EP0948730B1 - Verfahren und vorrichtung zur gewinnung von druckstickstoff - Google Patents
Verfahren und vorrichtung zur gewinnung von druckstickstoff Download PDFInfo
- Publication number
- EP0948730B1 EP0948730B1 EP97948844A EP97948844A EP0948730B1 EP 0948730 B1 EP0948730 B1 EP 0948730B1 EP 97948844 A EP97948844 A EP 97948844A EP 97948844 A EP97948844 A EP 97948844A EP 0948730 B1 EP0948730 B1 EP 0948730B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- pressure column
- low
- nitrogen
- product
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims description 132
- 229910052757 nitrogen Inorganic materials 0.000 title claims description 64
- 238000000034 method Methods 0.000 title claims description 36
- 239000007788 liquid Substances 0.000 claims description 63
- 239000007789 gas Substances 0.000 claims description 23
- 239000001301 oxygen Substances 0.000 claims description 23
- 229910052760 oxygen Inorganic materials 0.000 claims description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 22
- 238000001704 evaporation Methods 0.000 claims description 19
- 230000008020 evaporation Effects 0.000 claims description 17
- 238000007906 compression Methods 0.000 claims description 5
- 239000003507 refrigerant Substances 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 4
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 238000005194 fractionation Methods 0.000 claims 2
- 239000000047 product Substances 0.000 description 47
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 6
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000011552 falling film Substances 0.000 description 3
- 230000002631 hypothermal effect Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 206010016352 Feeling of relaxation Diseases 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000003990 capacitor Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000001307 helium Substances 0.000 description 2
- 229910052734 helium Inorganic materials 0.000 description 2
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 229910052754 neon Inorganic materials 0.000 description 2
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 238000004887 air purification Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- AFYPFACVUDMOHA-UHFFFAOYSA-N chlorotrifluoromethane Chemical compound FC(F)(F)Cl AFYPFACVUDMOHA-UHFFFAOYSA-N 0.000 description 1
- 238000005056 compaction Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000002706 hydrostatic effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000002040 relaxant effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
- F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
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- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F25J3/04006—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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- 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
- F25J3/04424—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 without thermally coupled high and low pressure columns, i.e. a so-called split columns
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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
- 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.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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- 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.
- F25J3/04884—Arrangement of reboiler-condensers
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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
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
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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
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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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
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
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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
- F25J2250/10—Boiler-condenser with superposed stages
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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
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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
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/42—One fluid being nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/50—One fluid being oxygen
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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
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
Definitions
- the invention is based, relative to nitrogen under high pressure with the task to gain little effort.
- the pressure increase in the nitrogen product from the low pressure column is therefore at least partially carried out in the liquid state.
- the pressure increase in the Liquid can be carried out by any known measure for example by means of a pump, using a hydrostatic potential and / or the pressure build-up evaporation on a tank. It means one less expenditure on equipment than a gas compressor. It will also be a indirect heat exchange is required in which the liquid is pressurized Low pressure column nitrogen is evaporated. Nevertheless, there is an overall economically particularly favorable process.
- the inventive method Compared to a removal of the pressure nitrogen product directly from the pressure column the inventive method also has the advantage of higher product purity on.
- the pressure column reduced concentration of volatile components such as Helium, neon and / or hydrogen can be achieved.
- the entire nitrogen product of the low pressure column liquid from the Low pressure column or their top condenser removed.
- the operating pressures of the double column can be in the method according to the invention for example 6 to 20, preferably 7 to 16 bar in the pressure column and for example 3 to 8, preferably 3 to 6 bar in the low pressure column.
- the top condenser of the low pressure column is, for example, with a liquid from the low pressure column such as the low pressure column sump liquid as Refrigerant operated. Return for the pressure column is usually through a Condenser-evaporator is generated over the top of the pressure column and the sump the low-pressure column are in heat-exchanging connection.
- a gas from the pressure column preferably a nitrogenous one Fraction from an upper or middle area of the pressure column, as a heat transfer medium be used. It can be the top fraction of the pressure column or act a gas that is withdrawn at an intermediate point of the pressure column. This The intermediate point is below the number of theoretical floors Pressure column head, which up to 5/6, preferably 1/3 to 5/6 of the total number theoretical plates within the pressure column. That with the indirect Heat exchange in the product evaporator is condensate at least partially, preferably completely back into the pressure column returned and used there as a return.
- the liquid nitrogen is used for indirect heat exchange only partially evaporated in the product evaporator and the liquid portion of the Nitrogen is returned to the low pressure column.
- the product evaporator will preferably operated as a falling film evaporator. That kind of evaporation enables a particularly low temperature difference and thus one correspondingly high evaporation pressure, which is also pure when used Nitrogen from the top of the pressure column as a heat transfer medium only slightly (about 0.3 to 0.8 bar) is below the pressure column pressure.
- the low pressure column serves as Flash gas separator when recycling the remaining liquid portion.
- the bottom liquid of the low pressure column is used as a refrigerant Condensation of the gaseous nitrogen from the low pressure column in the Top condenser of the low pressure column used.
- the method according to the invention is also relatively pure or pure oxygen (purity higher than 40 mol%, in particular higher than 80 mol% or higher than 90 mol%, preferably between 99.5 and 99.999 mol%) it is particularly beneficial if a liquid fraction, its oxygen content between that of the oxygen-containing liquid fraction from the pressure column and that of the bottom liquid of the low pressure column for condensation of the gaseous nitrogen from the low pressure column in the top condenser is used.
- compressed and cleaned air 1 is combined in one Main heat exchanger 2 cooled and a pressure column 4 under a pressure of 14 bar supplied (3).
- the rectification system also has a low pressure column 5 on, which is operated at a pressure of 5 bar and with the pressure column via a common condenser-evaporator (main condenser) 6 in heat-exchanging Connection is established.
- Part 8 of the nitrogen removed at the top of the pressure column is liquefied in the main condenser 6 and via lines 9 and 10 as a return placed on the pressure column.
- Bottom liquid 11 of the pressure column is after Hypothermia 15 as an oxygen-rich liquid fraction in the low pressure column 5 throttled (12).
- FIG. 1 Another part 20 of the liquid nitrogen 19 from the top condenser 17 is either as shown in Figure 1 taken from the low pressure column or directly branched off from line 19.
- This liquid nitrogen 20 is according to the invention in liquid state brought to pressure (in the example 14 bar) (pump 21) and over Line 22 through the subcooler 15 to a product evaporator 23.
- the method of FIG. 2 differs from this mainly in that Use of another heat transfer medium in the product evaporator.
- Top gas 7 of the pressure column 4 becomes a gas 35 'from an intermediate point here Pressure column passed into the liquefaction chamber of the product evaporator 23.
- the gas 35 'still has an oxygen content of about 2 mol% and thus a higher one Condensation temperature as the pure nitrogen from the top of the pressure column 6 (10 ppb Oxygen).
- the pressure on the evaporation side of the Product evaporator 23 (14 bar instead of 13.4 bar in the case of Figure 1).
- indirect heat exchange condensate 36 ' is on one of its Returned composition corresponding point in the pressure column 4, especially in the place of the extraction (line 35 'or something above).
- the double column is operated at a sufficiently high pressure (For example 8 to 15 bar), the entire feed air 3 ′ can be fed into the pressure column 4 be directed.
- a sufficiently high pressure For example 8 to 15 bar
- the operating pressures in pressure column 4 and low pressure column 5 are 15 bar in this example or 5 bar.
- Process cold is here due to work relaxation of steam 31, 31 'from the evaporation side of the overhead condenser 17 Low pressure column 5 generated.
- the relaxation machine 33 ' can also as in Figure 1 coupled to a compressor 26 for nitrogen product.
- a method according to FIG. 5 is used if in addition to pressure nitrogen pure oxygen (in the example: 99.5 mol%) is to be obtained.
- the refrigerant 13 'for the Top condenser 17 of the low pressure column 5 not from the sump, but from one Intermediate point is withdrawn, preferably from a liquid reservoir within the low pressure column 5, which is immediately below the feed of the oxygen-containing liquid fraction 11 from the pressure column 4 is arranged.
- the oxygen product can be liquid (42) and / or gaseous (43) are withdrawn.
- part 44 of the Liquid 42 are led into the top condenser 17. If the oxygen is below Pressure is required, oxygen 42 can be used according to the known method of Internal compression in the liquid state brought to pressure and then are evaporated, for example against part of the feed air.
- the method of FIG. 6 differs from that in several points Figure 1. For example, it shows a slightly different hypothermia Process streams represented by only one heat exchanger block 15 for this purpose is.
- a part of the bottom product 13 of the low pressure column 5 can be used as a liquid product (LOX) can be won.
- the nitrogen 9 liquefied in the main condenser 6 can partly subcooled 160 (15) and throttled into the low-pressure column 5 (161) become.
- the bottom liquid 11 of the pressure column can partially (162) in the Evaporation chamber of the top condenser 17 of the low pressure column passed (163) become.
- the pressure nitrogen product 24 is made from the Product evaporator 23 not post-compressed, but under the evaporation pressure deducted (29).
- the turbine exhaust gas 151 is warmed up again in the heat exchanger 2 and as residual gas 152 discharged or for the regeneration of a device for the Purification of the feed air used.
- the one in the relaxation machine 133 Mechanical energy obtained can be given to a generator or used for Compaction of a process fraction can be used, preferably by direct mechanical coupling of the relaxation machine 133 with a not shown Compressor.
- the main difference compared to Figure 1 lies in the product evaporator 23.
- This is operated on the liquefaction side with steam from the low pressure column. This is done on the Liquefaction side of the product evaporator 23 a part of the above the sump Low pressure column condensed gas. The resulting liquid 136 flows back into the low pressure column.
- the product evaporator 23 is in the Example arranged within the low pressure column. It can be used as a falling film evaporator be formed in which only partial evaporation takes place. Liquid remaining nitrogen can be returned to the low pressure column 5.
- the product evaporator 23 is similar to that in FIG 6 built into the double column. He sits here in the upper area of the pressure column 4. Die The liquefaction side of the product evaporator 23 is similar to that in FIGS. 1 to 5 with a portion 35 of the gaseous nitrogen 7 from the top of the pressure column 4 acted upon.
- FIG 8 there are subcoolers and product evaporators in a heat exchanger block 223 integrated.
- a portion 246 of the bottom liquid 11 of the Pressure column for additional head cooling of the pressure column (via valve 248) or Low pressure column (via valve 247) can be used.
- Process cold becomes like in figure 1 obtained by work-relaxation 33 of a part 32 of the feed air.
- the product evaporator 323 from FIG. 9 is a countercurrent heat exchanger, preferably realized as an aluminum plate heat exchanger. in the However, it differs from FIG. 8 from the subcooling heat exchanger 15 Cut.
- the liquid nitrogen 20, which is the Pump 21 is supplied instead of removal at the top of the low pressure column at least one theoretical or practical floor below the head of the Low pressure column are withdrawn.
- the liquid nitrogen 20 which is the Pump 21 is supplied instead of removal at the top of the low pressure column at least one theoretical or practical floor below the head of the Low pressure column are withdrawn.
- these floors preferably carried out as conventional rectification trays.
- FIGS. 6 to 9 a further modification can be made to the methods of FIGS. 6 to 9 be made in which a produced in the pressure column 4 Liquid nitrogen stream (160 in Figures 6 and 7) as a return to the top of the Low pressure column 5 is abandoned (via valve 161).
- This stream can also be removed from an intermediate point, the one to ten, preferably three up to five theoretical or practical floors below the head of the pressure column 4 is arranged.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
- Figur 1
- ein erstes Ausführungsbeispiel des erfindungsgemäßen Verfahrens und einer entsprechenden Vorrichtung mit einem außerhalb der Säulen angeordneten und mit Dampf aus der Drucksäule betriebenen Produktverdampfer,
- Figur 2
- ein abgewandeltes Ausführungsbeispiel mit Beheizung des Produktverdampfers durch eine Zwischenfraktion der Drucksäule,
- Figur 3
- eine weitere Variante des Beispiels von Figur 1 mit arbeitsleistender Entspannung von Restgas aus dem Kopfkondensator der Niederdrucksäule,
- Figur 4
- ein Beispiel mit arbeitsleistender Entspannung eines Gases aus der Niederdrucksäule,
- Figur 5
- ein Ausführungsbeispiel mit gleichzeitiger Gewinnung von reinem Sauerstoff in der Niederdrucksäule
- Figur 6
- ein weiteres Ausführungsbeispiel des erfindungsgemäßen Verfahrens und einer entsprechenden Vorrichtung mit einem innerhalb der Säulen angeordneten und mit Dampf aus der Niederdrucksäule betriebenen Produktverdampfer,
- Figur 7
- ein Ausführungsbeispiel mit einem innerhalb der Säulen angeordneten und mit Dampf aus der Drucksäule betriebenen Produktverdampfer und
- Figuren 8 und 9
- Ausführungsbeispiele mit einem außerhalb der Säulen angeordneten Produktverdampfer.
Claims (10)
- Verfahren zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft in einem Rektifiziersystem, das eine Drucksäule (4) und eine Niederdrucksäule (5) aufweist, wobei bei dem Verfahren Einsatzluft (1, 3; 1, 3') in die Drucksäule (4) eingeleitet, eine sauerstoffhaltige flüssige Fraktion (11) aus der Drucksäule (4) entnommen und in die Niederdrucksäule (5) eingespeist wird, gasförmiger Stickstoff (18) aus der Niederdrucksäule (5) in einem Kopfkondensator (17) durch indirekten Wärmeaustausch mit einer verdampfenden Flüssigkeit (13; 13', 44) mindestens teilweise kondensiert wird und Stickstoff aus der Niederdrucksäule als gasförmiges Druckstickstoffprodukt (24, 24', 25, 29) unter einem Druck gewonnen wird, der höher als der Betriebsdruck der Niederdrucksäule (5) ist, wobei mindestens ein Teil des bei dem indirekten Wärmeaustausch im Kopfkondensator (17) entstandenen flüssigen Stickstoffs oder aus der Niederdrucksäule abgezogener flüssiger Stickstoff (20) in flüssigem Zustand auf einen Druck gebracht (21) wird, der den Druck der Niederdrucksäule (5) übersteigt, in einem Produktverdampfer (23) durch indirekten Wärmeaustausch mit einem Wärmeträger (35; 35') verdampft wird und als Druckstickstoffprodukt (24, 24', 25, 29) gewonnen wird.
- Verfahren nach Anspruch 1, bei dem als Wärmeträger ein Gas aus der Drucksäule (4), vorzugsweise eine stickstoffhaltige Fraktion (35; 35') aus einem oberen oder mittleren Bereich der Drucksäule (4), und/oder ein Gas aus der Niederdrucksäule (5), vorzugsweise eine sauerstoffhaltige Fraktion aus einem unteren oder mittleren Bereich der Niederdrucksäule (5), eingesetzt wird.
- Verfahren nach Anspruch 1 oder 2, bei dem der flüssige Stickstoff (22) bei dem indirekten Wärmeaustausch im Produktverdampfer (23) nur teilweise verdampft und der flüssig verbliebene Anteil (45) des Stickstoffs in die Niederdrucksäule (5) zurückgeleitet wird.
- Verfahren nach einem der Ansprüche 1 bis 3, bei dem eine Prozeßfraktion (32, 31', 38) arbeitsleistend entspannt (33, 33', 33") und die bei der arbeitsleistenden Entspannung (33, 33', 33") gewonnene Energie zur Weiterverdichtung (26) des Druckstickstoffprodukts (24) stromabwärts des Produktverdampfers (23) verwendet wird.
- Verfahren nach einem der Ansprüche 1 bis 4, bei dem eine flüssige Fraktion (13'), deren Sauerstoffgehalt zwischen demjenigen der sauerstoffhaltigen flüssigen Fraktion (11) aus der Drucksäule (4) und demjenigen der Sumpfflüssigkeit (42) der Niederdrucksäule (5) liegt, zur Kondensation des gasförmigen Stickstoffs (18) aus der Niederdrucksäule (5) in dem Kopfkondensator (17) eingesetzt wird.
- Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft in einem Rektifiziersystem, das eine Drucksäule (4) und eine Niederdrucksäule (5) aufweist, mit einer Einsatzluftleitung (1, 3; 1, 3'), die in die Drucksäule (4) führt, mit einer Leitung (11) für eine sauerstoffhaltige flüssige Fraktion, die von der Drucksäule (4) in die Niederdrucksäule (5) führt, mit einem Kopfkondensator (17), dessen Verflüssigungsseite mit einem oberen Bereich der Niederdrucksäule (5) verbunden (18) ist, und mit einer Druckproduktleitung (24, 24', 25, 29) zur Entnahme von Stickstoff aus der Niederdrucksäule (5) als gasförmiges Druckprodukt, wobei die Verflüssigungsseite des Kopfkondensators (17) der Niederdrucksäule (5) oder der obere Bereich der Niederdrucksäule (5) über eine Flüssigstickstoffleitung (20, 22) mit Mitteln (21) zur Druckerhöhung einer Flüssigkeit und mit einem Produktverdampfer (23) zur Verdampfung durch indirekten Wärmeaustausch in Strömungsverbindung steht, wobei der Produktverdampfer (23) seinerseits mit der Druckproduktleitung (24, 24', 25, 29) verbunden ist.
- Vorrichtung nach Anspruch 6, bei der die Verflüssigungsseite des Produktverdampfers (23) mit einem oberen oder mittleren Bereich der Drucksäule und/oder mit einem unteren oder mittleren Bereich der Niederdrucksäule verbunden (7, 8; 35') ist.
- Vorrichtung nach Anspruch 6 oder 7, mit einer Flüssigkeitsrückleitung (45), die vom Produktverdampfer (23) in die Niederdrucksäule (5) führt.
- Vorrichtung nach einem der Ansprüche 6 bis 8, mit einer Entspannungsmaschine (33, 33', 33") zur arbeitsleistenden Entspannung einer Prozeßfraktion (32, 31', 38), die mit einem Verdichter (26) zur Weiterverdichtung des Druckstickstoffprodukts (24) stromabwärts des Produktverdampfers (23) gekoppelt ist.
- Vorrichtung nach einem der Ansprüche 6 bis 9, mit einer Flüssigkeitsleitung (13) für Kältemittel, die einerseits mit einem mittleren Bereich der Niederdrucksäule (5) oder mit einem unteren Bereich der Drucksäule und andererseits mit der Verdampfungsseite des Kopfkondensators (17) der Niederdrucksäule (5) verbunden ist.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP97948844A EP0948730B1 (de) | 1996-10-30 | 1997-10-30 | Verfahren und vorrichtung zur gewinnung von druckstickstoff |
Applications Claiming Priority (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19643916 | 1996-10-30 | ||
DE19643916 | 1996-10-30 | ||
EP97102533 | 1997-02-17 | ||
EP97102533 | 1997-02-17 | ||
DE19717124 | 1997-04-23 | ||
DE19717124 | 1997-04-23 | ||
DE19735154A DE19735154A1 (de) | 1996-10-30 | 1997-08-13 | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff |
DE19735154 | 1997-08-13 | ||
EP97948844A EP0948730B1 (de) | 1996-10-30 | 1997-10-30 | Verfahren und vorrichtung zur gewinnung von druckstickstoff |
PCT/EP1997/006010 WO1998019122A1 (de) | 1996-10-30 | 1997-10-30 | Verfahren und vorrichtung zur gewinnung von druckstickstoff |
Publications (2)
Publication Number | Publication Date |
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EP0948730A1 EP0948730A1 (de) | 1999-10-13 |
EP0948730B1 true EP0948730B1 (de) | 2000-08-30 |
Family
ID=27438467
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EP97948844A Expired - Lifetime EP0948730B1 (de) | 1996-10-30 | 1997-10-30 | Verfahren und vorrichtung zur gewinnung von druckstickstoff |
Country Status (11)
Country | Link |
---|---|
US (1) | US6196023B1 (de) |
EP (1) | EP0948730B1 (de) |
JP (1) | JP2001509246A (de) |
KR (1) | KR20000052974A (de) |
CN (1) | CN1235666A (de) |
CA (1) | CA2277838A1 (de) |
DE (2) | DE19735154A1 (de) |
DK (1) | DK0948730T3 (de) |
ES (1) | ES2150291T3 (de) |
PT (1) | PT948730E (de) |
WO (1) | WO1998019122A1 (de) |
Families Citing this family (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE19819263C2 (de) * | 1998-04-30 | 2003-08-21 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff |
EP0955509B1 (de) | 1998-04-30 | 2004-12-22 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff |
DE10018200A1 (de) * | 2000-04-12 | 2001-10-18 | Linde Gas Ag | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft |
DE10058332A1 (de) * | 2000-11-24 | 2002-05-29 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von Sauerstoff und Stickstoff |
US6397631B1 (en) | 2001-06-12 | 2002-06-04 | Air Products And Chemicals, Inc. | Air separation process |
EP1300640A1 (de) | 2001-10-04 | 2003-04-09 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von hoch reinem Stickstoff durch Tieftemperaturzerlegung von Luft |
US6499312B1 (en) | 2001-12-04 | 2002-12-31 | Praxair Technology, Inc. | Cryogenic rectification system for producing high purity nitrogen |
US6494060B1 (en) | 2001-12-04 | 2002-12-17 | Praxair Technology, Inc. | Cryogenic rectification system for producing high purity nitrogen using high pressure turboexpansion |
GB0422635D0 (en) * | 2004-10-12 | 2004-11-10 | Air Prod & Chem | Process for the cryogenic distillation of air |
CN102003865A (zh) * | 2010-11-09 | 2011-04-06 | 苏州制氧机有限责任公司 | 一种制氮装置及其制氮方法 |
US8991209B2 (en) * | 2010-12-13 | 2015-03-31 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for producing high-pressure nitrogen |
EP2662654A1 (de) * | 2012-05-07 | 2013-11-13 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Verfahren und Vorrichtung zur Abscheidung von Luft durch kryogene Destillation |
EP3027988A2 (de) * | 2013-08-02 | 2016-06-08 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur erzeugung von druckstickstoff |
CN103776239B (zh) * | 2014-01-13 | 2016-03-30 | 浙江海天气体有限公司 | 多功能制氮装置 |
US9366476B2 (en) | 2014-01-29 | 2016-06-14 | Praxair Technology, Inc. | Condenser-reboiler system and method with perforated vent tubes |
US9488408B2 (en) * | 2014-01-29 | 2016-11-08 | Praxair Technology, Inc. | Condenser-reboiler system and method |
EP3059536A1 (de) * | 2015-02-19 | 2016-08-24 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines Druckstickstoffprodukts |
EP3290843A3 (de) * | 2016-07-12 | 2018-06-13 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur erzeugung von druckstickstoff und flüssigstickstoff durch tieftemperaturzerlegung von luft |
WO2021242309A1 (en) * | 2020-05-26 | 2021-12-02 | Praxair Technology, Inc. | Enhancements to a dual column nitrogen producing cryogenic air separation unit |
WO2021242307A1 (en) * | 2020-05-28 | 2021-12-02 | Praxair Technology, Inc. | Enhancements to a dual column nitrogen producing cryogenic air separation unit |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2578532B1 (fr) * | 1985-03-11 | 1990-05-04 | Air Liquide | Procede et installation de production d'azote |
DE3528374A1 (de) * | 1985-08-07 | 1987-02-12 | Linde Ag | Verfahren und vorrichtung zur erzeugung von stickstoff mit ueberatmosphaerischem druck |
US5098457A (en) * | 1991-01-22 | 1992-03-24 | Union Carbide Industrial Gases Technology Corporation | Method and apparatus for producing elevated pressure nitrogen |
US5303556A (en) * | 1993-01-21 | 1994-04-19 | Praxair Technology, Inc. | Single column cryogenic rectification system for producing nitrogen gas at elevated pressure and high purity |
US5402647A (en) * | 1994-03-25 | 1995-04-04 | Praxair Technology, Inc. | Cryogenic rectification system for producing elevated pressure nitrogen |
-
1997
- 1997-08-13 DE DE19735154A patent/DE19735154A1/de not_active Withdrawn
- 1997-10-30 US US09/297,380 patent/US6196023B1/en not_active Expired - Fee Related
- 1997-10-30 JP JP52006298A patent/JP2001509246A/ja active Pending
- 1997-10-30 KR KR1019990703851A patent/KR20000052974A/ko not_active Application Discontinuation
- 1997-10-30 CN CN97199351A patent/CN1235666A/zh active Pending
- 1997-10-30 CA CA002277838A patent/CA2277838A1/en not_active Abandoned
- 1997-10-30 ES ES97948844T patent/ES2150291T3/es not_active Expired - Lifetime
- 1997-10-30 DE DE59702301T patent/DE59702301D1/de not_active Expired - Fee Related
- 1997-10-30 WO PCT/EP1997/006010 patent/WO1998019122A1/de not_active Application Discontinuation
- 1997-10-30 PT PT97948844T patent/PT948730E/pt unknown
- 1997-10-30 DK DK97948844T patent/DK0948730T3/da active
- 1997-10-30 EP EP97948844A patent/EP0948730B1/de not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
DE59702301D1 (de) | 2000-10-05 |
PT948730E (pt) | 2000-12-29 |
WO1998019122A1 (de) | 1998-05-07 |
JP2001509246A (ja) | 2001-07-10 |
EP0948730A1 (de) | 1999-10-13 |
CA2277838A1 (en) | 1998-05-07 |
ES2150291T3 (es) | 2000-11-16 |
DK0948730T3 (da) | 2000-10-16 |
US6196023B1 (en) | 2001-03-06 |
KR20000052974A (ko) | 2000-08-25 |
CN1235666A (zh) | 1999-11-17 |
DE19735154A1 (de) | 1998-05-07 |
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