EP1139046B1 - Process and device for producing high pressure oxygen product by cryogenic air separation - Google Patents
Process and device for producing high pressure oxygen product by cryogenic air separation Download PDFInfo
- Publication number
- EP1139046B1 EP1139046B1 EP00115777A EP00115777A EP1139046B1 EP 1139046 B1 EP1139046 B1 EP 1139046B1 EP 00115777 A EP00115777 A EP 00115777A EP 00115777 A EP00115777 A EP 00115777A EP 1139046 B1 EP1139046 B1 EP 1139046B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- pressure
- column
- feed air
- air stream
- feed
- 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
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
-
- 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
- F25J3/0446—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 the heat generated by mixing two different phases
- F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
Definitions
- the invention relates to a method and a device to obtain a pressurized oxygen product Cryogenic air separation each in accordance with the preambles of claims 1 and 9.
- a method and an apparatus of the type mentioned are out EP 697576 A1 known.
- the total air is at approximately high-pressure column pressure compresses and the mixing column air then to the operating pressure of the mixing column
- the mixing column operated under a pressure lower than the operating pressure of the high pressure column of the two-pillar system that is used for nitrogen-oxygen separation.
- the rectification system of the invention can be a two-column system, for example as classic double column system, be formed, but also as a three or Multi-pillar system. It can be used in addition to the columns for nitrogen-oxygen separation other devices for extracting other air components, especially noble gases (e.g. krypton, xenon and / or argon) exhibit.
- noble gases e.g. krypton, xenon and / or argon
- the oxygen-rich fraction used as the insert for the mixing column points an oxygen concentration higher than that of air and for example 70 to 99.5 mol%, preferably 90 to 98 mol%.
- Under Mixing column is understood to be a countercurrent contact column in which a more volatile gaseous fraction of a less volatile liquid is sent to.
- the method according to the invention is particularly suitable for the extraction of gaseous impure oxygen under pressure.
- An impure oxygen is used here Mixture with an oxygen content of 99.5 mol% or less, in particular of 70 to 99.5 mol%.
- the product pressures are, for example, 2.2 to 4.9 bar, preferably at 2.5 to 4.5 bar.
- the printed product if necessary, be compressed further in gaseous state. relaxed, with the relaxation of part of the mixing column air doing work is carried out. As a result, the high pressure of this partial air flow can Cooling can be used.
- the known method is not in all Cases energetically favorable.
- the invention has for its object a method of the type mentioned and to specify a corresponding device that is particularly small Have energy consumption.
- a total air flow which comprises at least the first and the second feed air flow, is compressed to a first pressure (p 2 ), which is lower than the operating pressure (p HDS ) of the high-pressure column , and under approximately this first pressure (p 1 ) is cleaned, that the cleaned total air flow is divided into the first and the second feed air flow and that the first feed air flow is further compressed separately from the second feed air flow to a second pressure (p 1 ) which is at least equal to the operating pressure (p HDS ) of the High pressure column
- the total air flow is not compressed to the highest pressure in the system, but to a lower value.
- the air part or parts that have a relatively high Require pressure - especially the high pressure column air - are deliberately separated further compressed. This allows you to use the least amount of energy Compress the feed air.
- the least amount of equipment is required if the first pressure is about the same the operating pressure of the mixing column.
- the mixing column air second Feed air flow) into the mixing column without any further pressure-changing measures be initiated.
- the first pressure can be lower than the operating pressure (p MiS ) of the mixing column.
- the second feed air stream is further compressed separately from the first feed air stream to a third pressure (p 3 ) which is at least equal to the operating pressure (p MiS ) of the mixing column.
- the liquid-pressurized oxygen-rich fraction is preferably added before the Feed on the mixing column in indirect heat exchange with an overheated one Airflow warmed up.
- the superheated airflow is caused, for example, by part of the Feed air is formed, which is at high pressure column pressure. This is at a Intermediate temperature from the main heat exchanger, in the feed air to about Dew point is cooled, removed and without further temperature changes Measures for indirect heat exchange with the oxygen-rich liquid brought. In this way, the temperature of the liquid on the mixing column is optimally given to the conditions in countercurrent mass transfer adjusted within the mixing column.
- the third feed air stream is preferably used before the work-related relaxation post-condensed, particularly during work-related relaxation mechanical energy is used to drive the post-compression.
- This can a turbine-booster combination can be used in the expansion turbine and post-compressor are mechanically coupled via a common shaft.
- the third feed air flow can be combined with the first and second on the first Pressure compressed and cleaned. Then it either becomes immediate led to post-compression or together with the first feed air flow densified.
- the second feed air stream after it has been further compressed and before it is fed in the mixing column can be relaxed while working.
- the further compression then takes place to a second pressure that is significantly higher than the mixing column pressure.
- the invention also relates to a device according to claim 9.
- feed air 1 is brought to a first pressure p 1 of, for example, 2.7 to 3.7 bar, preferably about 3.2 bar, in a two-stage air compressor 2 with after-cooling and enters a cleaning device 3 under this pressure which is preferably formed by a pair of molecular sieve adsorbers.
- the cleaned total air 4 is divided into three partial streams 5, 6, 7.
- the first feed air stream 5 is further compressed in a first post-compressor 8 to a second pressure p 2 of, for example, 4.4 to 7.0 bar, preferably about 5.7 bar, and flows into a main heat exchanger 10 after post-cooling 9.
- the first feed air stream leaves the main heat exchanger 10 via line 11 at approximately dew point temperature and is fed via line 12 into a high pressure column 13.
- the operating pressure p HDS of the high pressure column 13 is, for example, 4.3 to 6.9 bar, preferably about 5.6 bar.
- the rectification system also has a low pressure column 14 which is operated under, for example, 1.3 to 1.7 bar, preferably about 1.5 bar.
- the second feed air stream 6 is likewise passed through the main heat exchanger 10 at approximately the first pressure p 1 (minus line losses and pressure losses in the cleaning device) and finally flows via line 15 to the mixing column.
- the feed point is located directly above the bottom of the mixing column 16.
- the third partial stream 7 is post-compressed from about the first pressure p 1 in a second post-compressor 17 to a third pressure p 3 of, for example, 3.8 to 5.6 bar, preferably about 4.7 bar, and after post-cooling 18 via line 19, the warm one End of the main heat exchanger supplied. However, it is only cooled to an intermediate temperature and drawn off from the main heat exchanger 10 again via line 50 before the cold end and expanded in a turbine 20 to perform work. The relaxed air 21 is blown into the low pressure column 14. Post-compressor 17 and turbine 20 are directly mechanically coupled.
- the rectification system is in the exemplary embodiments as a classic Linde double column apparatus with a condenser-evaporator 22 as the main condenser
- the invention can also be used in rectification systems with others Capacitor and / or column configuration can be used.
- Oxygenated liquid 23 from the sump of the high pressure column 13 is in a first supercooling counterflow 24 cooled and after throttling 25 the Low pressure column 14 supplied at an intermediate point 26.
- Gaseous nitrogen 27 from the head of the high pressure column 13 to a part 28 in the main heat exchanger 10 warmed and obtained as pressure nitrogen product 29. The rest of 30 will be in Main capacitor 22 is substantially fully condensed.
- the won here liquid nitrogen 31 is at least partially 32 as a return to the high pressure column 13 abandoned. If necessary, another part 33 can be drawn off as a liquid product become.
- An intermediate liquid (impure nitrogen) of the high pressure column 34 serves after hypothermia 24 and throttling 35 as return for the low pressure column.
- Gaseous impure nitrogen 36 from the top of the low pressure column is in the Heat exchangers 24 and 10 warmed up and finally drawn off via line 37. He can be used as a regeneration gas for the cleaning device 3 as shown become.
- Liquid oxygen 38 is drawn off from the bottom of the low-pressure column, in one Pump 39 to a pressure of, for example, 5.7 to 6.5 bar, preferably about 6.1 bar brought, warmed in a second subcooling countercurrent 40 and finally abandoned on top of the mixing column 16 (41).
- the second Supercooling counterflow 40 becomes in particular an overheated airflow 42 cooled, the upstream of the cold end of the main heat exchanger from the first Feed air flow is branched, and at an intermediate temperature that is lower than the inlet temperature of the turbine 20. This airflow is followed by its cooling via line 43 again combined with the first feed air stream 11. Via the valve 44, the amount of by the second supercooling counterflow flowing airflow set.
- Gaseous impure compressed oxygen 51 is drawn off from the top of the mixing column 16, warmed in the main heat exchanger 10 and obtained as product 52.
- the mixing column Bottom liquid 45 and an intermediate liquid 46 are removed and over the Lines 47 and 48 at a suitable location on the low-pressure column 14 fed.
- Figure 2 differs from Figure 1 only in that the third feed air flow 207 together with the second feed air flow in the first post-compressor 108 is further compressed. This results in a higher inlet pressure on the turbine 20 reached and generated more cold accordingly.
- the cleaning device is operated at a first pressure p 1 'which is higher than the operating pressure p MiS of the mixing column.
- the first pressure p 1 ' is here, for example, 2.7 to 3.7 bar, preferably about 3.2 bar.
- the second feed air stream 306 is expanded upstream of its feed into the mixing column.
- a third feed air stream that is blown into the low pressure column does not exist.
- the second feed air stream 306 is further compressed downstream of its branch from the cleaned total air in the second post-compressor 317, which is driven by the turbine 320.
- the second feed air flow 349 which is further compressed to, for example, 3.8 to 5.6 bar, preferably about 4.7 bar, is fed to the turbine 320 via line 350 and is expanded there to perform work to approximately mixing column pressure p MiS .
- the cleaning 3 is operated under a particularly low first pressure p 1 "of, for example, 2.7 to 3.7 bar, preferably about 3.2 bar.
- the turbine 420 is operated as in FIG 1 is acted upon by a third feed air stream 407, 450, which, however, is not subsequently compressed here, but is instead expanded in a work-performing manner from approximately the first pressure p 1 "to approximately low-pressure column pressure.
- the turbine-driven post-compressor 418 is used here for further compression of the second feed air flow to the second pressure p 2 , which is approximately equal to the operating pressure p MiS of the mixing column.
- the air compressor and the post-compressor are 8, 108 preferably formed together as a three-stage machine.
- the further compression of the first feed air flow becomes one in the third stage Machine carried out, the first and second stage for air compression serve upstream of the cleaning 3.
- this machine can also be four stages, in which case the first three stages before Cleaning device 3 are arranged.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
Description
Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur Gewinnung eines Drucksauerstoff-Produkts durch Tieftemperaturzerlegung von Luft jeweils gemäß den Oberbegriffen der Ansprüche 1 und 9. Ein Verfahren und eine Vorrichtung der genannten Art sind aus EP 697576 A1 bekannt. In der EP 697 576 A wird die Gesamtluft auf etwa Hochdrucksäulendruck verdichtet und die Mischsäulenluft anschließend auf den Betriebsdruck der Mischsäule Bei der Erfindung wird die Mischsäule unter einem Druck betrieben, der niedriger als der Betriebsdruck der Hochdrucksäule des Zwei-Säulen-Systems ist, das zur Stickstoff-Sauerstoff-Trennung dient.The invention relates to a method and a device to obtain a pressurized oxygen product Cryogenic air separation each in accordance with the preambles of claims 1 and 9. A method and an apparatus of the type mentioned are out EP 697576 A1 known. In EP 697 576 A, the total air is at approximately high-pressure column pressure compresses and the mixing column air then to the operating pressure of the mixing column In the invention, the mixing column operated under a pressure lower than the operating pressure of the high pressure column of the two-pillar system that is used for nitrogen-oxygen separation.
Das Rektifiziersystem der Erfindung kann als Zweisäulensystem, beispielsweise als klassisches Doppelsäulensystem, ausgebildet sein, aber auch als Drei- oder Mehrsäulensystem. Es kann zusätzlich zu den Kolonnen zur Stickstoff-Sauerstoff-Trennung weitere Vorrichtungen zur Gewinnung anderer Luftkomponenten, insbesondere von Edelgasen (beispielsweise Krypton, Xenon und/oder Argon) aufweisen.The rectification system of the invention can be a two-column system, for example as classic double column system, be formed, but also as a three or Multi-pillar system. It can be used in addition to the columns for nitrogen-oxygen separation other devices for extracting other air components, especially noble gases (e.g. krypton, xenon and / or argon) exhibit.
Die sauerstoffreiche Fraktion, die als Einsatz für die Mischsäule verwendet wird, weist eine Sauerstoffkonzentration auf, die höher als diejenige von Luft ist und beispielsweise bei 70 bis 99,5 mol%, vorzugsweise bei 90 bis 98 mol% liegt. Unter Mischsäule wird eine Gegenstromkontaktkolonne verstanden, in der eine leichterflüchtige gasförmige Fraktion einer schwererflüchtigen Flüssigkeit entgegengeschickt wird.The oxygen-rich fraction used as the insert for the mixing column points an oxygen concentration higher than that of air and for example 70 to 99.5 mol%, preferably 90 to 98 mol%. Under Mixing column is understood to be a countercurrent contact column in which a more volatile gaseous fraction of a less volatile liquid is sent to.
Das erfindungsgemäße Verfahren eignet sich insbesondere zur Gewinnung von gasförmigem unreinem Sauerstoff unter Druck. Als unreiner Sauerstoff wird hier ein Gemisch mit einem Sauerstoffgehalt von 99,5 mol% oder weniger, insbesondere von 70 bis 99,5 mol% bezeichnet. Die Produktdrücke liegen beispielsweise bei 2,2 bis 4,9 bar, vorzugsweise bei 2,5 bis 4,5 bar. Selbstverständlich kann das Druckprodukt bei Bedarf in gasförmigem Zustand weiter verdichtet werden. entspannt, wobei die Entspannung eines Teils der Mischsäulenluft arbeitsleistend durchgeführt wird. Hierdurch kann zwar der hohe Druck dieses Teilluftstroms zur Kältegewinnung eingesetzt werden. Das bekannte Verfahren ist aber nicht in allen Fällen energetisch günstig.The method according to the invention is particularly suitable for the extraction of gaseous impure oxygen under pressure. An impure oxygen is used here Mixture with an oxygen content of 99.5 mol% or less, in particular of 70 to 99.5 mol%. The product pressures are, for example, 2.2 to 4.9 bar, preferably at 2.5 to 4.5 bar. Of course, the printed product if necessary, be compressed further in gaseous state. relaxed, with the relaxation of part of the mixing column air doing work is carried out. As a result, the high pressure of this partial air flow can Cooling can be used. The known method is not in all Cases energetically favorable.
Ein ähnlicher Prozess wird in der nicht vorveröffentlichten EP 1 024 464 A1 beschrieben. Hier werden erster und zweiter Einsatzluftstrom getrennt voneinander gereinigt.A similar process is used in the unpublished EP 1 024 464 A1. Here are the first and second The feed air stream is cleaned separately.
Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die einen besonders geringen Energieverbrauch aufweisen.The invention has for its object a method of the type mentioned and to specify a corresponding device that is particularly small Have energy consumption.
Diese Aufgabe wird dadurch gelöst, daß ein Gesamtluftstrom, der mindestens den ersten und den zweiten Einsatzluftstrom umfaßt, auf einen ersten Druck (p2) verdichtet wird, der niedriger als der Betriebsdruck (pHDS) der Hochdrucksäule ist, und unter etwa diesem ersten Druck (p1) gereinigt wird, daß der gereinigte Gesamtluftstrom in den ersten und den zweiten Einsatzluftstrom aufgeteilt wird und daß der erste Einsatzluftstrom getrennt vom zweiten Einsatzluftstrom auf einen zweiten Druck (p1) weiterverdichtet wird, der mindestens gleich dem Betriebsdruck (pHDS) der Hochdrucksäule istThis object is achieved in that a total air flow, which comprises at least the first and the second feed air flow, is compressed to a first pressure (p 2 ), which is lower than the operating pressure (p HDS ) of the high-pressure column , and under approximately this first pressure (p 1 ) is cleaned, that the cleaned total air flow is divided into the first and the second feed air flow and that the first feed air flow is further compressed separately from the second feed air flow to a second pressure (p 1 ) which is at least equal to the operating pressure (p HDS ) of the High pressure column
Der Gesamtluftstrom wird also nicht auf den höchsten Druck im System verdichtet, sondern auf einen niedrigeren Wert. Der oder die Luftteile, die einen relativ hohen Druck benötigen - insbesondere die Hochdrucksäulenluft - , werden gezielt separat weiterverdichtet. Hierdurch kann man mit dem geringstmöglichen Energieeinsatz beim Verdichten der Einsatzluft auskommen.The total air flow is not compressed to the highest pressure in the system, but to a lower value. The air part or parts that have a relatively high Require pressure - especially the high pressure column air - are deliberately separated further compressed. This allows you to use the least amount of energy Compress the feed air.
Den geringsten apparativen Aufwand erzielt man, wenn der erste Druck etwa gleich dem Betriebsdruck der Mischsäule ist. Hierbei kann die Mischsäulenluft (zweiter Einsatzluftstrom) ohne weitere druckverändernde Maßnahmen in die Mischsäule eingeleitet werden.The least amount of equipment is required if the first pressure is about the same the operating pressure of the mixing column. The mixing column air (second Feed air flow) into the mixing column without any further pressure-changing measures be initiated.
Alternativ dazu kann der erste Druck niedriger als der Betriebsdruck (pMiS) der Mischsäule sein. In diesem Fall wird der zweite Einsatzluftstrom getrennt vom ersten Einsatzluftstrom auf einen dritten Druck (p3) weiterverdichtet, der mindestens gleich dem Betriebsdruck (pMiS) der Mischsäule ist. Alternatively, the first pressure can be lower than the operating pressure (p MiS ) of the mixing column. In this case, the second feed air stream is further compressed separately from the first feed air stream to a third pressure (p 3 ) which is at least equal to the operating pressure (p MiS ) of the mixing column.
Vorzugsweise wird die flüssig auf Druck gebrachte sauerstoffreiche Fraktion vor dem Aufgeben auf die Mischsäule in indirektem Wärmeaustausch mit einem überhitzten Luftstrom angewärmt. Der überhitzte Luftstrom wird beispielsweise durch einen Teil der Einsatzluft gebildet, der sich auf Hochdrucksäulendruck befindet. Dieser wird bei einer Zwischentemperatur aus dem Hauptwärmetauscher, in dem Einsatzluft auf etwa Taupunkt abgekühlt wird, entnommen und ohne weitere temperaturverändemde Maßnahmen zu dem indirekten Wärmeaustausch mit der sauerstoffreichen Flüssigkeit gebracht. Auf diese Weise wird die Temperatur der Flüssigkeit, die auf die Mischsäule aufgegeben wird, optimal an die Verhältnisse beim Gegenstrom-Stoffaustausch innerhalb der Mischsäule angepaßt.The liquid-pressurized oxygen-rich fraction is preferably added before the Feed on the mixing column in indirect heat exchange with an overheated one Airflow warmed up. The superheated airflow is caused, for example, by part of the Feed air is formed, which is at high pressure column pressure. This is at a Intermediate temperature from the main heat exchanger, in the feed air to about Dew point is cooled, removed and without further temperature changes Measures for indirect heat exchange with the oxygen-rich liquid brought. In this way, the temperature of the liquid on the mixing column is optimally given to the conditions in countercurrent mass transfer adjusted within the mixing column.
Kälte wird bei dem Verfahren auf günstige Weise erzeugt, indem ein dritter Einsatzluftstrom arbeitsleistend entspannt und in die Niederdrucksäule eingeleitet wird. Hierdurch kann das "natürliche" Druckgefälle zwischen dem ersten Druck oder einem anderen Verfahrensdruck ausgenutzt werden, um Isolationsverluste auszugleichen und gegebenenfalls einen Teil der Produkte zu verflüssigen.Cold is generated in the process in a favorable manner by a third The air flow is relieved from work and introduced into the low pressure column. As a result, the "natural" pressure drop between the first pressure or a other process pressure can be used to compensate for insulation losses and if necessary to liquefy some of the products.
Vorzugsweise wird der dritte Einsatzluftstrom vor der arbeitsleistenden Entspannung nachverdichtet, wobei insbesondere bei der arbeitsleistenden Entspannung erzeugte mechanische Energie zum Antrieb der Nachverdichtung verwendet wird. Hierbei kann eine Turbinen-Booster-Kombination eingesetzt werden, bei der Entspannungsturbine und Nachverdichter über eine gemeinsame Welle mechanisch gekoppelt sind.The third feed air stream is preferably used before the work-related relaxation post-condensed, particularly during work-related relaxation mechanical energy is used to drive the post-compression. This can a turbine-booster combination can be used in the expansion turbine and post-compressor are mechanically coupled via a common shaft.
Der dritte Einsatzluftstrom kann gemeinsam mit dem ersten und zweiten auf den ersten Druck verdichtetet und gereinigt werden. Anschließend wird er entweder unmittelbar zur Nachverdichtung geführt oder noch gemeinsam mit dem ersten Einsatzluftstrom nachverdichtet.The third feed air flow can be combined with the first and second on the first Pressure compressed and cleaned. Then it either becomes immediate led to post-compression or together with the first feed air flow densified.
Alternativ zur Einblasung des dritten Einsatzluftstroms in die Niederdrucksäule kann der zweite Einsatzluftstrom nach seiner Weiterverdichtung und vor der Einspeisung in die Mischsäule arbeitsleistend entspannt werden. Die Weiterverdichtung erfolgt dann auf einen zweiten Druck, der deutlich höher als der Mischsäulendruck ist.As an alternative to blowing the third feed air stream into the low pressure column the second feed air stream after it has been further compressed and before it is fed in the mixing column can be relaxed while working. The further compression then takes place to a second pressure that is significantly higher than the mixing column pressure.
Die Erfindung betrifft außerdem eine Vorrichtung gemäß Patentanspruch 9. The invention also relates to a device according to claim 9.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:
- Figur 1
- ein Verfahren und eine Vorrichtung mit arbeitsleistender Entspannung eines Teils der auf den ersten Druck verdichteten Luft,
Figur 2- einen abgewandelten Prozeß mit arbeitsleistender Entspannung eines Teils der auf den zweiten Druck verdichteten Luft,
- Figur 3
- ein Verfahren mit arbeitsleistender Entspannung der Mischsäulenluft und
- Figur 4
- eine andere Variante von Figur 1 ohne Nachverdichtung der Turbinenluft.
- Figure 1
- a method and a device with work-relieving relaxation of a portion of the air compressed to the first pressure,
- Figure 2
- a modified process with relaxation of part of the air compressed to the second pressure,
- Figure 3
- a process with relaxation of the mixing column air and
- Figure 4
- another variant of Figure 1 without recompression of the turbine air.
Bei dem in Figur 1 dargestellten Prozeß wird Einsatzluft 1 in einem zweistufigen
Luftverdichter 2 mit Nachkühlung auf einen ersten Druck p1 von beispielsweise 2,7 bis
3,7 bar, vorzugsweise etwa 3,2 bar gebracht und tritt unter diesem Druck in eine
Reinigungseinrichtung 3 ein, die vorzugsweise durch ein Paar von
Molekularsiebadsorbern gebildet wird. Die gereinigte Gesamtluft 4 wird in drei
Teilströme 5, 6, 7 aufgeteilt.In the process shown in FIG. 1, feed air 1 is brought to a first pressure p 1 of, for example, 2.7 to 3.7 bar, preferably about 3.2 bar, in a two-
Der erste Einsatzluftstrom 5 wird in einem ersten Nachverdichter 8 auf einen zweiten
Druck p2 von beispielsweise 4,4 bis 7,0 bar, vorzugsweise etwa 5,7 bar
weiterverdichtet und strömt nach Nachkühlung 9 in einen Hauptwärmetauscher 10 ein.
Der erste Einsatzluftstrom verläßt den Hauptwärmetauscher 10 über Leitung 11 bei
etwa Taupunktstemperatur und wird über Leitung 12 in eine Hochdrucksäule 13
eingespeist. Der Betriebsdruck pHDS der Hochdrucksäule 13 beträgt beispielsweise 4,3
bis 6,9 bar, vorzugsweise etwa 5,6 bar. Das Rektifiziersystem weist außerdem eine
Niederdrucksäule 14 auf, die unter beispielsweise 1,3 bis 1,7 bar, vorzugsweise etwa
1,5 bar betrieben wird.The first feed air stream 5 is further compressed in a first post-compressor 8 to a second pressure p 2 of, for example, 4.4 to 7.0 bar, preferably about 5.7 bar, and flows into a
Der zweite Einsatzluftstrom 6 wird unter etwa dem ersten Druck p1 (abzüglich
Leitungsverlusten und Druckverlusten in der Reinigungseinrichtung) ebenfalls durch
den Hauptwärmetauscher 10 geleitet und strömt schließlich über Leitung 15 der
Mischsäule zu. Die Einspeisestelle liegt unmittelbar über dem Sumpf der Mischsäule
16. The second
Der dritte Teilstrom 7 wird von etwa dem ersten Druck p1 in einem zweiten
Nachverdichter 17 auf einen dritten Druck p3 von beispielsweise 3,8 bis 5,6 bar,
vorzugsweise etwa 4,7 bar nachverdichtet und nach Nachkühlung 18 über Leitung 19
dem warmen Ende des Hauptwärmetauschers zugeleitet. Er wird jedoch lediglich auf
eine Zwischentemperatur abgekühlt und bereits vor dem kalten Ende über Leitung 50
wieder aus dem Hauptwärmetauscher 10 abgezogen und in einer Turbine 20
arbeitsleistend entspannt. Die entspannte Luft 21 wird in die Niederdrucksäule 14
eingeblasen. Nachverdichter 17 und Turbine 20 sind unmittelbar mechanisch
gekoppelt.The third
Das Rektifiziersystem ist in den Ausführungsbeispielen als klassischer Linde-Doppelsäulen-Apparat
mit einem Kondensator-Verdampfer 22 als Hauptkondensator
ausgeführt Die Erfindung kann jedoch auch bei Rektifiziersystemen mit anderer
Kondensator- und/oder Säulenkonfiguration eingesetzt werden.The rectification system is in the exemplary embodiments as a classic Linde double column apparatus
with a condenser-
Sauerstoffangereicherte Flüssigkeit 23 aus dem Sumpf der Hochdrucksäule 13 wird in
einem ersten Unterkühlungs-Gegenströmer 24 abgekühlt und nach Drosselung 25 der
Niederdrucksäule 14 an einer Zwischenstelle 26 zugeführt. Gasförmiger Stickstoff 27
vom Kopf der Hochdrucksäule 13 kann zu einem Teil 28 im Hauptwärmetauscher 10
angewärmt und als Druckstickstoffprodukt 29 gewonnen werden. Der Rest 30 wird im
Hauptkondensator 22 im wesentlichen vollständig kondensiert. Der hierbei gewonnene
flüssige Stickstoff 31 wird mindestens zum Teil 32 als Rücklauf auf die Hochdrucksäule
13 aufgegeben. Bei Bedarf kann ein anderer Teil 33 als Flüssigprodukt abgezogen
werden. Eine Zwischenflüssigkeit (unreiner Stickstoff) der Hochdrucksäule 34 dient
nach Unterkühlung 24 und Drosselung 35 als Rücklauf für die Niederdrucksäule.
Gasförmiger Unreinstickstoff 36 vom Kopf der Niederdrucksäule wird in den
Wärmetauschem 24 und 10 angewärmt und schließlich über Leitung 37 abgezogen. Er
kann wie dargestellt als Regeneriergas für die Reinigungseinrichtung 3 eingesetzt
werden.Oxygenated liquid 23 from the sump of the
Aus dem Sumpf der Niederdrucksäule wird flüssiger Sauerstoff 38 abgezogen, in einer
Pumpe 39 auf einen Druck von beispielsweise 5,7 bis 6,5 bar, vorzugsweise etwa
6,1 bar gebracht, in einem zweiten Unterkühlungs-Gegenströmer 40 angewärmt und
schließlich auf dem Kopf der Mischsäule 16 aufgegeben (41). Im zweiten
Unterkühlungs-Gegenströmer 40 wird insbesondere ein überhitzter Luftstrom 42
abgekühlt, der stromaufwärts des kalten Endes des Hauptwärmetauschers vom ersten
Einsatzluftstrom abgezweigt wird, und zwar bei einer Zwischentemperatur, die
niedriger als die Eintrittstemperatur der Turbine 20 ist. Dieser Luftstrom wird nach
seiner Abkühlung über Leitung 43 wieder mit dem ersten Einsatzluftstrom 11 vereinigt.
Über das Ventil 44 wird die Menge des durch den zweiten Unterkühlungs-Gegenströmer
fließenden Luftstroms eingestellt.Liquid oxygen 38 is drawn off from the bottom of the low-pressure column, in one
Vom Kopf der Mischsäule 16 wird gasförmiger unreiner Drucksauerstoff 51 abgezogen,
im Hauptwärmetauscher 10 angewärmt und als Produkt 52 gewonnen. Der Mischsäule
werden Sumpfflüssigkeit 45 und eine Zwischenflüssigkeit 46 entnommen und über die
Leitungen 47 beziehungsweise 48 an geeigneter Stelle der Niederdrucksäule 14
zugeführt.Gaseous impure compressed
Figur 2 unterscheidet sich lediglich dadurch von Figur 1, daß der dritte Einsatzluftstrom
207 gemeinsam mit dem zweiten Einsatzluftstrom im ersten Nachverdichter 108
weiterverdichtet wird. Dadurch wird ein höherer Eintrittsdruck an der Turbine 20
erreicht und entsprechend mehr Kälte erzeugt.Figure 2 differs from Figure 1 only in that the third
In der Variante von Figur 3 wird die Reinigungseinrichtung unter einem ersten Druck
p1' betrieben, der höher als der Betriebsdruck pMiS der Mischsäule ist. Der erste Druck
p1' beträgt hier beispielsweise 2,7 bis 3,7 bar, vorzugsweise etwa 3,2 bar. Hier wird der
zweite Einsatzluftstrom 306 stromaufwärts seiner Einspeisung in die Mischsäule
entspannt. Ein dritter Einsatzluftstrom, der in die Niederdrucksäule eingeblasen wird,
existiert nicht. Der zweite Einsatzluftstrom 306 wird stromabwärts seiner Abzweigung
von der gereinigten Gesamtluft in dem zweiten Nachverdichter 317 weiterverdichtet,
der von der Turbine 320 angetrieben wird. Der auf beispielsweise 3,8 bis 5,6 bar,
vorzugsweise etwa 4,7 bar weiterverdichtete zweite Einsatzluftstrom 349 wird über
Leitung 350 der Turbine 320 zugeführt und dort arbeitsleistend auf etwa
Mischsäulendruck pMiS entspannt.In the variant of FIG. 3, the cleaning device is operated at a first pressure p 1 'which is higher than the operating pressure p MiS of the mixing column. The first pressure p 1 'is here, for example, 2.7 to 3.7 bar, preferably about 3.2 bar. Here, the second
Ähnlich wie in Figur 3 wird in dem Verfahren von Figur 4 die Reinigung 3 unter einem
besonders niedrigen ersten Druck p1" von beispielsweise 2,7 bis 3,7 bar, vorzugsweise
etwa 3,2 bar betrieben. Die Turbine 420 wird wie in Figur 1 mit einem dritten
Einsatzluftstrom 407, 450 beaufschlagt, der allerdings hier nicht nachverdichtet wird,
sondern unmittelbar von etwa dem ersten Druck p1" aus auf etwa
Niederdrucksäulendruck arbeitsleistend entspannt wird. Der von der Turbine
angetriebene Nachverdichter 418 wird hier zur Weiterverdichtung des zweiten
Einsatzluftstroms auf den zweiten Druck p2 eingesetzt, der etwa gleich dem
Betriebsdruck pMiS der Mischsäule ist.4, the cleaning 3 is operated under a particularly low first pressure p 1 "of, for example, 2.7 to 3.7 bar, preferably about 3.2 bar. The
Bei allen Ausführungsbeispielen sind der Luftverdichter und der Nachverdichter 8, 108 vorzugsweise gemeinsam als dreistufige Maschine ausgebildet. Anders ausgedrückt wird die Weiterverdichtung des ersten Einsatzluftstroms in der dritten Stufe einer Maschine durchgeführt, deren erste und zweite Stufe zur Luftverdichtung stromaufwärts der Reinigung 3 dienen. Altemativ dazu kann diese Maschine auch vierstufig ausgebildet sein, wobei in diesem Fall die ersten drei Stufen vor der Reinigungseinrichtung 3 angeordnet sind.In all of the exemplary embodiments, the air compressor and the post-compressor are 8, 108 preferably formed together as a three-stage machine. Expressed differently the further compression of the first feed air flow becomes one in the third stage Machine carried out, the first and second stage for air compression serve upstream of the cleaning 3. Alternatively, this machine can also be four stages, in which case the first three stages before Cleaning device 3 are arranged.
Claims (9)
- Process for obtaining a pressurized oxygen product by low-temperature fractionation of air in a rectification system which includes a high-pressure column (13) and a low-pressure column (14), in whicha first feed air stream (12) is introduced into the high-pressure column (13),an oxygen-rich fraction (38) from the low-pressure column (14) is pressurized (39) in liquid form and is added (41) to a mixing column (16),a second feed air stream (6, 15, 306, 406) is introduced into the lower region of the mixing column (16) and is brought into countercurrent contact with the oxygen-rich fraction (41),the mixing column (16) being operated at a pressure (pMiS) which is lower than the operating pressure (pHDS) of the high-pressure column (13), and in whichgaseous impure oxygen (51) is removed as top product from the upper region of the mixing column (16) and obtained as pressurized oxygen product (52),a total air stream (1), which contains the first and second feed air streams, is compressed (2) to a first pressure (p1) which is lower than the operating pressure (pHDS) of the high-pressure column (13) and is purified (3) at approximately this first pressure (p1), in thatthe purified total air stream (4) is divided into the first feed air stream (5) and the second feed air stream (6, 306, 406), and in thatthe first feed air stream (5) is compressed further (8, 108), separately from the second feed air stream, to a second pressure (p2) which is at least equal to the operating pressure (pHDS) of the high-pressure column (13).
- Process according to Claim 1, characterized in that the first pressure (p1) is approximately equal to the operating pressure (pMiS) of the mixing column (16).
- Process according to Claim 1, characterized in that the first pressure is lower than the operating pressure (pMiS) of the mixing column (16), and in that the second feed air stream (306, 406) is compressed further (317, 417), separately from the first feed air stream, to a third pressure (p3) which is at least equal to the operating pressure (pMiS) of the mixing column (16).
- Process according to one of Claims 1 to 3, characterized in that the oxygen-rich fraction which has been pressurized in liquid form, before it is added (41) to the mixing column (16), is heated in indirect heat exchange (40) with a superheated air stream (42).
- Process according to one of Claims 1 to 4, characterized in that a third feed air stream (7, 50, 207, 407, 450) is expanded (20, 420) in a work-performing manner and is introduced (21) into the low-pressure column (14).
- Process according to Claim 5, characterized in that the third feed air stream (7) is recompressed (17) prior to the work-performing expansion (20), with mechanical energy which is generated in particular during the work-performing expansion (20) being used for the recompression (17).
- Process according to one of Claims 5 to 6, characterized in that the third feed air stream is formed by a part of the total air stream (4) downstream of the purification (3) and is fed (7, 207) directly or after further compression (108) together with the first feed air stream to the recompression (17).
- Process according to one of Claims 1 to 4, characterized in that the second feed air stream (306, 349, 350) is expanded (320) in a work-performing manner before being introduced into the mixing column.
- Apparatus for obtaining a pressurized oxygen product by low-temperature fractionation of air, having a rectification system, which includes a high-pressure column (13) and a low-pressure column (14), and havinga first feed air line (5, 11, 12), which leads into the high-pressure column (13),a liquid line (38, 41) for removing an oxygen-rich fraction from the low-pressure column (14), which includes means (39) for increasing pressure and leads to a mixing column (16),a second feed air line (6, 15) which leads into the lower region of the mixing column (16), and havingan oxygen product line, which is connected to the upper region of the mixing column (16),a total air line, which leads through an air compressor (2) and a purification device (3) and downstream is connected to the first and second feed air lines, characterized bya recompressor (8, 108) which is arranged in the first feed air line (5, 11, 12).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10015602 | 2000-03-29 | ||
DE10015602A DE10015602A1 (en) | 2000-03-29 | 2000-03-29 | Method and device for obtaining a printed product by low-temperature separation of air |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1139046A1 EP1139046A1 (en) | 2001-10-04 |
EP1139046B1 true EP1139046B1 (en) | 2004-04-21 |
Family
ID=7636828
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP00115777A Expired - Lifetime EP1139046B1 (en) | 2000-03-29 | 2000-07-21 | Process and device for producing high pressure oxygen product by cryogenic air separation |
Country Status (7)
Country | Link |
---|---|
US (1) | US20010052244A1 (en) |
EP (1) | EP1139046B1 (en) |
KR (1) | KR20010093765A (en) |
CN (1) | CN1179181C (en) |
AT (1) | ATE265032T1 (en) |
DE (2) | DE10015602A1 (en) |
ES (1) | ES2219230T3 (en) |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011116981A2 (en) | 2010-03-26 | 2011-09-29 | Linde Aktiengesellschaft | Device for the cryogenic separation of air |
WO2011116871A2 (en) | 2010-03-26 | 2011-09-29 | Linde Aktiengesellschaft | Device for the cryogenic separation of air |
EP2503269A1 (en) | 2011-03-25 | 2012-09-26 | Linde Aktiengesellschaft | Device for cryogenic decomposition of air |
WO2014067662A2 (en) | 2012-11-02 | 2014-05-08 | Linde Aktiengesellschaft | Process for the low-temperature separation of air in an air separation plant and air separation plant |
DE102013002094A1 (en) | 2013-02-05 | 2014-08-07 | Linde Aktiengesellschaft | Method for producing liquid and gaseous oxygen by low temperature separation of air in air separation system in industrial application, involves feeding feed air flow to portion in mixed column and to another portion in separating column |
DE102015015684A1 (en) | 2015-12-03 | 2016-07-21 | Linde Aktiengesellschaft | Process for the cryogenic separation of air and air separation plant |
EP3179187A1 (en) | 2015-12-07 | 2017-06-14 | Linde Aktiengesellschaft | Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus |
EP3248962A1 (en) | 2016-05-24 | 2017-11-29 | Linde Aktiengesellschaft | Process and combination of systems for the production of urea |
EP3248670A1 (en) | 2016-05-24 | 2017-11-29 | Linde Aktiengesellschaft | Process and combination of systems for producing nitrogen-containing synthetic products |
RU2641766C2 (en) * | 2012-11-02 | 2018-01-22 | Линде Акциенгезелльшафт | Method of low-temperature separation of air in plant for air separation and plant for air separation |
Families Citing this family (25)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7437890B2 (en) * | 2006-01-12 | 2008-10-21 | Praxair Technology, Inc. | Cryogenic air separation system with multi-pressure air liquefaction |
DE102007031759A1 (en) | 2007-07-07 | 2009-01-08 | Linde Ag | Method and apparatus for producing gaseous pressure product by cryogenic separation of air |
DE102007031765A1 (en) | 2007-07-07 | 2009-01-08 | Linde Ag | Process for the cryogenic separation of air |
DE102009034979A1 (en) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Method for producing pressurized oxygen by evaporating liquid oxygen using a copper and nickel heat exchanger block |
EP2312248A1 (en) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Method and device for obtaining pressurised oxygen and krypton/xenon |
DE102011114090A1 (en) * | 2010-11-09 | 2012-05-10 | Linde Aktiengesellschaft | Method for cryogenic separation of air in distillation column-system for nitrogen-oxygen separation, involves withdrawing liquid from high-pressure column in flowing manner and discharging liquid into low-pressure column |
DE102010052544A1 (en) | 2010-11-25 | 2012-05-31 | Linde Ag | Process for obtaining a gaseous product by cryogenic separation of air |
DE102010052545A1 (en) | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
DE102011015430A1 (en) | 2011-03-29 | 2012-10-04 | Linde Aktiengesellschaft | Method and apparatus for producing flat gas |
DE102011015429A1 (en) | 2011-03-29 | 2012-10-04 | Linde Ag | Method involves for operating rebox burner, involves removing gaseous oxygen stream from upper region of mixing column and leading out oxygen product used for production of gas mixture |
EP2520886A1 (en) | 2011-05-05 | 2012-11-07 | Linde AG | Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air |
DE102011112909A1 (en) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Process and apparatus for recovering steel |
EP2600090B1 (en) | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Method and device for generating pressurised oxygen by cryogenic decomposition of air |
DE102011121314A1 (en) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
DE102012017484A1 (en) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Process and plant for the production of liquid and gaseous oxygen products by cryogenic separation of air |
DE102012017488A1 (en) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements |
EP2784420A1 (en) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
WO2014154339A2 (en) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
EP2801777A1 (en) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Air separation plant with main compressor drive |
DE102013017590A1 (en) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer |
EP2963371B1 (en) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for creating a pressurised gas product by the cryogenic decomposition of air |
EP2963367A1 (en) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Method and device for cryogenic air separation with variable power consumption |
EP2963370B1 (en) | 2014-07-05 | 2018-06-13 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
EP2963369B1 (en) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
CN114413571A (en) * | 2022-01-24 | 2022-04-29 | 四川空分集团工程有限公司 | Low energy consumption low pressure oxygen air separation plant |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5454227A (en) * | 1994-08-17 | 1995-10-03 | The Boc Group, Inc. | Air separation method and apparatus |
US5551258A (en) * | 1994-12-15 | 1996-09-03 | The Boc Group Plc | Air separation |
DE19815885A1 (en) * | 1998-04-08 | 1999-10-14 | Linde Ag | Air separation method producing gas, or gas and liquid e.g. for steel plant |
-
2000
- 2000-03-29 DE DE10015602A patent/DE10015602A1/en not_active Withdrawn
- 2000-07-21 EP EP00115777A patent/EP1139046B1/en not_active Expired - Lifetime
- 2000-07-21 ES ES00115777T patent/ES2219230T3/en not_active Expired - Lifetime
- 2000-07-21 DE DE50006148T patent/DE50006148D1/en not_active Expired - Fee Related
- 2000-07-21 AT AT00115777T patent/ATE265032T1/en not_active IP Right Cessation
-
2001
- 2001-03-28 CN CNB01109513XA patent/CN1179181C/en not_active Expired - Fee Related
- 2001-03-29 KR KR1020010016494A patent/KR20010093765A/en active IP Right Grant
- 2001-03-29 US US09/819,951 patent/US20010052244A1/en not_active Abandoned
Cited By (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011116981A2 (en) | 2010-03-26 | 2011-09-29 | Linde Aktiengesellschaft | Device for the cryogenic separation of air |
WO2011116871A2 (en) | 2010-03-26 | 2011-09-29 | Linde Aktiengesellschaft | Device for the cryogenic separation of air |
DE102010012920A1 (en) | 2010-03-26 | 2011-09-29 | Linde Aktiengesellschaft | Apparatus for the cryogenic separation of air |
EP2503269A1 (en) | 2011-03-25 | 2012-09-26 | Linde Aktiengesellschaft | Device for cryogenic decomposition of air |
DE102011015233A1 (en) | 2011-03-25 | 2012-09-27 | Linde Ag | Apparatus for the cryogenic separation of air |
WO2014067662A3 (en) * | 2012-11-02 | 2015-04-16 | Linde Aktiengesellschaft | Process for the low-temperature separation of air in an air separation plant and air separation plant |
DE102012021694A1 (en) | 2012-11-02 | 2014-05-08 | Linde Aktiengesellschaft | Process for the cryogenic separation of air in an air separation plant and air separation plant |
WO2014067662A2 (en) | 2012-11-02 | 2014-05-08 | Linde Aktiengesellschaft | Process for the low-temperature separation of air in an air separation plant and air separation plant |
RU2641766C2 (en) * | 2012-11-02 | 2018-01-22 | Линде Акциенгезелльшафт | Method of low-temperature separation of air in plant for air separation and plant for air separation |
DE102013002094A1 (en) | 2013-02-05 | 2014-08-07 | Linde Aktiengesellschaft | Method for producing liquid and gaseous oxygen by low temperature separation of air in air separation system in industrial application, involves feeding feed air flow to portion in mixed column and to another portion in separating column |
DE102015015684A1 (en) | 2015-12-03 | 2016-07-21 | Linde Aktiengesellschaft | Process for the cryogenic separation of air and air separation plant |
EP3179187A1 (en) | 2015-12-07 | 2017-06-14 | Linde Aktiengesellschaft | Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus |
EP3179186A1 (en) | 2015-12-07 | 2017-06-14 | Linde Aktiengesellschaft | Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus |
EP3248962A1 (en) | 2016-05-24 | 2017-11-29 | Linde Aktiengesellschaft | Process and combination of systems for the production of urea |
EP3248670A1 (en) | 2016-05-24 | 2017-11-29 | Linde Aktiengesellschaft | Process and combination of systems for producing nitrogen-containing synthetic products |
WO2017202629A1 (en) | 2016-05-24 | 2017-11-30 | Linde Aktiengesellschaft | Method and system combination for the preparation of urea |
Also Published As
Publication number | Publication date |
---|---|
KR20010093765A (en) | 2001-10-29 |
CN1320798A (en) | 2001-11-07 |
EP1139046A1 (en) | 2001-10-04 |
ATE265032T1 (en) | 2004-05-15 |
DE50006148D1 (en) | 2004-05-27 |
ES2219230T3 (en) | 2004-12-01 |
US20010052244A1 (en) | 2001-12-20 |
CN1179181C (en) | 2004-12-08 |
DE10015602A1 (en) | 2001-10-04 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP1139046B1 (en) | Process and device for producing high pressure oxygen product by cryogenic air separation | |
EP2015012A2 (en) | Process for the cryogenic separation of air | |
WO2007104449A1 (en) | Method and apparatus for fractionating air at low temperatures | |
EP2015013A2 (en) | Process and device for producing a gaseous pressurised product by cryogenic separation of air | |
EP1031804B1 (en) | Air separation process with nitrogen recycling | |
EP2236964B1 (en) | Method and device for low-temperature air separation | |
EP1074805B1 (en) | Process for producing oxygen under pressure and device therefor | |
EP2963370B1 (en) | Method and device for the cryogenic decomposition of air | |
EP1357342A1 (en) | Cryogenic triple column air separation system with argon recovery | |
DE102009048456A1 (en) | Method and apparatus for the cryogenic separation of air | |
DE10238282A1 (en) | Process for the low temperature decomposition of air comprises feeding a first process air stream into a high pressure column, producing a first oxygen-enriched fraction in the high pressure column, and further processing | |
EP3290843A2 (en) | Method and device for extracting pressurised nitrogen and pressurised nitrogen by cryogenic decomposition of air | |
DE19951521A1 (en) | Recovering pressurized product by low temperature decomposition of air in rectification system comprises cold compressing heat carrier stream before introducing into mixing column | |
EP0768503B1 (en) | Triple column air separation process | |
EP2963369B1 (en) | Method and device for the cryogenic decomposition of air | |
EP2053331A1 (en) | Method and device for low-temperature air separation | |
EP2551619A1 (en) | Method and device for extracting pressurised oxygen and pressurised nitrogen by cryogenic decomposition of air | |
EP3394536A1 (en) | Method and device for obtaining pure nitrogen and pure oxygen by low-temperature separation of air | |
DE102007042462A1 (en) | Method and apparatus for the cryogenic separation of air | |
DE19933558C5 (en) | Three-column process and apparatus for the cryogenic separation of air | |
WO2011110301A2 (en) | Method and device for cryogenic separation of air | |
EP1199532B1 (en) | Three-column system for the cryogenic separation of air | |
EP2963371B1 (en) | Method and device for creating a pressurised gas product by the cryogenic decomposition of air | |
EP3343159A1 (en) | Method and device for creating gaseous oxygen and gaseous pressurised nitrogen | |
DE10045121A1 (en) | Method and device for obtaining a gaseous product by low-temperature separation of air |
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;SI |
|
17P | Request for examination filed |
Effective date: 20020308 |
|
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 |
|
GRAP | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOSNIGR1 |
|
RTI1 | Title (correction) |
Free format text: PROCESS AND DEVICE FOR PRODUCING HIGH PRESSURE OXYGEN PRODUCT BY CRYOGENIC AIR SEPARATION |
|
GRAS | Grant fee paid |
Free format text: ORIGINAL CODE: EPIDOSNIGR3 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: CY Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040421 Ref country code: IE Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040421 |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: FG4D Free format text: NOT ENGLISH |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: EP |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FG4D Free format text: GERMAN |
|
REF | Corresponds to: |
Ref document number: 50006148 Country of ref document: DE Date of ref document: 20040527 Kind code of ref document: P |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: AT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040721 Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040721 Ref country code: DK Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040721 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: CH Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040731 Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040731 Ref country code: MC Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040731 Ref country code: LI Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040731 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: TRGR |
|
GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) |
Effective date: 20040723 |
|
REG | Reference to a national code |
Ref country code: GR Ref legal event code: EP Ref document number: 20040402504 Country of ref document: GR |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2219230 Country of ref document: ES Kind code of ref document: T3 Ref country code: IE Ref legal event code: FD4D |
|
ET | Fr: translation filed | ||
BERE | Be: lapsed |
Owner name: *LINDE A.G. Effective date: 20040731 |
|
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 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: PL |
|
26N | No opposition filed |
Effective date: 20050124 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20070719 Year of fee payment: 8 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: ES Payment date: 20070824 Year of fee payment: 8 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: FI Payment date: 20070712 Year of fee payment: 8 |
|
BERE | Be: lapsed |
Owner name: *LINDE A.G. Effective date: 20040731 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: PT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20040921 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GB Payment date: 20070718 Year of fee payment: 8 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: IT Payment date: 20070730 Year of fee payment: 8 Ref country code: NL Payment date: 20070703 Year of fee payment: 8 Ref country code: SE Payment date: 20070704 Year of fee payment: 8 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: FR Payment date: 20070710 Year of fee payment: 8 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GR Payment date: 20070618 Year of fee payment: 8 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: CA |
|
EUG | Se: european patent has lapsed | ||
GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 20080721 |
|
NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee |
Effective date: 20090201 |
|
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: 20090203 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST Effective date: 20090331 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090201 Ref country code: FI Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080721 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090204 Ref country code: GB Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080721 |
|
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: 20080731 Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080721 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20080722 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: ES Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080722 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080722 |