EP0716280B1 - Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft - Google Patents
Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft Download PDFInfo
- Publication number
- EP0716280B1 EP0716280B1 EP95118951A EP95118951A EP0716280B1 EP 0716280 B1 EP0716280 B1 EP 0716280B1 EP 95118951 A EP95118951 A EP 95118951A EP 95118951 A EP95118951 A EP 95118951A EP 0716280 B1 EP0716280 B1 EP 0716280B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- condenser
- evaporator
- air
- substream
- 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.)
- Expired - Lifetime
Links
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
- F25J3/04006—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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
-
- 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
-
- 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
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/923—Inert gas
- Y10S62/924—Argon
Definitions
- the invention relates to a method and a device for cryogenic decomposition of air in which a first partial stream of compressed and cleaned air cools, fed to a main rectification system and there in liquid oxygen and gaseous nitrogen is broken down, being in a first condenser-evaporator a liquid product fraction in indirect heat exchange with a second Partial stream of compressed and cleaned air evaporates, the second partial stream at the indirect heat exchange in the first condenser-evaporator at least partially condensed and an argon-containing oxygen fraction from the Main rectification system fed to a raw argon column and there in raw argon and in an oxygen-rich residual liquid is separated and being vaporous Raw argon from the top of the raw argon column through indirect heat exchange with at least part of the second partial flow downstream of the first condenser-evaporator is liquefied in a second condenser-evaporator, wherein in the second condenser-evaporator at least part of the second partial flow evaporates.
- the invention is therefore based on the object, the method and the device of the type mentioned at the outset to be particularly economical and in particular a particularly high product purity and / or a particularly large one Product yield with a particularly low equipment and operational technology To achieve effort and / or with a particularly low energy consumption.
- This object is achieved in the invention in that the entire or in essentially all of the cold required to liquefy raw argon the evaporation of the second partial stream is made available.
- the amount of refrigeration required for the liquefaction of raw argon corresponds at least the heat of vaporization of the return flow for the crude argon column. If liquid argon is withdrawn from the raw argon column, the Refrigeration quantity for product quantity, for example if the Product liquefaction takes place in the second condenser evaporator; alternatively can the product liquefaction of the raw argon with the help of another refrigerant be carried out, preferably in a separate capacitor. With “im essentially all "are at least 90%, preferably at least 95%, most preferably at least 99% of this amount of cold is meant. The rest of The amount of cold can be, for example, by adding a small amount further liquid fraction (e.g.
- a single heat exchanger is preferably used as the second Condenser evaporator used It can also be used by more than one apparatus Block be realized, the evaporation spaces communicate with each other.
- the nitrogen content of the liquefied air in the second partial flow higher than that in the sump liquid from one of the pillars of the Main rectification system, usually in the top condenser of the crude argon column is evaporated.
- the Separation performance of the crude argon column can be improved, or you can (cheaper) Mass transfer elements with higher pressure loss per theoretical floor use and still achieve a high separation effect.
- the liquid product fraction can in the invention by any air component or be formed by any mixture of air components, for example through oxygen or nitrogen or through an intermediate such as raw argon, which contains small amounts of oxygen and / or nitrogen in addition to argon.
- the liquid can be, for example Rectification column or a storage or buffer tank.
- Be the first Condenser evaporators can be the main heat exchanger in which also the Heating of the gaseous products against feed air takes place, or a separate heat exchanger (secondary condenser) can be used.
- the second partial air flow can, for example, 35 to 45 mol%, preferably contain 35 to 40 mol% of the total amount of feed air; the rest of Feed air or part of it forms the first partial air flow.
- the invention can advantageously be applied to a double column process, so if the main rectification system is a pressure column and a low pressure column
- the first partial air flow is introduced into the pressure column and the deducted argon-containing oxygen fraction from the low pressure column.
- the liquid product fraction against which the second partial air flow condenses in in this case formed by a liquid oxygen stream from the low pressure column.
- the condenser-evaporator vaporized the second partial stream without further Pressure increase is initiated in the main rectification system.
- the entire liquefied second air stream are passed into the second condenser-evaporator, wherein some or all of the steam generated therein is transferred to a rectification column (for example, the low pressure column of a double column).
- the second partial flow in the indirect Heat exchange with the liquid oxygen flow is under a pressure that is higher than the highest pressure in the main rectification system, for example under one supercritical pressure; the pressure of the second partial air flow can be 30 to, for example 55 bar, preferably 45 to 52 bar above the highest pressure in the Main rectification system (e.g. the operating pressure of a pressure column).
- the Liquefaction temperature against the evaporating product fraction condensing air can thus reach the evaporation temperature of the Product fraction to be adjusted.
- the post-compressed air can also be used to generate refrigeration work-related relaxation can be used.
- the Partial pressure energy in the second partial flow in a work-relieving relaxation be recovered (see EP-B-93448).
- the standard volume at least 21%, for example 21 to 30%, preferably 22 to 25% of the amount of feed air corresponds to the main rectification system in liquid form.
- the amount refers to the standard volume.
- This liquid withdrawal can be done both by Lead out of the rectifying column or columns in a liquid state and subsequent external evaporation, preferably under pressure (e.g. Evaporation of the liquid product fraction in the first condenser-evaporator), as also by removal as a liquid product, for example for storage in Tanks.
- the share of 21% can be achieved, for example, that the entire oxygen product in the first condenser evaporator evaporates and additionally a small amount of nitrogen and / or oxygen as a liquid product be won.
- a third partial flow of compressed and cleaned air is preferred relaxed workload and fed to the main rectification system. Its amount is, for example, 0 to 45 mol%, preferably 15 to 40 mol% of the total Feed air; the second partial air flow contains, for example, 35 to 45 mol%, preferably 35 to 40 mol% of the total amount of feed air; the rest of Feed air forms the first partial air flow.
- the third partial flow can be branched off from the second partial flow, for example, preferably downstream of a post-compressor, the second partial flow brings a pressure above the maximum pressure of the main rectification system.
- the third can Partial stream branched off from the first or even identical to the first partial stream his.
- the relaxed third partial flow preferably fed into the pressure column.
- the work-relieving relaxation of the third partial flow can (for example after branching off from the first partial flow) also of about Bring pressure column pressure to low pressure column pressure; the relaxed air must then be led into the low pressure column.
- a further liquid product stream can advantageously be operated in an indirect manner Heat exchange with compressed and cleaned air can be evaporated.
- Heat exchange with compressed and cleaned air can be evaporated.
- a smaller one Liquid flow of nitrogen and / or raw argon latent heat with condensing Exchange air for example with the second partial air flow.
- a first partial stream 101 of compressed and cleaned air 1 is under pressure from 5 to 10 bar, preferably 5.5 to 6.5 bar in a main heat exchanger 2 in indirect heat exchange with product streams cooled to about dew point.
- the main rectification system has a double column 4 with a pressure column 5 (5 to 10 bar, preferably 5.5 to 6.5 bar), low pressure column 6 (1.3 to 2 bar, preferably 1.5 to 1.7 bar) and intermediate main condenser 7. Bottom liquid 9 out the pressure column 5 is in a counterflow 8 against product flows Low-pressure column supercooled and fed into the low-pressure column 6 (line 10).
- Gaseous nitrogen 11 from the top of the pressure column 5 is in the main condenser 7 liquefied against evaporating liquid in the sump of the low pressure column 6
- Some of the condensate 12 is fed to the pressure column 5 as a return (Line 13) and to another part 14 after hypothermia 8 in the Low pressure column 6 fed (15).
- Low pressure nitrogen 16 and impure nitrogen 17 are after removal from the low pressure column 6 in the heat exchangers 8 and 2 warmed to about ambient temperature.
- Product oxygen is the liquid oxygen stream 18 from the bottom of the Low pressure column 6 withdrawn and by means of a pump 19 to an increased pressure brought from, for example, 5 to 80 bar, depending on the product pressure required. (Of course there are also other methods for increasing the pressure in the liquid Phase applicable, for example by using a hydrostatic potential or by pressure build-up evaporation on a storage tank.)
- the liquid High pressure oxygen 20 is evaporated in the main heat exchanger 2 and as withdrawn internally compressed gaseous product 21.
- a second partial flow 201, 202 of the compressed and cleaned air condenses after being in a post-compressor 206 was brought to a pressure of 12 to 60 bar, preferably 15 to 40 bar.
- An argon-containing oxygen fraction 22 from the low pressure column 6 is in a Raw argon column 24 in raw argon at the top of the column and in an oxygen-rich Residual liquid disassembled. The latter is via line 23, optionally through a Pump pumped, fed back into the low pressure column 6. To generate Return 25 and possibly to obtain liquid raw argon 26 that gaseous raw argon in a top condenser 27 by indirect Liquefied heat exchange. (The raw argon product can alternatively or additionally are removed as gas.)
- Argon production by air separation is also described in EP-B-377117 and the older applications DE 4406051 (EP-A-669508), DE 4406049 and DE 4406069 (EP-A-669509).
- the liquefied second partial stream 203/204 is fed to the Evaporation side of the top condenser 27 of the crude argon column passed and there evaporates.
- the second partial flow is previously subcooled in counterflow 8 and throttled to about low pressure column pressure (e.g. not by a expansion valve shown).
- the indirect heat exchange with Vapor produced from crude argon is fed via line 205 to the low pressure column 6 and / or passed via 205a into the product line 17 for impure nitrogen.
- liquid nitrogen from the pressure column via the lines 28 and 29 led to the main heat exchanger 2 and via line 30 as gaseous Product will be deducted.
- the liquid nitrogen can be internally compressed if necessary by a pump 31, for example.
- liquid crude argon which is gaseous increased pressure is required.
- Raw argon can - just like the one to be vaporized Nitrogen and oxygen flows - either from a column or from a buffer or Storage tank can be removed.
- the invention is applicable in particular on the raw argon internal compression according to EP-A-171711, EP-B-331028 or EP-B-363861.
- the evaporation of the liquid product (s) against the second partial flow of air can also deviate from the representation in the drawing in one or more Secondary condensers, which are separated from the main heat exchanger become.
- Part of the oxygen product can be obtained as a liquid product (line 33); it is also possible to remove a certain amount of oxygen from the gas Remove low pressure column 6 and heat it up in the main heat exchanger 2 (in the drawing not shown).
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
Druck in bar | |
Luftdruck (Leitung 1) | 6,50 |
Zweiter Teilstrom 202/203 | 58,0 |
Drucksäule 5 | 6,20 |
Niederdrucksäule 6 | 1,60 |
Kopf der Rohargonsäule 24 | 1,05 |
Verdampfungsseite des Rohargonkondensators 27 | 1,40 |
Innenverdichteter Sauerstoff (Leitung 20) | 20,0 |
Innenverdichteter Stickstoff (Leitung 29) | 25,0 |
Claims (10)
- Verfahren zur Tieftemperaturzerlegung von Luft, bei dem ein erster Teilstrom (101) von verdichteter und gereinigter Luft (1) abgekühlt (2), einem Hauptrektifiziersystem (4) zugeführt und dort in flüssigen Sauerstoff und gasförmigen Stickstoff zerlegt wird, wobei in einem ersten Kondensator-Verdampfer (2) eine flüssige Produktfraktion (20; 29) in indirektem Wärmeaustausch mit einem zweiten Teilstrom (202, 203) von verdichteter und gereinigter Luft verdampft, der zweite Teilstrom (202, 203) bei dem indirekten Wärmeaustausch in dem ersten Kondensator-Verdampfer (2) mindestens teilweise kondensiert und eine argonhaltige Sauerstofffraktion (22) aus dem Hauptrektifiziersystem (4) einer Rohargonsäule (24) zugeführt und dort in Rohargon und in eine sauerstoffreiche Restflüssigkeit getrennt wird und wobei dampfförmiges Rohargon vom Kopf der Rohargonsäule durch indirekten Wärmeaustausch mit mindestens einem Teil des zweiten Teilstroms (203) stromabwärts des ersten Kondensator-Verdampfers (2) in einem zweiten Kondensator-Verdampfer (27) verflüssigt wird, wobei in dem zweiten Kondensator-Verdampfer (27) mindestens ein Teil des zweiten Teilstroms (203) verdampft, dadurch gekennzeichnet, daß die gesamte oder im wesentlichen die gesamte für die Verflüssigung von Rohargon benötigte Kälte durch die Verdampfung des zweiten Teilstroms (203) zur Verfügung gestellt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß mindestens ein Teil des bei dem indirekten Wärmeaustausch im zweiten Kondensator-Verdampfer (27) verdampften zweiten Teilstroms (205) ohne weitere Druckerhöhung in das Hauptrektifiziersystem (4) eingeleitet wird.
- Verfahren nach einem der Ansprüche 1 oder 2, dadurch gekennzeichnet, daß die flüssige Produktfraktion durch einen flüssigen Sauerstoffstrom (18) aus dem Hauptrektifiziersystem (4), insbesondere aus der Niederdrucksäule (6) eines Doppelsäulensystems, gebildet wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der Druck der flüssigen Produktfraktion (20; 29) stromaufwärts des indirekten Wärmeaustauschs (2) mit dem zweiten Teilstrom (202, 203) erhöht (19; 31) wird.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß der zweite Teilstrom (202, 203) bei dem indirekten Wärmeaustausch (2) mit der flüssigen Produktfraktion (20; 29) unter einem Druck steht, der höher ist als der höchste Druck im Hauptrektifiziersystem (4).
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß mindestens 21 % der Einsatzluftmenge dem Hauptrektifiziersystem (4) in flüssiger Form entnommen werden.
- Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß ein dritter Teilstrom (301) von verdichteter und gereinigter Luft arbeitsleistend entspannt (32) und dem Hauptrektifiziersystem (4) zugeführt wird.
- Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß ein weiterer flüssiger Produktstrom in indirektem Wärmeaustausch mit verdichteter und gereinigter Luft verdampft wird.
- Vorrichtung zur Tieftemperaturzerlegung von Luft nach dem Verfahren gemäß einem der Ansprüche 1 bis 8 mit einem Hauptrektifiziersystem (4), mit einer ersten (101) und einer zweiten (202, 203) Luftleitung, die mit einer Quelle (1) für verdichtete und gereinigte Luft verbunden sind, wobei die erste Luftleitung (101) in das Hauptrektifiziersystem (4) führt (3), mit einer Flüssigleitung (20; 29), die einerseits mit einer Quelle für eine flüssige Produktfraktion und andererseits mit dem Verdampfungsraum eines ersten Kondensator-Verdampfers (2) verbunden ist, durch dessen Verflüssigungsraum die zweite Luftleitung (202, 203) führt, und mit einer Rohargonsäule (24), die (über 22, 23) mit dem Hauptrektifiziersystem (4) und mit dem Verflüssigungsraum eines zweiten Kondensator-Verdampfers (27) verbunden ist, wobei die zweite Luftleitung (202, 203) stromabwärts des ersten Kondensator-Verdampfers (2) mit dem einzigen Verdampfungsraum des zweiten Kondensator-Verdampfers (27) verbunden (204) ist, dadurch gekennzeichnet, daß der zweite Kondensator-Verdampfer (27) den einzigen Kopfkondensator (27) der Rohargonsäule (24) bildet.
- Vorrichtung nach Anspruch 9, gekennzeichnet durch eine Dampfleitung (205), die den Verdampfungsraum des zweiten Kondensator-Verdampfers (27) mit dem Hauptrektifiziersystem (4) verbindet und keine Vorrichtungen zur Druckerhöhung enthält.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4443190 | 1994-12-05 | ||
DE4443190A DE4443190A1 (de) | 1994-12-05 | 1994-12-05 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0716280A2 EP0716280A2 (de) | 1996-06-12 |
EP0716280A3 EP0716280A3 (de) | 1997-04-16 |
EP0716280B1 true EP0716280B1 (de) | 2001-05-16 |
Family
ID=6534925
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP95118951A Expired - Lifetime EP0716280B1 (de) | 1994-12-05 | 1995-12-01 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
Country Status (7)
Country | Link |
---|---|
US (1) | US5644934A (de) |
EP (1) | EP0716280B1 (de) |
JP (1) | JPH08233458A (de) |
KR (1) | KR960024196A (de) |
CN (1) | CN1125838A (de) |
DE (2) | DE4443190A1 (de) |
TW (1) | TW299244B (de) |
Cited By (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102007031759A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft |
DE102007031765A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren zur Tieftemperaturzerlegung von Luft |
DE102009034979A1 (de) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff |
EP2312248A1 (de) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Verfahren und Vorrichtung Gewinnung von Drucksauerstoff und Krypton/Xenon |
EP2458311A1 (de) | 2010-11-25 | 2012-05-30 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102010052544A1 (de) | 2010-11-25 | 2012-05-31 | Linde Ag | Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
EP2520886A1 (de) | 2011-05-05 | 2012-11-07 | Linde AG | Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
EP2568242A1 (de) | 2011-09-08 | 2013-03-13 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Stahl |
EP2600090A1 (de) | 2011-12-01 | 2013-06-05 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft |
DE102011121314A1 (de) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102013017590A1 (de) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage |
DE102012017488A1 (de) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren |
EP2784420A1 (de) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Verfahren zur Luftzerlegung und Luftzerlegungsanlage |
WO2014154339A2 (de) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Verfahren zur luftzerlegung und luftzerlegungsanlage |
EP2801777A1 (de) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Luftzerlegungsanlage mit Hauptverdichterantrieb |
EP2963367A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch |
EP2963371A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft |
EP2963369A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
EP2963370A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE19636306A1 (de) | 1996-09-06 | 1998-02-05 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft |
US6347534B1 (en) * | 1999-05-25 | 2002-02-19 | Air Liquide Process And Construction | Cryogenic distillation system for air separation |
US6276170B1 (en) | 1999-05-25 | 2001-08-21 | Air Liquide Process And Construction | Cryogenic distillation system for air separation |
US6202441B1 (en) * | 1999-05-25 | 2001-03-20 | Air Liquide Process And Construction, Inc. | Cryogenic distillation system for air separation |
US6196024B1 (en) * | 1999-05-25 | 2001-03-06 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Cryogenic distillation system for air separation |
WO2013053425A2 (de) * | 2011-09-20 | 2013-04-18 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur erzeugung zweier gereinigter luftteilströme |
CN105758114A (zh) * | 2014-12-19 | 2016-07-13 | 常熟市永安工业气体制造有限公司 | 氩气制备装置 |
JP6440232B1 (ja) * | 2018-03-20 | 2018-12-19 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | 製品窒素ガスおよび製品アルゴンの製造方法およびその製造装置 |
Family Cites Families (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4555256A (en) * | 1982-05-03 | 1985-11-26 | Linde Aktiengesellschaft | Process and device for the production of gaseous oxygen at elevated pressure |
DE3428968A1 (de) * | 1984-08-06 | 1986-02-13 | Linde Ag, 6200 Wiesbaden | Verfahren und vorrichtung zur zerlegung von rohargon |
US4715873A (en) * | 1986-04-24 | 1987-12-29 | Air Products And Chemicals, Inc. | Liquefied gases using an air recycle liquefier |
US4871382A (en) * | 1987-12-14 | 1989-10-03 | Air Products And Chemicals, Inc. | Air separation process using packed columns for oxygen and argon recovery |
DE3840506A1 (de) * | 1988-12-01 | 1990-06-07 | Linde Ag | Verfahren und vorrichtung zur luftzerlegung |
US5049173A (en) * | 1990-03-06 | 1991-09-17 | Air Products And Chemicals, Inc. | Production of ultra-high purity oxygen from cryogenic air separation plants |
US5049174A (en) * | 1990-06-18 | 1991-09-17 | Air Products And Chemicals, Inc. | Hybrid membrane - cryogenic generation of argon concurrently with nitrogen |
US5108476A (en) * | 1990-06-27 | 1992-04-28 | Union Carbide Industrial Gases Technology Corporation | Cryogenic air separation system with dual temperature feed turboexpansion |
US5159816A (en) * | 1991-05-14 | 1992-11-03 | Air Products And Chemicals, Inc. | Method of purifying argon through cryogenic adsorption |
US5315833A (en) * | 1991-10-15 | 1994-05-31 | Liquid Air Engineering Corporation | Process for the mixed production of high and low purity oxygen |
US5245831A (en) * | 1992-02-13 | 1993-09-21 | Air Products And Chemicals, Inc. | Single heat pump cycle for increased argon recovery |
US5365741A (en) * | 1993-05-13 | 1994-11-22 | Praxair Technology, Inc. | Cryogenic rectification system with liquid oxygen boiler |
DE4317916A1 (de) * | 1993-05-28 | 1994-12-01 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Argon |
GB9410696D0 (en) * | 1994-05-27 | 1994-07-13 | Boc Group Plc | Air separation |
US5440884A (en) * | 1994-07-14 | 1995-08-15 | Praxair Technology, Inc. | Cryogenic air separation system with liquid air stripping |
US5522224A (en) * | 1994-08-15 | 1996-06-04 | Praxair Technology, Inc. | Model predictive control method for an air-separation system |
US5469710A (en) * | 1994-10-26 | 1995-11-28 | Praxair Technology, Inc. | Cryogenic rectification system with enhanced argon recovery |
-
1994
- 1994-12-05 DE DE4443190A patent/DE4443190A1/de not_active Withdrawn
-
1995
- 1995-11-29 JP JP7332550A patent/JPH08233458A/ja active Pending
- 1995-12-01 DE DE59509262T patent/DE59509262D1/de not_active Expired - Fee Related
- 1995-12-01 TW TW084112821A patent/TW299244B/zh active
- 1995-12-01 EP EP95118951A patent/EP0716280B1/de not_active Expired - Lifetime
- 1995-12-04 US US08/566,701 patent/US5644934A/en not_active Expired - Fee Related
- 1995-12-05 KR KR1019950046689A patent/KR960024196A/ko not_active Application Discontinuation
- 1995-12-05 CN CN95117579A patent/CN1125838A/zh active Pending
Cited By (25)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102007031759A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft |
DE102007031765A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren zur Tieftemperaturzerlegung von Luft |
EP2015013A2 (de) | 2007-07-07 | 2009-01-14 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft |
EP2015012A2 (de) | 2007-07-07 | 2009-01-14 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft |
DE102009034979A1 (de) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff |
EP2312248A1 (de) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Verfahren und Vorrichtung Gewinnung von Drucksauerstoff und Krypton/Xenon |
EP2458311A1 (de) | 2010-11-25 | 2012-05-30 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102010052545A1 (de) | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102010052544A1 (de) | 2010-11-25 | 2012-05-31 | Linde Ag | Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
EP2466236A1 (de) | 2010-11-25 | 2012-06-20 | Linde Aktiengesellschaft | Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tiefemperaturzerlegung von Luft |
EP2520886A1 (de) | 2011-05-05 | 2012-11-07 | Linde AG | Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102011112909A1 (de) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Stahl |
EP2568242A1 (de) | 2011-09-08 | 2013-03-13 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Stahl |
EP2600090A1 (de) | 2011-12-01 | 2013-06-05 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft |
DE102011121314A1 (de) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE102012017488A1 (de) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren |
EP2784420A1 (de) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Verfahren zur Luftzerlegung und Luftzerlegungsanlage |
WO2014154339A2 (de) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Verfahren zur luftzerlegung und luftzerlegungsanlage |
EP2801777A1 (de) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Luftzerlegungsanlage mit Hauptverdichterantrieb |
DE102013017590A1 (de) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage |
EP2963367A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch |
EP2963371A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft |
EP2963369A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
EP2963370A1 (de) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
WO2016005031A1 (de) | 2014-07-05 | 2016-01-14 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft mit variablem energieverbrauch |
Also Published As
Publication number | Publication date |
---|---|
KR960024196A (ko) | 1996-07-20 |
TW299244B (de) | 1997-03-01 |
DE4443190A1 (de) | 1996-06-13 |
JPH08233458A (ja) | 1996-09-13 |
CN1125838A (zh) | 1996-07-03 |
DE59509262D1 (de) | 2001-06-21 |
EP0716280A3 (de) | 1997-04-16 |
US5644934A (en) | 1997-07-08 |
EP0716280A2 (de) | 1996-06-12 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0716280B1 (de) | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft | |
EP1308680B1 (de) | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft | |
EP2235460B1 (de) | Verfahren und vorrichtung zur tieftemperatur-luftzerlegung | |
EP0955509B1 (de) | Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff | |
EP1243882B1 (de) | Argongewinnung mit einem Drei-Säulen-System zur Luftzerlegung und einer Rohargonsäule | |
DE69214409T3 (de) | Verfahren zur Herstellung unreinen Sauerstoffs | |
DE10139727A1 (de) | Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft | |
EP1482266B1 (de) | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft | |
EP0948730B1 (de) | Verfahren und vorrichtung zur gewinnung von druckstickstoff | |
EP0669508B1 (de) | Verfahren und Vorrichtung zur Gewinnung von reinem Argon | |
DE10018200A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft | |
WO2020169257A1 (de) | Verfahren und anlage zur tieftemperaturzerlegung von luft | |
DE19609490A1 (de) | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft | |
DE60008455T2 (de) | Tieftemperaturdestillationsanlage zur Luftzerleggung | |
DE10103968A1 (de) | Drei-Säulen-System zur Tieftemperaturzerlegung von Luft | |
DE60007686T2 (de) | Tieftemperaturrektifikationsystem zur Luftzerleggung | |
DE10161584A1 (de) | Vorrichtung und Verfahren zur Erzeugung gasförmigen Sauerstoffs unter erhöhtem Druck | |
DE10232430A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft | |
DE10045128A1 (de) | Verfahren und Vorrichtung zur Erzeugung hoch reinen Stickstoffs durch Tieftemperatur-Luftzerlegung | |
DE20319823U1 (de) | Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung | |
DE19950570A1 (de) | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft | |
DE19819338A1 (de) | Verfahren und Vorrichtung zur Gewinnung von hochreinem Druckstickstoff | |
EP0828122A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft | |
DE19819263A1 (de) | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff | |
DE10009977A1 (de) | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
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: A2 Designated state(s): BE DE FR GB IT |
|
PUAL | Search report despatched |
Free format text: ORIGINAL CODE: 0009013 |
|
AK | Designated contracting states |
Kind code of ref document: A3 Designated state(s): BE DE FR GB IT |
|
17P | Request for examination filed |
Effective date: 19970612 |
|
17Q | First examination report despatched |
Effective date: 19990526 |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
RTI1 | Title (correction) |
Free format text: METHOD AND APPARATUS FOR THE LOW TEMPERATURE AIR SEPARATION |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): BE DE FR GB IT |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRE;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.SCRIBED TIME-LIMIT Effective date: 20010516 |
|
REF | Corresponds to: |
Ref document number: 59509262 Country of ref document: DE Date of ref document: 20010621 |
|
GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) |
Effective date: 20010731 |
|
ET | Fr: translation filed | ||
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20011231 |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: IF02 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed | ||
BERE | Be: lapsed |
Owner name: LINDE A.G. Effective date: 20011231 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GB Payment date: 20071128 Year of fee payment: 13 Ref country code: FR Payment date: 20071210 Year of fee payment: 13 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20071129 Year of fee payment: 13 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: CA |
|
GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 20081201 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST Effective date: 20090831 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090701 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20081201 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20081231 |