ersetzen, alternativ dazu kann jedoch auch zusätzlich eine entsprechende Pumpe 55 vorgesehen sein (in der
Wie bereits erläutert werden die Tanks 72 in der erfindungsgemäßen Luftzerlegungsanlage 100 im Wechselbetrieb gefahren, wobei, wie erläutert, die Flüssigfraktion 41 zumindest einem der Tanks 72 zugeführt und zumindest einem der Tanks 72 entnommen aber dabei keinem der Tanks 72 gleichzeitig zugeführt und zur Bereitstellung des Luftprodukts entnommen wird.As already explained, the
Beispielsweise wird hierbei immer nur eines der Ventile des Ventilpaars 71 geöffnet.For example, only one of the valves of the
Der dem entsprechenden Ventil zugeordnete Tank 72 wird auf diese Weise befüllt. Ein entsprechendes bodenseitiges Ventil 74 ist geschlossen. Gleichzeitig hierzu, oder auch erst nach ausreichender Füllung des entsprechenden Tanks 72, wird der Druck in dem jeweiligen Tank 72 durch den Druckaufbauverdampfer 73 erhöht. Ist der entsprechende Tank 72 ausreichend befüllt und steht unter dem gewünschten Druck, wird das entsprechende Ventil des Ventilpaars 71 geschlossen (und das jeweils andere geöffnet) und anschließend ein Ventil 74 bodenseitig des Tanks 72 geöffnet (und das jeweils andere geschlossen). Der im Tank 72 enthaltene Reinsauerstoff kann daher, wie bereits zuvor erläutert, über die Leitung 56 zum kalten Ende des Hauptwärmetauschers 9 fließen und dort unter dem erhöhten Druck verdampft und auf etwa Umgebungstemperatur angewärmt und schließlich über Leitung 57 entnommen werden. Gleichzeitig füllt sich der andere Tank 72.The
Die erfindungsgemäße Luftzerlegungsanlage 100 mit der Tankanordnung 70 erweist sich dabei als besonders vorteilhaft, weil der in den entsprechenden Tanks 72 jeweils vorliegende Flüssigsauerstoff nicht direkt, d.h. insbesondere nicht ohne eine weitere Überprüfung, an die Anlagengrenze abgegeben wird. Vielmehr ist es vorgesehen, mittels einer Kontrolleinrichtung 75, die im dargestellten Beispiel nur am rechten Tank 72 veranschaulicht ist, die Reinheit des Sauerstoffs im jeweiligen Tank 72 kontinuierlich oder intermittierend zu überwachen. Das bodenseitig des entsprechenden Tanks 72 angeordnete Ventil 74 wird nur jeweils dann geöffnet, wenn der Sauerstoff im entsprechenden Tank 72 eine ausreichende Reinheit aufweist. Ist dies nicht der Fall, kann der Tankinhalt des Tanks 72 verworfen oder über eine nicht dargestellte Leitung beispielsweise in die Reinsauerstoffsäule 38 zurückgeführt werden. Auf diese Weise wird sichergestellt, dass an der Anlagengrenze stets Sauerstoff mit hoher und insbesondere spezifizierbarer Reinheit abgegeben wird. Dies ist in herkömmlichen Anlagen nicht möglich, weil, wie erläutert, mit einer entsprechenden Pumpe 55 kontinuierlich Sauerstoff gefördert wird.The
Eine kontinuierliche Bereitstellung von Drucksauerstoff an der Anlagengrenze über die Leitung 57 ist dennoch gewährleistet, weil, wie erwähnt, die Tanks 72 abwechselnd betrieben werden können. So kann stets aus einem der beiden Tanks 72 Sauerstoff über das bodenseitig angeordnete Ventil 74 entnommen werden, während der jeweils andere Tank 72 befüllt und mittels der Kontrolleinrichtung 75 überprüft wird.A continuous supply of pressurized oxygen at the system boundary via the
Zur Reinheitsüberwachung kann jede Kontrolleinrichtung 75 verwendet werden, die aus dem Stand der Technik bekannt ist. Vorzugsweise erfolgt die Reinheitsüberwachung mittels Gaschromatographie.Any
Ein weiterer vorteilhafter Aspekt der erfindungsgemäßen Luftzerlegungsanlage 100 ergibt sich dadurch, dass, wie erläutert, der Eintrag von Kontaminationen in der Tankanordnung 70 gegenüber der Verdichtung mittels einer Pumpe 55 deutlich reduziert ist. Als bekannte Kontaminationsquellen bei Pumpen gelten beispielsweise die Pumpendichtungen, die in der Tankanordnung 70 vollständig entfallen.Another advantageous aspect of the
Claims (10)
- Method for obtaining an air product (GOX-IC) in an air-separating system (100) in which a liquid fraction (41) is obtained from feed air (8) and is at least partially used for providing the air product (GOX-IC), wherein the liquid fraction (41) is temporarily stored in a tank arrangement (70) having at least two tanks (72), wherein the liquid fraction (41) is fed to at least one of the tanks (72) and is withdrawn from at least one of the tanks (72) in order to provide the air product (GOX-IC), and in the process is fed to and withdrawn from none of the tanks (72) simultaneously, and wherein the pressure of the liquid fraction (41) in the tank arrangement (70) is increased by means of pressure build-up vaporization, characterized in that the composition of the liquid fraction (41) in the tank (72) is determined in each case before the liquid fraction (41) is withdrawn from a tank (72).
- Method according to Claim 1, wherein the pressure of the liquid fraction (41) is increased to a target pressure in order to provide the air product (GOX-IC) in a liquid state, then vaporized against a heat transfer medium (8), and finally discharged in a gaseous state as the air product (GOX-IC).
- Method according to either of the preceding claims, wherein the liquid fraction (41), if its composition determined in the tank (72) corresponds to a prespecified value, is used to provide the air product (GOX-IC).
- Method according to any one of the preceding claims, wherein the feed air (8) is cooled in a main heat exchanger (9) and fed (11, 43) into a first separation column (12) of the air-separating system (100), wherein, at least from an oxygen-enriched stream (36) from the first separation column (12), pure oxygen is obtained as the liquid fraction (41) in a second separation column (38), wherein the pure oxygen is temporarily stored in the tank arrangement (70), increased in pressure, vaporized in the main heat exchanger (9) against at least a portion of the feed air (8) as heat transfer medium, and discharged in a gaseous state as the air product (GOX-IC).
- Method according to Claim 4, wherein fluid is withdrawn from the first separation column (12) and heated in a head condenser (13) of the first separation column (12), whereof a first fluid stream (14) is further heated in the main heat exchanger (9) and then expanded in an expansion machine (21), and a second fluid stream (18) is compressed in a compressor (30) coupled to the expansion machine (21), then cooled in the main heat exchanger (9), and finally fed again into the first separation column (12).
- Air-separating system (100), configured to carry out a method according to any one of the preceding claims, having a separation system (12, 13, 38) designed to obtain the liquid fraction (41) from the feed air (8), and having a delivery system (70, 9) designed to provide the air product (GOX-IC) using at least a portion of the liquid fraction (41), wherein the delivery system (70, 9) comprises the tank arrangement (70) having the at least two tanks (72), is designed to temporarily store the liquid fraction (41), and can be operated in such a way that the liquid fraction (41) can be supplied to at least one of the tanks (72) and can be withdrawn from at least one of the tanks (72) in order to provide the air product (GOX-IC), and in the process can be supplied to and withdrawn from none of the tanks (72) simultaneously, and wherein the system has in the tank arrangement (70) means for increasing the pressure of the liquid fraction (41) by means of pressure build-up vaporization,
characterized in that a control device (75) is provided by means of which the composition of this liquid fraction (41) in the tank (72) can be determined in each case before the liquid fraction (41) is withdrawn from a tank (72) in order to provide the air product (GOX-IC). - Air-separating system (100) according to Claim 6, which is designed to increase a pressure of the liquid fraction (41) in a liquid state to a target pressure, and to vaporize the liquid fraction (41) against a heat transfer medium (8) and discharge it as the gaseous air product (GOX-IC).
- Air-separating system (100) according to Claims 6 or 7, having at least one main heat exchanger (9) in which the feed air (8) can be cooled and a first separation column (12) into which the feed air (8) can be fed (11, 43), wherein a second separation column (12) is provided which is designed to obtain, from an oxygen-enriched stream (36) from the first separation column (12), pure oxygen as the liquid fraction (41), wherein the pure oxygen, after temporary storage in the tank arrangement (70) and after an increase in pressure, can be vaporized in the main heat exchanger (9) against at least a portion of the feed air (8) as heat transfer medium and can be discharged in a gaseous state as the air product (GOX-IC).
- Air-separating system (100) according to Claim 8, wherein the fluid can be withdrawn from the first separation column (12) and heated in a head condenser (13) of the first separation column (12), whereof a first fluid stream (14) can be further heated in the main heat exchanger (9) and can then be expanded in an expansion machine (21), and a second fluid stream (18) can be compressed in a compressor (30) coupled to the expansion machine (21), then cooled in the main heat exchanger (9), and finally fed again into the first separation column (12).
- Air-separating system (100) according to any one of Claims 6 to 9, wherein the liquid fraction (41) can be withdrawn from the separating system (12, 13, 38) at an extraction point, which is geodetically above a feed point into the tank arrangement (70).
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PCT/EP2014/000937 WO2014173496A2 (en) | 2013-04-25 | 2014-04-08 | Method for obtaining an air product in an air separating system with temporary storage, and air separating system |
EP14716757.1A EP2989400B1 (en) | 2013-04-25 | 2014-04-08 | Method for obtaining an air product in an air separating system with temporary storage, and air separating system |
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EP3193114B1 (en) * | 2016-01-14 | 2019-08-21 | Linde Aktiengesellschaft | Method for obtaining an air product in an air separation assembly and air separation assembly |
CN106195623A (en) * | 2016-07-12 | 2016-12-07 | 安徽淮化股份有限公司 | A kind of air separation unit nitrogen-sealed gas track remodelling method |
JP6900241B2 (en) | 2017-05-31 | 2021-07-07 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Gas production system |
CN109307724A (en) * | 2018-12-18 | 2019-02-05 | 同方威视技术股份有限公司 | Gas-chromatography-ion mobility spectrometry is combined equipment |
EP4081747A1 (en) | 2019-12-23 | 2022-11-02 | Linde GmbH | Process and plant for provision of an oxygen product |
JP2024058676A (en) | 2022-09-06 | 2024-04-26 | レール・リキード-ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Air separation device and air separation method |
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EP0464630A1 (en) | 1990-06-27 | 1992-01-08 | Praxair Technology, Inc. | Cryogenic air separation with dual product boiler |
EP1995537A2 (en) | 2007-05-24 | 2008-11-26 | Linde Aktiengesellschaft | Process and device for the cryogenic separation of air |
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DE676616C (en) | 1936-09-04 | 1939-06-08 | Messer & Co Gmbh | Process for the production of gaseous oxygen under pressure |
JP2967422B2 (en) | 1990-03-30 | 1999-10-25 | 日本酸素株式会社 | Air liquefaction separation device and control method thereof |
US6295840B1 (en) | 2000-11-15 | 2001-10-02 | Air Products And Chemicals, Inc. | Pressurized liquid cryogen process |
DE10205878A1 (en) * | 2002-02-13 | 2003-08-21 | Linde Ag | Cryogenic air separation process |
EP1544559A1 (en) | 2003-12-20 | 2005-06-22 | Linde AG | Process and device for the cryogenic separation of air |
JP5005708B2 (en) * | 2009-01-06 | 2012-08-22 | 大陽日酸株式会社 | Air separation method and apparatus |
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2014
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US3133444A (en) | 1961-08-16 | 1964-05-19 | Linde Eismasch Ag | Sampling arrangement for liquid gases |
EP0464630A1 (en) | 1990-06-27 | 1992-01-08 | Praxair Technology, Inc. | Cryogenic air separation with dual product boiler |
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WO2014173496A3 (en) | 2015-08-20 |
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US20160069611A1 (en) | 2016-03-10 |
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