EP1139046B1 - Verfahren und Vorrichtung zur Gewinnung Sauerstoffdruckprodukt durch Tieftemperaturzerlegung von Luft - Google Patents
Verfahren und Vorrichtung zur Gewinnung Sauerstoffdruckprodukt durch Tieftemperaturzerlegung von Luft 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
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- Prior art keywords
- pressure
- column
- feed air
- air stream
- feed
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/0446—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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.
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- 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)
Description
- 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.
Claims (9)
- Verfahren zur Gewinnung eines Drucksauerstoff-Produkts durch Tieftemperaturzerlegung von Luft in einem Rektifiziersystem, das eine Hochdrucksäule (13) und eine Niederdrucksäule (14) aufweist, bei demein erster Einsatzluftstrom (12) in die Hochdrucksäule (13) eingeführt wird,eine sauerstoffreiche Fraktion (38) aus der Niederdrucksäule (14) flüssig auf Druck gebracht (39) und auf eine Mischsäule (16) aufgegeben (41) wird,ein zweiter Einsatzluftstrom (6, 15, 306, 406) in den unteren Bereich der Mischsäule (16) eingeleitet und in Gegenstromkontakt mit der sauerstoffreichen Fraktion (41) gebracht wird,wobei die Mischsäule (16) unter einem Druck (pMiS) betrieben wird, der niedriger als der Betriebsdruck (PHDS) der Hochdrucksäule (13) ist, und bei demaus dem oberen Bereich der Mischsäule (16) gasförmiger unreiner Drucksauerstoff (51) als Kopfprodukt entnommen und als Drucksauerstoff-Produkt (52) gewonnen wird,ein Gesamtluftstrom (1), der den ersten und den zweiten Einsatzluftstromenthält, auf einen ersten Druck (p1) verdichtet (2) wird, der niedriger als der Betriebsdruck (PHDS) der Hochdrucksäule (13) ist, und unter etwa diesem ersten Druck (p1) gereinigt (3) wird, daßder gereinigte Gesamtluftstrom (4) in den ersten (5) und den zweiten (6, 306, 406) Einsatzluftstrom aufgeteilt wird und daßder erste Einsatzluftstrom (5) getrennt vom zweiten Einsatzluftstrom auf einen zweiten Druck (p2) weiterverdichtet (8, 108) wird, der mindestens gleich dem Betriebsdruck (pHDS) der Hochdrucksäule (13) ist.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der erste Druck (p1) etwa gleich dem Betriebsdruck (pMiS) der Mischsäule (16) ist.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der erste Druck niedriger als der Betriebsdruck (pMiS) der Mischsäule (16) ist und daß der zweite Einsatzluftstrom (306, 406) getrennt vom ersten Einsatzluftstrom auf einen dritten Druck (p3) weiterverdichtet (317, 417) wird, der mindestens gleich dem Betriebsdruck (pMiS) der Mischsäule (16) ist.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die flüssig auf Druck gebrachte sauerstoffreiche Fraktion vor dem Aufgeben (41) auf die Mischsäule (16) in indirektem Wärmeaustausch (40) mit einem überhitzten Luftstrom (42) angewärmt wird.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß ein dritter Einsatzluftstrom (7, 50, 207, 407, 450) arbeitsleistend entspannt (20, 420) und in die Niederdrucksäule (14) eingeleitet (21) wird.
- Verfahren nach Ansprüch 5, dadurch gekennzeichnet, daß der dritte Einsatzluftstrom (7) vor der arbeitsleistenden Entspannung (20) nachverdichtet (17) wird, wobei insbesondere bei der arbeitsleistenden Entspannung (20) erzeugte mechanische Energie zur Nachverdichtung (17) verwendet wird.
- Verfahren nach einem der Ansprüche 5 bis 6, dadurch gekennzeichnet, daß der dritte Einsatzluftstrom durch einen Teil des Gesamtluftstroms (4) stromabwärts der Reinigung (3) gebildet wird und direkt oder nach gemeinsamer Weiterverdichtung (108) mit dem ersten Einsatzluftstrom der Nachverdichtung (17) zugeführt (7, 207) wird.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß der zweite Einsatzluftstrom (306, 349, 350) vor seiner Einleitung in die Mischsäule arbeitsleistend entspannt (320) wird.
- Vorrichtung zur Gewinnung eines Drucksauerstoff-Produkts durch Tieftemperaturzerlegung von Luft mit einem Rektifiziersystem, das eine Hochdrucksäule (13) und eine Niederdrucksäule (14) aufweist, und miteiner ersten Einsatzluftleitung (5, 11, 12), die in die Hochdrucksäule (13) führt,einer Flüssigleitung (38, 41) zur Entnahme einer sauerstoffreichen Fraktion aus der Niederdrucksäule (14), die Mittel (39) zur Druckerhöhung enthält und zu einer Mischsäule (16) führt,einer zweiten Einsatzluftleitung (6, 15), die in den unteren Bereich der Mischsäule (16) führt, und mit
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DE10015602 | 2000-03-29 | ||
DE10015602A DE10015602A1 (de) | 2000-03-29 | 2000-03-29 | Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft |
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US (1) | US20010052244A1 (de) |
EP (1) | EP1139046B1 (de) |
KR (1) | KR20010093765A (de) |
CN (1) | CN1179181C (de) |
AT (1) | ATE265032T1 (de) |
DE (2) | DE10015602A1 (de) |
ES (1) | ES2219230T3 (de) |
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US5551258A (en) * | 1994-12-15 | 1996-09-03 | The Boc Group Plc | Air separation |
DE19815885A1 (de) * | 1998-04-08 | 1999-10-14 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt bei der Tieftemperaturzerlegung von Luft |
-
2000
- 2000-03-29 DE DE10015602A patent/DE10015602A1/de not_active Withdrawn
- 2000-07-21 EP EP00115777A patent/EP1139046B1/de not_active Expired - Lifetime
- 2000-07-21 ES ES00115777T patent/ES2219230T3/es not_active Expired - Lifetime
- 2000-07-21 DE DE50006148T patent/DE50006148D1/de not_active Expired - Fee Related
- 2000-07-21 AT AT00115777T patent/ATE265032T1/de not_active IP Right Cessation
-
2001
- 2001-03-28 CN CNB01109513XA patent/CN1179181C/zh not_active Expired - Fee Related
- 2001-03-29 KR KR1020010016494A patent/KR20010093765A/ko active IP Right Grant
- 2001-03-29 US US09/819,951 patent/US20010052244A1/en not_active Abandoned
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Also Published As
Publication number | Publication date |
---|---|
KR20010093765A (ko) | 2001-10-29 |
CN1320798A (zh) | 2001-11-07 |
EP1139046A1 (de) | 2001-10-04 |
ATE265032T1 (de) | 2004-05-15 |
DE50006148D1 (de) | 2004-05-27 |
ES2219230T3 (es) | 2004-12-01 |
US20010052244A1 (en) | 2001-12-20 |
CN1179181C (zh) | 2004-12-08 |
DE10015602A1 (de) | 2001-10-04 |
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