EP0989375A1 - Process and liquefier for producing liquid air - Google Patents
Process and liquefier for producing liquid air Download PDFInfo
- Publication number
- EP0989375A1 EP0989375A1 EP99117725A EP99117725A EP0989375A1 EP 0989375 A1 EP0989375 A1 EP 0989375A1 EP 99117725 A EP99117725 A EP 99117725A EP 99117725 A EP99117725 A EP 99117725A EP 0989375 A1 EP0989375 A1 EP 0989375A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- gas
- warm
- work
- rectification
- 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.)
- Withdrawn
Links
- 238000000034 method Methods 0.000 title claims abstract description 56
- 239000007788 liquid Substances 0.000 title claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 60
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000001301 oxygen Substances 0.000 claims abstract description 8
- 239000012530 fluid Substances 0.000 claims abstract description 3
- 238000004140 cleaning Methods 0.000 claims description 15
- 238000010926 purge Methods 0.000 claims description 9
- 230000008929 regeneration Effects 0.000 claims description 9
- 238000011069 regeneration method Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 238000007906 compression Methods 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 2
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 238000005056 compaction Methods 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- 230000002040 relaxant effect Effects 0.000 claims description 2
- 239000002689 soil Substances 0.000 claims 2
- 239000002808 molecular sieve Substances 0.000 claims 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims 1
- 238000000746 purification Methods 0.000 abstract 2
- 239000000047 product Substances 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Images
Classifications
-
- 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
- F25J3/044—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 single pressure main column system only
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
- F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
- F25J1/0255—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature controlling the composition of the feed or liquefied gas, e.g. to achieve a particular heating value of natural gas
-
- 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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
- F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
-
- 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
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
-
- 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
- F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
Definitions
- the invention relates to a method for producing liquid air with a Oxygen content between 16 and 21 mol% in a low-temperature process, where atmospheric air is used as the feed gas in a warm part of the Process water vapor, carbon dioxide and airborne contaminants can be removed by cleaning, by compaction and work Relaxing process streams generated cold and in a cold part of the Process by low temperature rectification the liquid air is obtained.
- the invention also relates to a condenser for performing the method according to one of claims 1 to 9 with a cleaning station, with at least one Device for compressing process gas, with at least one device for work-relieving expansion of process gas and with a rectification column separation stages, head cooling and one installed in the rectification column Sump heating.
- Air becomes one Low-temperature process liquefied, subjected to a low-temperature rectification and one liquid air product with an oxygen content between 16.5 and 21% oxygen manufactured.
- This air is made up of an oxygen and a nitrogen product mixed (Synthetic Liquid Air, SLA).
- SLA Synthetic Liquid Air
- the object of the invention is therefore, the liquid air with less effort to manufacture as it is required as a product.
- the liquid air under Use less than four theoretical plates as a liquid top product is generated in the rectification and that also a liquid bottom product of the rectification, used exergetically and as warm residual gas to the Atmosphere or at least partially used in cleaning. So far, one had to use an order of magnitude more theoretical floors producing an oxygen and a nitrogen product is now only a small one To do a fraction of the cutting work.
- the extraction of liquid air as Top product also saves intermediate storage of liquid oxygen and liquid nitrogen.
- impurities for example hydrocarbons. The exergy content of the bottom product is largely used and the residual gas generated after use can be used be used for further use.
- the Cleaning carried out adsorptively, the residual gas as regeneration and / or Purge gas can be used. Because the liquid bottom product from the rectification is taken to an accumulation of hydrocarbons at the Avoid rectification and in the air product and there for the adsorptive cleaning Purge and regeneration gas is required, the use of the residual gas saves one otherwise providing regeneration and purge gas.
- the atmospheric air can be a warmed gas stream from the cold part of the Process mixed and the resulting warm mixed flow to one Initial pressure compressed for work-related relaxation and then cleaned become.
- the atmospheric air can be precompressed and a warmed gas flow out mixed into the cold part of the process and the resulting warm mixed flow compressed at an initial pressure for work-related relaxation and afterwards getting cleaned.
- the most favorable configuration of the compression and cleaning is by Optimizing the process and thereby determining which compressors are on the market are available.
- the purified warm mixed stream compressed to the initial pressure is preferred Countercurrent to a cold gas and the liquid bottom product of the rectification part to an initial temperature for work-related relaxation pre-cooled and further cooled by the work-relieving relaxation during a other part of said warm mixed flow in countercurrent both pre-cooled as well as further cooled, at least partially liquefied and then isenthalp relaxed and fed to the rectification as a choke flow.
- a head gas from the Rectification fed and both together as the cold gas for cooling in the Counterflow can be used. This configuration of the inventive method when both gas flows at the same pressure available.
- the liquid bottom product can cool the warm mixed stream evaporated and warmed.
- the cold content of the bottom product used in a cheap way.
- liquid bottom product for indirect cooling of the warm mixed stream evaporated, heated to an inlet temperature of a residual gas turbine over the Residual gas turbine directed, thereby cooled back and again for cooling the warm mixed current used.
- Work relaxation in the Residual gas turbine has advantages if there is a sufficiently large pressure difference between the Rectification pressure and the atmosphere or use in cleaning is present.
- Characteristic of the liquefier according to the invention is that the sump heater the rectification column as indirect heating with an electric heater or with a heating tube arrangement is executed, the heating tube arrangement being a suitable one leads warm fluid, preferably a warm process gas, and that the number of Separation stages of a theoretical number of plates of less than four theoretical plates corresponds.
- the electric heater is particularly suitable for small systems where a correspondingly higher power consumption is not significant compared to one Effort for installing a heating tube arrangement with associated Process gas lines.
- the small number of separation stages guarantees one low total pressure drop for the gas conversion in the rectification column.
- On Top condenser is omitted, since liquid from the reactor flow leads to the column return forms.
- columns are included Capacitors and used with a variety of isolators. The The condenser according to the invention thus requires less investment and because of low pressure drop in the column less energy.
- the cleaning station is preferably designed with switchable Molsiebadsorbem, wherein at least one adsorber with process gas to be cleaned and at least one further adsorber are charged with regeneration gas or purge gas, whereby as Regeneration gas or purge gas residual gas from the condenser can be used.
- the compression devices are preferably designed as turbo compressors. she can in the design of the method with a pre-compression of the air and post-compression (see above) via a common shaft and only one Be motor driven.
- the devices for work relaxation are preferred as turbines executed, the turbines particularly preferably in a turbine / booster arrangement or are integrated in a turbine / generator arrangement.
- the invention is explained in more detail using an embodiment with a figure.
- the Figure shows an inventive method with admixing a heated Gas flow to atmospheric air.
- the figure shows a schematic representation of an embodiment of the inventive method and the liquefier according to the invention.
- Atmospheric air 1 together with a warmed partial stream 2 from the cold part of the process as a warm mixed stream 3 via a compressor 4, usually with Intercooling between compressor stages (not shown in the figure), and one After cooler 5 with water separator and a cleaning 6 with switchable Molsiebadsorbern directed.
- a partial flow 7 is in a heat exchanger 8 an inlet temperature of a generator turbine 9 is pre-cooled and in the turbine 9 cooled further.
- Another part of the warm mixed stream 3 is in the Heat exchanger 8 further cooled, at least partially liquefied, as stream 10 expanded in a throttle 11 and as stream 12 of a rectification column 13 fed.
- a top gas 14 of the rectification column 13 forms together with the Via the turbine 9 relaxed partial flow 7, a cold gas 15 is the Heat exchanger 8 passes and forms as a heated gas stream 2 with the atmospheric air 1 the mixed flow 3.
- a liquid formed in the throttle 11 Phase is partly used in the rectification column 13 as reflux and one other part at the top of the rectification column as a liquid air product 16 taken.
- a bottom liquid obtained in the column is used to generate Heated steam rising in the rectification column 17.
- Part 18 of the Bottom liquid is evaporated in the heat exchanger 8, warmed as residual gas 19 at least partially used in cleaning 6 as a purge and regeneration gas and on guided the atmosphere.
- the rectification column 13 has internals 20 equipped that correspond to a theoretical number of trays less than 4. Bell bottoms are preferred.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Die Erfindung betrifft ein Verfahren zur Erzeugung von flüssiger Luft mit einem Sauerstoffgehalt zwischen 16 und 21 mol% in einem Tieftemperaturprozeß, wobei atmosphärische Luft als Einsatzgas verwendet wird, in einem warmen Teil des Verfahrens Wasserdampf, Kohlendioxid und in der Luft mitgeführte Verunreinigungen durch eine Reinigung entfernt werden, durch Verdichten und arbeitsleistendes Entspannen von Verfahrensströmen Kälte erzeugt und in einem kalten Teil des Verfahrens durch Tieftemperaturrektifikation die flüssige Luft gewonnen wird.The invention relates to a method for producing liquid air with a Oxygen content between 16 and 21 mol% in a low-temperature process, where atmospheric air is used as the feed gas in a warm part of the Process water vapor, carbon dioxide and airborne contaminants can be removed by cleaning, by compaction and work Relaxing process streams generated cold and in a cold part of the Process by low temperature rectification the liquid air is obtained.
Die Erfindung betrifft außerdem einen Verflüssiger zur Durchführung des Verfahrens
nach einem der Ansprüche 1 bis 9 mit einer Reinigungsstation, mit mindestens einer
Vorrichtung zur Verdichtung von Prozeßgas, mit mindestens einer Vorrichtung zur
arbeitsleistenden Entspannung von Prozeßgas und mit einer Rektifikationskolonne mit
in der Rektifikationskolonne installierten Trennstufen, einer Kopfkühlung und einer
Sumpfheizung.The invention also relates to a condenser for performing the method
according to one of
Aus der Veröffentlichung in Process Engineering (March 1997) "The Air that I
Breathe" ist ein Verfahren nach dem Oberbegriff des Anspruchs 1 und ein
Verflüssiger nach dem Oberbegriff des Anspruchs 10 bekannt. Luft wird in einem
Tieftemperaturprozeß verflüssigt, einer Tieftemperaturrektifikation unterworfen und ein
flüssiges Luftprodukt mit einem Sauerstoffgehalt zwischen 16,5 und 21 % Sauerstoff
hergestellt. Diese Luft wird aus einem Sauerstoff- und einem Stickstoffprodukt
gemischt (Synthetic Liquid Air, SLA). Nachteilig ist hierbei, daß erst Energie
eingesetzt wird, um die Luft zu zerlegen, und daß dann die flüssigen Produkte
Sauerstoff und Stickstoff wieder zu SLA vermischt werden.From the publication in Process Engineering (March 1997) "The Air that I
Breathe "is a method according to the preamble of
Aufgabe der Erfindung ist es daher, die flüssige Luft mit weniger Aufwand so herzustellen, wie sie als Produkt benötigt wird. The object of the invention is therefore, the liquid air with less effort to manufacture as it is required as a product.
Diese Aufgabe wird erfindungsgemäß gelöst von einem Verfahren mit den Merkmalen
des Anspruchs 1 und von einem Verflüssiger mit den Merkmalen des Anspruchs 10.
Ausführungen der Erfindung sind Gegenstand von Unteransprüchen.According to the invention, this object is achieved by a method having the features
of
Kennzeichnend an dem erfindungsgemäßen Verfahren ist, daß die flüssige Luft unter Verwendung von weniger als vier theoretischen Böden als ein flüssiges Kopfprodukt bei der Rektifikation erzeugt wird und daß außerdem ein flüssiges Sumpfprodukt bei der Rektifikation gewonnen, exergetisch genutzt und als warmes Restgas an die Atmosphäre geleitet oder mindestens teilweise bei der Reinigung verwendet wird. Mußte man bisher um eine Größenordnung mehr theoretische Böden einsetzen um ein Sauerstoff- und ein Stickstoffprodukt zu erzeugen, so ist jetzt nur ein kleiner Bruchteil der Trennarbeit zu verrichten. Die Gewinnung der flüssigen Luft als Kopfprodukt erspart außerdem ein Zwischenspeichern von flüssigem Sauerstoff und flüssigem Stickstoff. Mit dem flüssigen Sumpfprodukt werden Verunreinigungen, beispielsweise Kohlenwasserstoffe, abgezogen. Der Exergieinhalt des Sumpfprodukts wird weitgehend genutzt und das nach der Nutzung anfallende Restgas kann einer weiteren Nutzung zugeführt werden.It is characteristic of the method according to the invention that the liquid air under Use less than four theoretical plates as a liquid top product is generated in the rectification and that also a liquid bottom product of the rectification, used exergetically and as warm residual gas to the Atmosphere or at least partially used in cleaning. So far, one had to use an order of magnitude more theoretical floors producing an oxygen and a nitrogen product is now only a small one To do a fraction of the cutting work. The extraction of liquid air as Top product also saves intermediate storage of liquid oxygen and liquid nitrogen. With the liquid bottom product, impurities, for example hydrocarbons. The exergy content of the bottom product is largely used and the residual gas generated after use can be used be used for further use.
Bei einer vorteilhaften Ausgestaltung des erfindungsgemäßen Verfahrens wird die Reinigung adsorptiv vorgenommen, wobei das Restgas als Regenerier- und/oder Spülgas verwendet werden kann. Da das flüssige Sumpfprodukt aus der Rektifikation entnommen wird, um eine Anreicherung von Kohlenwasserstoffen bei der Rektifikation und im Luftprodukt zu vermeiden und da für die adsorptive Reinigung Spül- und Regeneriergas benötigt wird, erspart die Nutzung des Restgases eine anderweitige Bereitstellung von Regenerier- und Spülgas.In an advantageous embodiment of the method according to the invention, the Cleaning carried out adsorptively, the residual gas as regeneration and / or Purge gas can be used. Because the liquid bottom product from the rectification is taken to an accumulation of hydrocarbons at the Avoid rectification and in the air product and there for the adsorptive cleaning Purge and regeneration gas is required, the use of the residual gas saves one otherwise providing regeneration and purge gas.
Der atmosphärischen Luft kann ein angewärmter Gasstrom aus dem kalten Teil des Verfahrens zugemischt und der resultierende warme Mischstrom auf einen Anfangsdruck für arbeitsleistendes Entspannen verdichtet und danach gereinigt werden.The atmospheric air can be a warmed gas stream from the cold part of the Process mixed and the resulting warm mixed flow to one Initial pressure compressed for work-related relaxation and then cleaned become.
Alternativ kann die atmosphärische Luft vorverdichtet, ein angewärmter Gasstrom aus dem kalten Teil des Verfahrens zugemischt und der resultierende warme Mischstrom auf einem Anfangsdruck für arbeitsleistendes Entspannen verdichtet und danach gereinigt werden. Alternatively, the atmospheric air can be precompressed and a warmed gas flow out mixed into the cold part of the process and the resulting warm mixed flow compressed at an initial pressure for work-related relaxation and afterwards getting cleaned.
Bei einer anderen Ausgestaltung des erfindungsgemäßen Verfahrens wird die atmosphärische Luft vorverdichtet und danach gereinigt, ein angewärmter Gasstrom aus dem kalten Teil des Verfahrens zugemischt und der resultierende warme Mischstrom auf einen Anfangsduck für arbeitsleistendes Entspannen verdichtet.In another embodiment of the method according to the invention atmospheric air pre-compressed and then cleaned, a warmed gas stream admixed from the cold part of the process and the resulting warm mixing stream compressed to an initial pressure for work-related relaxation.
Die jeweils günstigste Ausgestaltung der Verdichtung und Reinigung wird durch Optimieren des Verfahrens und dadurch bestimmt, welche Verdichter am Markt erhältlich sind.The most favorable configuration of the compression and cleaning is by Optimizing the process and thereby determining which compressors are on the market are available.
Bevorzugt wird der auf den Anfangsdruck verdichtete gereinigte warme Mischstrom im Gegenstrom zu einem Kaltgas und dem flüssigen Sumpfprodukt der Rektifikation zu einem Teil auf eine Anfangstemperatur für das arbeitsleistende Entspannen vorgekühlt und durch das arbeitsleistende Entspannen weiter abgekühlt, während ein anderer Teil des besagten warmen Mischstromes im Gegenstrom sowohl vorgekühlt als auch weiter abgekühlt, mindestens teilweise verflüssigt und anschließend isenthalp entspannt und als Drosselstrom der Rektifikation zugeführt wird.The purified warm mixed stream compressed to the initial pressure is preferred Countercurrent to a cold gas and the liquid bottom product of the rectification part to an initial temperature for work-related relaxation pre-cooled and further cooled by the work-relieving relaxation during a other part of said warm mixed flow in countercurrent both pre-cooled as well as further cooled, at least partially liquefied and then isenthalp relaxed and fed to the rectification as a choke flow.
Dem arbeitsleistend entspannten Teil des Mischstromes kann ein Kopfgas aus der Rektifikation zugeführt und beide zusammen als das Kaltgas für die Kühlung im Gegenstrom verwendet werden. Besonders vorteilhaft ist diese Ausgestaltung des erfindungsgemäßen Verfahrens, wenn beide Gasströme bei gleichem Druck vorliegen.A head gas from the Rectification fed and both together as the cold gas for cooling in the Counterflow can be used. This configuration of the inventive method when both gas flows at the same pressure available.
Das flüssige Sumpfprodukt kann bei der Kühlung des warmen Mischstromes verdampft und angewärmt werden. Dabei wird der Kälteinhalt des Sumpfproduktes auf eine günstige Art und Weise genutzt.The liquid bottom product can cool the warm mixed stream evaporated and warmed. The cold content of the bottom product used in a cheap way.
Bei einer anderen Ausgestaltung des erfindungsgemäßen Verfahrens wird das flüssige Sumpfprodukt bei der indirekten Kühlung des warmen Mischstromes verdampft, auf eine Eintrittstemperatur einer Restgasturbine erwärmt über die Restgasturbine geleitet, dadurch wieder zurückgekühlt und wieder zur Kühlung des warmen Mischstromes verwendet. Die arbeitsleistende Entspannung in der Restgasturbine hat Vorteile, wenn ein ausreichend großes Druckgefälle zwischen dem Rektifikationsdruck und der Atmosphäre bzw. der Verwendung bei der Reinigung vorliegt.In another embodiment of the method according to the invention liquid bottom product for indirect cooling of the warm mixed stream evaporated, heated to an inlet temperature of a residual gas turbine over the Residual gas turbine directed, thereby cooled back and again for cooling the warm mixed current used. Work relaxation in the Residual gas turbine has advantages if there is a sufficiently large pressure difference between the Rectification pressure and the atmosphere or use in cleaning is present.
Kennzeichnend an dem erfindungsgemäßen Verflüssiger ist, daß die Sumpfheizung der Rektifikationskolonne als indirekte Heizung mit einem Elektroerhitzer oder mit einer Heizrohranordnung ausgeführt ist, wobei die Heizrohranordnung ein geeignetes warmes Fluid, vorzugsweise ein warmes Prozeßgas führt, und daß die Anzahl der Trennstufen einer theoretischen Bodenzahl von weniger als vier theoretischen Böden entspricht.Characteristic of the liquefier according to the invention is that the sump heater the rectification column as indirect heating with an electric heater or with a heating tube arrangement is executed, the heating tube arrangement being a suitable one leads warm fluid, preferably a warm process gas, and that the number of Separation stages of a theoretical number of plates of less than four theoretical plates corresponds.
Der Elektroerhitzer eignet sich besonders für kleine Anlagen, bei denen ein entsprechend höherer Stromverbrauch nicht ins Gewicht fällt verglichen mit einem Aufwand für die Installation einer Heizrohranordnung mit zugehörigen Prozeßgasleitungen. Die geringe Anzahl von Trennstufen gewährleistet einen geringen Gesamtdruckabfall für den Gasumsatz in der Rektifikationskolonne. Ein Kopfkondensator entfällt, da Flüssigkeit aus dem Drosselstrom den Kolonnenrücklauf bildet. In Verfahren nach dem Stand der Technik hingegen werden Kolonnen mit Kondensatoren und mit einer Vielzahl von Trennstufen eingesetzt. Der erfindungsgemäße Verflüssiger benötigt somit weniger Investition und wegen des geringen Druckabfalls in der Kolonne weniger Energie.The electric heater is particularly suitable for small systems where a correspondingly higher power consumption is not significant compared to one Effort for installing a heating tube arrangement with associated Process gas lines. The small number of separation stages guarantees one low total pressure drop for the gas conversion in the rectification column. On Top condenser is omitted, since liquid from the reactor flow leads to the column return forms. In contrast, in processes according to the prior art, columns are included Capacitors and used with a variety of isolators. The The condenser according to the invention thus requires less investment and because of low pressure drop in the column less energy.
Die Reinigungsstation ist bevorzugt mit umschaltbaren Molsiebadsorbem ausgeführt, wobei mindestens ein Adsorber mit zu reinigendem Prozeßgas und mindestens ein weiterer Adsorber mit Regeneriergas oder Spülgas beaufschlagt sind, wobei als Regeneriergas oder Spülgas Restgas aus dem Verflüssiger verwendet werden kann.The cleaning station is preferably designed with switchable Molsiebadsorbem, wherein at least one adsorber with process gas to be cleaned and at least one further adsorber are charged with regeneration gas or purge gas, whereby as Regeneration gas or purge gas residual gas from the condenser can be used.
Die Vorrichtungen zur Verdichtung sind bevorzugt als Turboverdichter ausgeführt. Sie können bei der Ausgestaltung des Verfahrens mit einer Vorverdichtung der Luft und einer Nachverdichtung (siehe oben) über eine gemeinsame Welle und nur einen Motor angetrieben sein.The compression devices are preferably designed as turbo compressors. she can in the design of the method with a pre-compression of the air and post-compression (see above) via a common shaft and only one Be motor driven.
Die Vorrichtungen zur arbeitsleistenden Entspannung sind bevorzugt als Turbinen ausgeführt, wobei die Turbinen besonders bevorzugt in einer Turbinen/Booster-Anordnung oder in einer Turbinen/ Generator-Anordnung integriert sind. The devices for work relaxation are preferred as turbines executed, the turbines particularly preferably in a turbine / booster arrangement or are integrated in a turbine / generator arrangement.
Die Erfindung wird anhand einer Ausführungsform mit einer Figur näher erläutert. Die Figur zeigt ein erfindungsgemäßes Verfahren mit Zumischen eines angewärmten Gasstromes zur atmosphärischen Luft.The invention is explained in more detail using an embodiment with a figure. The Figure shows an inventive method with admixing a heated Gas flow to atmospheric air.
Die Figur zeigt in einer schematischen Darstellung eine Ausgestaltung des
erfindungsgemäßen Verfahrens und des erfindungsgemäßen Verflüssigers.
Atmosphärische Luft 1 wird zusammen mit einem angewärmten Teilstrom 2 aus dem
kalten Teil des Verfahrens als warmer Mischstrom 3 über einen Verdichter 4, meist mit
Zwischenkühlung zwischen Verdichterstufen (in der Figur nicht dargestellt), und einen
Nachkühler 5 mit Wasserabscheider und eine Reinigung 6 mit umschaltbaren
Molsiebadsorbern geleitet. Ein Teilstrom 7 wird in einem Wärmeaustauscher 8 auf
eine Eintrittstemperatur einer Generatorturbine 9 vorgekühlt und in der Turbine 9
weiter abgekühlt. Ein anderer Teil des warmen Mischstromes 3 wird im
Wärmeaustauscher 8 weiter abgekühlt, mindestens teilweise verflüssigt, als Strom 10
in einer Drossel 11 entspannt und als Strom 12 einer Rektifikationskolonne 13
zugeführt. Ein Kopfgas 14 der Rektifikationskolonne 13 bildet zusammen mit dem
über die Turbine 9 entspannten Teilstrom 7 ein Kaltgas 15, wird über den
Wärmeaustauscher 8 geleitet und bildet als angewärmter Gasstrom 2 mit der
atmosphärischen Luft 1 den Mischstrom 3. Eine in der Drossel 11 gebildete flüssige
Phase wird teils in der Rektifikationskolonne 13 als Rücklauf genutzt und zu einem
anderen Teil am Kopf der Rektifikationskolonne als flüssiges Luftprodukt 16
entnommen. Eine in der Kolonne anfallende Sumpfflüssigkeit wird zur Erzeugung von
in der Rektifikationskolonne aufsteigendem Dampf beheizt 17. Ein Teil 18 der
Sumpfflüssigkeit wird im Wärmeaustauscher 8 verdampft, angewärmt, als Restgas 19
mindestens teilweise in der Reinigung 6 als Spül- und Regeneriergas genutzt und an
die Atmosphäre geleitet. Die Rektifikationskolonne 13 ist mit Einbauten 20
ausgestattet, die einer theoretischen Bodenzahl kleiner als 4 entsprechen.
Glockenböden werden bevorzugt.The figure shows a schematic representation of an embodiment of the
inventive method and the liquefier according to the invention.
Für das erfindungsgemäße Verfahren gemäß Figur sind in der Tabelle
Verfahrensdaten angegeben.
Phase = 2 entspricht einem Dampfanteil = 0 mol%
Verdampferleistung: 10 kW
Verdichterleistung: 1 MW
Phase = 2 corresponds to a steam fraction = 0 mol%
Evaporator power: 10 kW
Compressor output: 1 MW
Claims (13)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19843629A DE19843629A1 (en) | 1998-09-23 | 1998-09-23 | Process and liquefier for the production of liquid air |
| DE19843629 | 1998-09-23 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| EP0989375A1 true EP0989375A1 (en) | 2000-03-29 |
Family
ID=7881973
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP99117725A Withdrawn EP0989375A1 (en) | 1998-09-23 | 1999-09-08 | Process and liquefier for producing liquid air |
Country Status (3)
| Country | Link |
|---|---|
| US (1) | US6230518B1 (en) |
| EP (1) | EP0989375A1 (en) |
| DE (1) | DE19843629A1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1050729A1 (en) * | 1999-05-04 | 2000-11-08 | Praxair Technology, Inc. | Cryogenic air separation system comprising a dephlegmator |
| WO2013185783A1 (en) | 2012-06-11 | 2013-12-19 | Arano-Trade Ltd. | Energy transformation system |
| EP3552971A3 (en) * | 2018-03-23 | 2020-02-12 | United Technologies Corporation | Propulsion system cooling control |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5979440A (en) * | 1997-06-16 | 1999-11-09 | Sequal Technologies, Inc. | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
| US7086231B2 (en) * | 2003-02-05 | 2006-08-08 | Active Power, Inc. | Thermal and compressed air storage system |
| US20060059936A1 (en) * | 2004-09-17 | 2006-03-23 | Radke Robert E | Systems and methods for providing cooling in compressed air storage power supply systems |
| US8333330B2 (en) * | 2004-09-17 | 2012-12-18 | Active Power, Inc. | Systems and methods for controlling temperature and pressure of fluids |
| US7314059B2 (en) * | 2004-09-17 | 2008-01-01 | Active Power, Inc. | Systems and methods for controlling pressure of fluids |
| JP2011506895A (en) * | 2007-12-07 | 2011-03-03 | ドレッサー ランド カンパニー | Compressor apparatus and method for gas liquefaction system |
| US7821158B2 (en) * | 2008-05-27 | 2010-10-26 | Expansion Energy, Llc | System and method for liquid air production, power storage and power release |
| US20100024478A1 (en) * | 2008-07-29 | 2010-02-04 | Horst Corduan | Process and device for recovering argon by low-temperature separation of air |
| US8907524B2 (en) | 2013-05-09 | 2014-12-09 | Expansion Energy Llc | Systems and methods of semi-centralized power storage and power production for multi-directional smart grid and other applications |
| US10655913B2 (en) | 2016-09-12 | 2020-05-19 | Stanislav Sinatov | Method for energy storage with co-production of peaking power and liquefied natural gas |
| US11835270B1 (en) | 2018-06-22 | 2023-12-05 | Booz Allen Hamilton Inc. | Thermal management systems |
| US11293673B1 (en) | 2018-11-01 | 2022-04-05 | Booz Allen Hamilton Inc. | Thermal management systems |
| US11448431B1 (en) | 2018-11-01 | 2022-09-20 | Booz Allen Hamilton Inc. | Thermal management systems for extended operation |
| US11421917B1 (en) * | 2018-11-01 | 2022-08-23 | Booz Allen Hamilton Inc. | Thermal management systems |
| US11835271B1 (en) | 2019-03-05 | 2023-12-05 | Booz Allen Hamilton Inc. | Thermal management systems |
| US11629892B1 (en) | 2019-06-18 | 2023-04-18 | Booz Allen Hamilton Inc. | Thermal management systems |
| US11752837B1 (en) | 2019-11-15 | 2023-09-12 | Booz Allen Hamilton Inc. | Processing vapor exhausted by thermal management systems |
| US11561030B1 (en) | 2020-06-15 | 2023-01-24 | Booz Allen Hamilton Inc. | Thermal management systems |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4169361A (en) * | 1975-10-28 | 1979-10-02 | Linde Aktiengesellschaft | Method of and apparatus for the generation of cold |
| DE4303670A1 (en) * | 1993-02-09 | 1994-08-11 | Foerster Hans Dr | Method for the separation of vaporous components from air and industrial gases |
| US5373699A (en) * | 1989-08-18 | 1994-12-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes George Claude | Process for the production of nitrogen by cryogenic distillation of atmospheric air |
| US5507147A (en) * | 1994-05-05 | 1996-04-16 | Foerster; Hans | Method of separating vaporous substances from air saturated with high proportions of components having a low boiling point |
| US5546765A (en) * | 1994-09-14 | 1996-08-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Air separating unit |
| EP0774634A2 (en) * | 1995-11-17 | 1997-05-21 | The BOC Group plc | Gas manufacture |
| EP0856713A2 (en) * | 1997-01-31 | 1998-08-05 | The BOC Group plc | Production of cryogenic liquid mixtures |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5379598A (en) * | 1993-08-23 | 1995-01-10 | The Boc Group, Inc. | Cryogenic rectification process and apparatus for vaporizing a pumped liquid product |
| FR2714721B1 (en) * | 1993-12-31 | 1996-02-16 | Air Liquide | Method and installation for liquefying a gas. |
| US5454227A (en) * | 1994-08-17 | 1995-10-03 | The Boc Group, Inc. | Air separation method and apparatus |
-
1998
- 1998-09-23 DE DE19843629A patent/DE19843629A1/en not_active Withdrawn
-
1999
- 1999-09-08 EP EP99117725A patent/EP0989375A1/en not_active Withdrawn
- 1999-09-23 US US09/401,949 patent/US6230518B1/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4169361A (en) * | 1975-10-28 | 1979-10-02 | Linde Aktiengesellschaft | Method of and apparatus for the generation of cold |
| US5373699A (en) * | 1989-08-18 | 1994-12-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes George Claude | Process for the production of nitrogen by cryogenic distillation of atmospheric air |
| DE4303670A1 (en) * | 1993-02-09 | 1994-08-11 | Foerster Hans Dr | Method for the separation of vaporous components from air and industrial gases |
| US5507147A (en) * | 1994-05-05 | 1996-04-16 | Foerster; Hans | Method of separating vaporous substances from air saturated with high proportions of components having a low boiling point |
| US5546765A (en) * | 1994-09-14 | 1996-08-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Air separating unit |
| EP0774634A2 (en) * | 1995-11-17 | 1997-05-21 | The BOC Group plc | Gas manufacture |
| EP0856713A2 (en) * | 1997-01-31 | 1998-08-05 | The BOC Group plc | Production of cryogenic liquid mixtures |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1050729A1 (en) * | 1999-05-04 | 2000-11-08 | Praxair Technology, Inc. | Cryogenic air separation system comprising a dephlegmator |
| WO2013185783A1 (en) | 2012-06-11 | 2013-12-19 | Arano-Trade Ltd. | Energy transformation system |
| EP3552971A3 (en) * | 2018-03-23 | 2020-02-12 | United Technologies Corporation | Propulsion system cooling control |
| US11299279B2 (en) | 2018-03-23 | 2022-04-12 | Raytheon Technologies Corporation | Chilled working fluid generation and separation for an aircraft |
| US11305879B2 (en) | 2018-03-23 | 2022-04-19 | Raytheon Technologies Corporation | Propulsion system cooling control |
| US11542016B2 (en) | 2018-03-23 | 2023-01-03 | Raytheon Technologies Corporation | Cryogenic cooling system for an aircraft |
Also Published As
| Publication number | Publication date |
|---|---|
| DE19843629A1 (en) | 2000-03-30 |
| US6230518B1 (en) | 2001-05-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0989375A1 (en) | Process and liquefier for producing liquid air | |
| EP0505812B1 (en) | Low temperature air separation process | |
| DE69509841T2 (en) | Method and device for producing oxygen | |
| EP0316768B1 (en) | Air separation process by low temperature rectification | |
| DE69012923T2 (en) | Method and device for producing nitrogen from air. | |
| DE69509836T2 (en) | Air separation method and apparatus | |
| DE69413918T2 (en) | Cryogenic air separation | |
| EP0100923B1 (en) | Process and apparatus for separating a gas mixture | |
| DE69201522T2 (en) | High pressure air separation process with extraction of liquid. | |
| EP0758733A2 (en) | Air separation process and apparatus by low temperature rectification | |
| EP1074805B1 (en) | Process for producing oxygen under pressure and device therefor | |
| DE2544340A1 (en) | PROCEDURE FOR AIR SEPARATION | |
| DE3817244A1 (en) | METHOD FOR DEEP TEMPERATURE DISPOSAL OF AIR | |
| DE69420882T2 (en) | Method and device for producing gaseous oxygen and / or gaseous nitrogen under pressure by decomposing air | |
| DE69814519T2 (en) | Cryogenic process with double acid and external evaporator condenser for an oxygen and nitrogen mixture | |
| WO2010017968A2 (en) | Process and device for cryogenic air fractionation | |
| DE69614950T2 (en) | METHOD AND DEVICE FOR PRODUCING HIGH PURITY NITROGEN | |
| DE3528374A1 (en) | METHOD AND DEVICE FOR PRODUCING NITROGEN WITH OVER-ATMOSPHERIC PRESSURE | |
| WO2014026738A2 (en) | Method and device for generating electrical energy | |
| EP0363861B1 (en) | Process for obtaining impure argon | |
| EP0768503B1 (en) | Triple column air separation process | |
| DE69520134T2 (en) | Method and device for compressing a gas mixture to be distilled and for relaxing at least one gas stream | |
| DE4210638A1 (en) | High purity hydrogen and carbon mon:oxide recovery from dry gas mixt. - by one stage partial condensation and purificn. giving high yield at reduced cost | |
| DE69414282T2 (en) | Process and plant for the production of pressurized oxygen | |
| DE4030750A1 (en) | Combination triple duty compressor for prodn. of nitrogen@ and oxygen@ - has multiple shaft machine providing compression for feed air, first main stage, and coolant nitrogen streams |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
| AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
| AX | Request for extension of the european patent |
Free format text: AL;LT;LV;MK;RO PAYMENT 19990908;SI PAYMENT 19990908 |
|
| 17P | Request for examination filed |
Effective date: 20000228 |
|
| RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: LINDE TECHNISCHE GASE GMBH |
|
| AKX | Designation fees paid |
Free format text: AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
| AXX | Extension fees paid |
Free format text: RO PAYMENT 19990908;SI PAYMENT 19990908 |
|
| RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: LINDE GAS AG |
|
| 17Q | First examination report despatched |
Effective date: 20010702 |
|
| RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: LINDE AG |
|
| STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
| 18D | Application deemed to be withdrawn |
Effective date: 20020115 |