EP0758733B1 - Air separation process and apparatus by low temperature rectification - Google Patents

Air separation process and apparatus by low temperature rectification Download PDF

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Publication number
EP0758733B1
EP0758733B1 EP96112620A EP96112620A EP0758733B1 EP 0758733 B1 EP0758733 B1 EP 0758733B1 EP 96112620 A EP96112620 A EP 96112620A EP 96112620 A EP96112620 A EP 96112620A EP 0758733 B1 EP0758733 B1 EP 0758733B1
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Prior art keywords
stream
air
liquid
pressure
rectifier
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EP96112620A
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German (de)
French (fr)
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EP0758733A2 (en
EP0758733A3 (en
Inventor
Helmut Dipl.-Ing. Attlfellner
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Linde GmbH
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Linde GmbH
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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
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F25J3/04127—Gas turbine as the prime mechanical driver
    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • F25J3/046—Completely integrated air feed compression, i.e. common MAC
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/915—Combustion

Definitions

  • the invention relates to a method for air separation by low-temperature rectification in a rectification column system which has at least one rectification column with steps (a) to (h) listed in claim 1.
  • Such methods integrate the air separation by distillation and a process in which Compressed air and possibly air gases are consumed by the feed air for the Air separator and the air required in the chemical process are compressed together become.
  • the work-related relaxation of exhaust gases from the chemical Reaction generated mechanical energy is often used to generate electrical energy Energy used. If necessary, mechanical energy can also be used directly Air compression can be used.
  • the chemical reaction can be for example, coal gasification or combustion.
  • one of the products is removed from the rectification in liquid form liquid state pressurized and then against one accordingly condensed process stream evaporates, the latter at least partially condensed.
  • this internal compression it is possible to produce a gaseous product, as is often the case is required for a chemical process, with relatively little equipment to manufacture.
  • a method of the type mentioned at the outset is known from EP-A-0 584 419.
  • part of the compressed air is fed to a combustion chamber, the rest serves as Feed air for air separation.
  • Liquid oxygen becomes a low pressure stage Double rectification column removed, pressurized with a pump and counter post-compressed air evaporates.
  • the invention is based, such a method and a task to design the corresponding device so that the process is energetically special can be driven cheaply.
  • This object is achieved in that at least part of the mechanical Energy used in the work-related relaxation of the exhaust gas of the chemical Reaction is generated, is used for post-compression of the process stream, which is used for Evaporation of the liquid product stream by indirect heat exchange is used.
  • the process stream for evaporation of the liquid product can by a part of the first partial stream of the compressed air or from a nitrogen product stream the or one of the rectification columns are formed.
  • the first case it is preferred part of the feed air compressed to at least rectification pressure, partially or completely condensed against the evaporating liquid product and then fed into the or one of the rectification columns.
  • gaseous nitrogen for example from the pressure column of a double rectification column removed, post-compressed, at least partially condensed and as reflux one of the rectification columns abandoned and / or withdrawn as a liquid product.
  • Work generated in the refrigeration cycle can be used to recompress the process stream can be used, for example, via a second compressor, which mechanically with the expansion machine for the process stream is coupled.
  • This second Compressor can precompress the compressor coupled to the gas turbine downstream.
  • the liquid product stream from the lower Area of the low pressure column can be removed so that gaseous oxygen as internally compressed printed product is obtained.
  • Nitrogen e.g. from the top of the pressure column
  • argon from one connected argon rectification liquid pressure and against the post-compressed process stream are evaporated.
  • the liquid product or products before or after internal compression in a liquid tank caching it is possible the liquid product or products before or after internal compression in a liquid tank caching.
  • the invention also relates to a device for air separation by Low temperature rectification according to claim 8.
  • atmospheric air is drawn in through a filter 2, in an air compressor 3 compressed to a pressure of 5 to 14 bar, preferably 5.5 to 6.5 bar and then divided into a first partial flow 4 and a second partial flow 5.
  • the second partial stream 5 is fed to a combustion chamber 6 and there with a fuel 7 burned.
  • the exhaust gas 8 from the combustion is working in a gas turbine 9 relaxed.
  • the first partial stream 4 is freed from the heat of compression (aftercooler 10), in direct heat exchange with water 11 further cooled in a molecular sieve system 12 cleaned and fed via line 13 to the main heat exchanger 14.
  • the on about Dew point cooled air is a via line 15 of the pressure column 17 Double rectification column 16 fed, preferably directly above the sump.
  • the Operating pressure of the pressure column 17 is 5 to 14 bar, preferably 5.5 to 6.5 bar. At the Gaseous nitrogen produced at the top of the pressure column 17 becomes in the main condenser 19 liquefied against evaporating oxygen from the bottom of the low pressure column 18.
  • the condensate 20 is returned to the pressure column 17 (line 21) or - after subcooling in counterflow 23 - on the low pressure column 18 abandoned (line 22).
  • Oxygenated bottom liquid 24 from the Pressure column 17 is also supercooled (23) and at an intermediate level in the Low pressure column 18 (operating pressure 1.3 to 2 bar, preferably 1.5 to 1.7 bar) fed.
  • Gaseous nitrogen 25 from the top of the low pressure column can go after Heating in the counterflow 23 and in the main heat exchanger 14 via line 26 as Product will be deducted.
  • At least part of the oxygen product generated in the low pressure column 17 is withdrawn in liquid form (line 27) and brought to pressure by means of a pump 28, for example to 5 to 110 bar, depending on the product pressure required.
  • the pressure can be increased by static height or by Pressure build-up evaporation can be effected in a liquid tank.
  • the High-pressure liquid is evaporated in the main heat exchanger 14 and via line 29 dissipated as a gaseous printed product.
  • product evaporation is all in one Condenser evaporator separate from the main heat exchanger possible (see for example EP-A-0 584 419).
  • a part 30 of the cleaned feed air is used as Process stream used, which is used for the evaporation of the internally compressed Liquid product supplies the required heat. It is in a first post-compressor 31 and a second post-compressor 33 to a pressure of 12 to 120 bar, preferably 15 brought up to 60 bar.
  • the heat of compression is in each case in an aftercooler 32, 34 away.
  • the post-compressed air condenses at least in the main heat exchanger 14 partially, preferably completely against the evaporating liquid oxygen and is throttled via line 35 into the pressure column 17.
  • the entry point is located preferably some theoretical floors above the introduction of the main air (line 15).
  • a portion 36 of the post-compressed air is between the two post-compressors 31, 33 branched off at a temperature between the warm and cold ends of the Main heat exchanger lying temperature supplied to a turbine 37 and there Working from 10 to 60 bar, preferably 12 to 50 bar to about Pressure column pressure relaxed. The mechanical energy generated thereby becomes Post-compression 33 is used. The relaxed air 38 is shared with the Main air 15 led to the pressure column 17.
  • the turbine can 37 leading branch, the second post-compressor 33 and the after-cooler 34 omitted become.
  • the pressure required for the evaporation of the liquid product must then can be achieved in the first (and only) post-compressor 31.
  • the embodiment shown in Figure 2 differs from Figure 1 by Use of nitrogen 230 from the pressure column 17 instead of air for the Evaporation of the liquid pressurized oxygen.
  • the nitrogen gas 230 is first in the Main heat exchanger 14 warmed to about ambient temperature and then in the first post-compressor 231 and in the second post-compressor 233 to a pressure of brought from 12 to 120 bar, preferably 15 to 60 bar.
  • Part of the redensified Nitrogen is in the main heat exchanger 14 against the evaporating Liquid oxygen at least partially, preferably completely condensed and over Line 235 throttled in the pressure column 17; another part 236 is in the turbine 237, which drives the second post-compressor 233, relaxed to approximately pressure column pressure and returned to the circuit via line 238.
  • It is an embodiment with low or otherwise covered cooling requirements possible to do without the turbine-compressor combination 237/233.
  • gas turbine 9, air compressor 3 and first are seated Post-compressor 31/231, preferably on a common shaft. It depends on the mechanical energy generated in the gas turbine (taking into account the Efficiency of the machines) less or greater than that of the driven ones Compressors 3, 31/231 required power can also be a motor or generator sit on the common wave.
  • the mass transfer elements in pressure column 17 and low pressure column 18 can be made from conventional still bottoms, packing (disordered pack) and / or orderly pack exist. Combinations of different types of elements in a column are possible. Because of the low pressure drop, orderly ones Packs in all columns, especially in the low pressure column, preferred.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

Die Erfindung betrifft ein Verfahren zur Luftzerlegung durch Tieftemperaturrektifikation in einem Rektifiziersäulensystem, das mindestens eine Rektifiziersäule aufweist, mit den im Patentanspruch 1 aufgeführten Schritten (a) bis (h).The invention relates to a method for air separation by low-temperature rectification in a rectification column system which has at least one rectification column with steps (a) to (h) listed in claim 1.

Derartige Verfahren integrieren die destillative Luftzerlegung und einen Prozeß, in der Druckluft und gegebenenfalls Luftgase verbraucht werden, indem die Einsatzluft für den Luftzerleger und die in dem chemischen Prozeß benötigte Luft gemeinsam verdichtet werden. Die durch arbeitsleistende Entspannung von Abgasen aus der chemischen Reaktion erzeugte mechanische Energie wird häufig zur Gewinnung elektrischer Energie eingesetzt. Gegebenenfalls kann mechanische Energie auch unmittelbar zur Luftverdichtung verwendet werden. Bei der chemischen Reaktion kann es sich beispielsweise um eine Kohlevergasung oder um eine Verbrennung handeln.Such methods integrate the air separation by distillation and a process in which Compressed air and possibly air gases are consumed by the feed air for the Air separator and the air required in the chemical process are compressed together become. The work-related relaxation of exhaust gases from the chemical Reaction generated mechanical energy is often used to generate electrical energy Energy used. If necessary, mechanical energy can also be used directly Air compression can be used. The chemical reaction can be for example, coal gasification or combustion.

Bei dem Verfahren wird eines der Produkte flüssig aus der Rektifikation entnommen, im flüssigen Zustand auf Druck gebracht und anschließend gegen einen entsprechend verdichteten Prozeßstrom verdampft, wobei letzterer mindestens teilweise kondensiert. Mit Hilfe dieser Innenverdichtung ist es möglich, ein gasförmiges Produkt, wie es häufig für einen chemischen Prozeß benötigt wird, mit relativ geringem apparativem Aufwand herzustellen.In the process, one of the products is removed from the rectification in liquid form liquid state pressurized and then against one accordingly condensed process stream evaporates, the latter at least partially condensed. With the help of this internal compression, it is possible to produce a gaseous product, as is often the case is required for a chemical process, with relatively little equipment to manufacture.

Ein Verfahren der eingangs genannten Art ist aus der EP-A-0 584 419 bekannt. Hier wird ein Teil der verdichteten Luft einer Brennkammer zugeführt, der Rest dient als Einsatzluft für die Luftzerlegung. Flüssigsauerstoff wird aus der Niederdruckstufe einer Doppelrektifiziersäule entnommen, mit Hilfe einer Pumpe auf Druck gebracht und gegen nachverdichtete Luft verdampft.A method of the type mentioned at the outset is known from EP-A-0 584 419. Here part of the compressed air is fed to a combustion chamber, the rest serves as Feed air for air separation. Liquid oxygen becomes a low pressure stage Double rectification column removed, pressurized with a pump and counter post-compressed air evaporates.

Der Erfindung liegt die Aufgabe zugrunde, ein derartiges Verfahren und eine entsprechende Vorrichtung so auszugestalten, daß der Prozeß energetisch besonders günstig gefahren werden kann.The invention is based, such a method and a task to design the corresponding device so that the process is energetically special can be driven cheaply.

Diese Aufgabe wird dadurch gelöst, daß mindestens ein Teil der mechanischen Energie, die bei der arbeitsleistenden Entspannung des Abgases der chemischen Reaktion erzeugt wird, zur Nachverdichtung des Prozeßstroms verwendet wird, der zur Verdampfung des Flüssigproduktstroms durch indirekten Wärmeaustausch dient. This object is achieved in that at least part of the mechanical Energy used in the work-related relaxation of the exhaust gas of the chemical Reaction is generated, is used for post-compression of the process stream, which is used for Evaporation of the liquid product stream by indirect heat exchange is used.

Es braucht damit keine externe Energie für die Nachverdichtung des Prozeßstroms eingesetzt zu werden. Durch einfache mechanische Kopplung der Entspannungsmaschine für Abgas (in der Regel einer Gasturbine) mit einem Kompressor zur Nachverdichtung über eine gemeinsame Welle kann die bei der Entspannung geleistete Arbeit auf den Verdichter übertragen werden. Möglicherweise überschüssige mechanische Energie kann beispielsweise von einem Bremsgebläse aufgenommen werden, günstiger ist jedoch die Umwandlung in elektrische Energie durch Ankopplung eines Generators an die gemeinsame Welle.This means that no external energy is required for the recompression of the process stream to be used. By simple mechanical coupling of the Relaxation machine for exhaust gas (usually a gas turbine) with one Compressor for post-compression via a common shaft can be used in the Relaxation work can be transferred to the compressor. Possibly Excess mechanical energy can be generated, for example, by a brake blower are included, however, the conversion into electrical energy is cheaper by coupling a generator to the common shaft.

Zusätzlich kann ein Teil der mechanischen Energie, die bei der arbeitsleistenden Entspannung des Abgases der chemischen Reaktion erzeugt wird, auf andere Verdichter übertragen, insbesondere zur gemeinsamen Verdichtung des Luftstroms verwendet werden. Ein Generator/Elektromotor dient zum Ausgleich eines eventuellen Überschusses/Defizits an mechanischer Energie zum Antrieb der zwei oder mehr Verdichter.In addition, some of the mechanical energy used in the work Relaxation of the exhaust gas of the chemical reaction is generated on others Transfer compressor, especially for the common compression of the air flow be used. A generator / electric motor is used to compensate for a possible Excess / deficit of mechanical energy to drive the two or more Compressor.

Der Prozeßstrom zur Verdampfung des Flüssigprodukts kann durch einen Teil des ersten Teilstroms der verdichteten Luft oder durch einen Stickstoff-Produktstrom aus der oder einer der Rektifiziersäulen gebildet werden. Im ersten Fall wird vorzugsweise ein Teil der auf mindestens Rektifizierdruck verdichteten Einsatzluft nachverdichtet, gegen das verdampfende Flüssigprodukt teilweise oder vollständig kondensiert und anschließend in die oder eine der Rektifiziersäulen eingespeist. Im zweiten Fall wird gasförmiger Stickstoff beispielsweise aus der Drucksäule einer Doppelrektifiziersäule entnommen, nachverdichtet, mindestens teilweise kondensiert und als Rücklauf auf eine der Rektifiziersäulen aufgegeben und/oder als Flüssigprodukt abgezogen.The process stream for evaporation of the liquid product can by a part of the first partial stream of the compressed air or from a nitrogen product stream the or one of the rectification columns are formed. In the first case it is preferred part of the feed air compressed to at least rectification pressure, partially or completely condensed against the evaporating liquid product and then fed into the or one of the rectification columns. In the second case gaseous nitrogen, for example from the pressure column of a double rectification column removed, post-compressed, at least partially condensed and as reflux one of the rectification columns abandoned and / or withdrawn as a liquid product.

Es ist ferner günstig, wenn ein Teil des nachverdichteten Prozeßstroms, der nicht in indirekten Wärmeaustausch mit dem verdampfenden Flüssigproduktstrom gebracht wird, arbeitsleistend entspannt wird. Damit können die Verdampfung des innenverdichteten Produkts und ein Kältekreislauf, der beispielsweise mit Luft oder Stickstoff betrieben wird, integriert werden.It is also advantageous if a part of the post-compressed process stream that is not in brought indirect heat exchange with the evaporating liquid product stream will be relaxed while working. So that the evaporation of the internally compressed product and a refrigeration cycle, for example with air or Nitrogen is operated, be integrated.

Im Kältekreislauf erzeugte Arbeit kann zur Nachverdichtung des Prozeßstroms verwendet werden, beispielsweise über einen zweiten Verdichter, der mechanisch mit der Entspannungsmaschine für den Prozeßstrom gekoppelt ist. Dieser zweite Verdichter kann dem mit der Gasturbine gekoppelten Kompressor vor- oder nachgeschaltet sein.Work generated in the refrigeration cycle can be used to recompress the process stream can be used, for example, via a second compressor, which mechanically with the expansion machine for the process stream is coupled. This second Compressor can precompress the compressor coupled to the gas turbine downstream.

Wenn das Rektifiziersäulensystem eine aus Drucksäule und Niederdrucksäule bestehende Doppelsäule aufweist, kann der Flüssigproduktstrom aus dem unteren Bereich der Niederdrucksäule entnommen werden, so daß gasförmiger Sauerstoff als innenverdichtetes Druckprodukt gewonnen wird. Alternativ oder zusätzlich können Stickstoff (beispielsweise vom Kopf der Drucksäule) oder Argon aus einer angeschlossenen Argonrektifikation flüssig auf Druck gebracht und gegen den nachverdichteten Prozeßstrom verdampft werden. Selbstverständlich ist es möglich, das oder die Flüssigprodukte vor oder nach der Innenverdichtung in einem Flüssigtank zwischenzuspeichern.If the rectification column system is one of a pressure column and a low pressure column has existing double column, the liquid product stream from the lower Area of the low pressure column can be removed so that gaseous oxygen as internally compressed printed product is obtained. Alternatively or additionally you can Nitrogen (e.g. from the top of the pressure column) or argon from one connected argon rectification liquid pressure and against the post-compressed process stream are evaporated. Of course it is possible the liquid product or products before or after internal compression in a liquid tank caching.

Die Erfindung betrifft außerdem eine Vorrichtung zur Luftzerlegung durch Tieftemperaturrektifikation gemäß Patentanspruch 8.The invention also relates to a device for air separation by Low temperature rectification according to claim 8.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:

Figur 1
ein besonders bevorzugtes Ausführungsbeispiel für das erfindungsgemäße Verfahren und die erfindungsgemäße Vorrichtung, bei dem der nachverdichtete Prozeßstrom durch einen Teil der verdichteten Einsatzluft gebildet wird, und
Figur 2
ein weiteres Ausführungbeispiel mit Stickstoff als nachverdichtetem Prozeßstrom.
The invention and further details of the invention are explained in more detail below with reference to exemplary embodiments shown in the drawings. Here show:
Figure 1
a particularly preferred embodiment for the method and the device according to the invention, in which the post-compressed process stream is formed by part of the compressed feed air, and
Figure 2
another embodiment with nitrogen as a post-compressed process stream.

Zunächst werden anhand von Figur 1 diejenigen Vefahrensschritte und Apparateteile beschrieben, die beiden Ausführungsbeispielen gemeinsam sind.First, those process steps and apparatus parts are shown with reference to FIG described, the two embodiments are common.

Atmosphärische Luft wird bei 1 durch ein Filter 2 angesaugt, in einem Luftverdichter 3 auf einen Druck von 5 bis 14 bar, vorzugsweise 5,5 bis 6,5 bar komprimiert und anschließend in einen ersten Teilstrom 4 und einen zweiten Teilstrom 5 geteilt. Der zweite Teilstrom 5 wird einer Brennkammer 6 zugeführt und dort mit einem Brennstoff 7 verbrannt. Das Abgas 8 aus der Verbrennung wird in einer Gasturbine 9 arbeitsleistend entspannt. At 1, atmospheric air is drawn in through a filter 2, in an air compressor 3 compressed to a pressure of 5 to 14 bar, preferably 5.5 to 6.5 bar and then divided into a first partial flow 4 and a second partial flow 5. The second partial stream 5 is fed to a combustion chamber 6 and there with a fuel 7 burned. The exhaust gas 8 from the combustion is working in a gas turbine 9 relaxed.

Der erste Teilstrom 4 wird von der Kompressionswärme befreit (Nachkühler 10), in direktem Wärmeaustausch mit Wasser 11 weiter abgekühlt, in einer Molsiebanlage 12 gereinigt und über Leitung 13 dem Hauptwärmetauscher 14 zugeleitet. Die auf etwa Taupunkt abgekühlte Luft wird über Leitung 15 der Drucksäule 17 einer Doppelrektifiziersäule 16 zugeleitet, vorzugsweise direkt oberhalb des Sumpfes. Der Betriebsdruck der Drucksäule 17 beträgt 5 bis 14 bar, vorzugsweise 5,5 bis 6,5 bar. Am Kopf der Drucksäule 17 anfallender gasförmiger Stickstoff wird im Hauptkondensator 19 gegen verdampfenden Sauerstoff aus dem Sumpf der Niederdrucksäule 18 verflüssigt. Das Kondensat 20 wird als Rücklauf auf die Drucksäule 17 (Leitung 21) beziehungsweise - nach Unterkühlung im Gegenströmer 23 - auf die Niederdrucksäule 18 aufgegeben (Leitung 22). Sauerstoffangereicherte Sumpfflüssigkeit 24 aus der Drucksäule 17 wird ebenfalls unterkühlt (23) und auf einem Zwischenniveau in die Niederdrucksäule 18 (Betriebsdruck 1,3 bis 2 bar, vorzugsweise 1,5 bis 1,7 bar) eingespeist. Gasförmiger Stickstoff 25 vom Kopf der Niederdrucksäule kann nach Anwärmung im Gegenströmer 23 und im Hauptwärmetauscher 14 über Leitung 26 als Produkt abgezogen werden.The first partial stream 4 is freed from the heat of compression (aftercooler 10), in direct heat exchange with water 11 further cooled in a molecular sieve system 12 cleaned and fed via line 13 to the main heat exchanger 14. The on about Dew point cooled air is a via line 15 of the pressure column 17 Double rectification column 16 fed, preferably directly above the sump. The Operating pressure of the pressure column 17 is 5 to 14 bar, preferably 5.5 to 6.5 bar. At the Gaseous nitrogen produced at the top of the pressure column 17 becomes in the main condenser 19 liquefied against evaporating oxygen from the bottom of the low pressure column 18. The condensate 20 is returned to the pressure column 17 (line 21) or - after subcooling in counterflow 23 - on the low pressure column 18 abandoned (line 22). Oxygenated bottom liquid 24 from the Pressure column 17 is also supercooled (23) and at an intermediate level in the Low pressure column 18 (operating pressure 1.3 to 2 bar, preferably 1.5 to 1.7 bar) fed. Gaseous nitrogen 25 from the top of the low pressure column can go after Heating in the counterflow 23 and in the main heat exchanger 14 via line 26 as Product will be deducted.

Mindestens ein Teil des in der Niederdrucksäule 17 erzeugten Sauerstoffprodukts wird flüssig abgezogen (Leitung 27) und mittels einer Pumpe 28 auf Druck gebracht, beispielsweise auf 5 bis 110 bar, je nach benötigtem Produktdruck. Alternativ oder zusätzlich kann die Druckerhöhung durch statische Höhe oder durch Druckaufbauverdampfung in einem Flüssigtank bewirkt werden. Die Hochdruckflüssigkeit wird im Hauptwärmetauscher 14 verdampft und über Leitung 29 als gasförmiges Druckprodukt abgeführt. Alternativ ist die Produktverdampfung in einem vom Hauptwärmetauscher getrennten Kondensator-Verdampfter möglich (siehe beispielweise EP-A-0 584 419).At least part of the oxygen product generated in the low pressure column 17 is withdrawn in liquid form (line 27) and brought to pressure by means of a pump 28, for example to 5 to 110 bar, depending on the product pressure required. Alternatively or in addition, the pressure can be increased by static height or by Pressure build-up evaporation can be effected in a liquid tank. The High-pressure liquid is evaporated in the main heat exchanger 14 and via line 29 dissipated as a gaseous printed product. Alternatively, product evaporation is all in one Condenser evaporator separate from the main heat exchanger possible (see for example EP-A-0 584 419).

Im Beispiel der Figur 1 wird speziell ein Teil 30 der gereinigten Einsatzluft als Prozeßstrom eingesetzt, der die für die Verdampfung des innenverdichteten Flüssigprodukts benötigte Wärme liefert. Er wird in einem ersten Nachverdichter 31 und einem zweiten Nachverdichter 33 auf einen Druck von 12 bis 120 bar, vorzugsweise 15 bis 60 bar gebracht. Die Kompressionswärme wird jeweils in einem Nachkühler 32, 34 entfernt. Im Hauptwärmetauscher 14 kondensiert die nachverdichtete Luft mindestens teilweise, vorzugsweise vollständig gegen den verdampfenden Flüssigsauerstoff und wird über Leitung 35 in die Drucksäule 17 eingedrosselt. Die Einspeisestelle liegt vorzugsweise einige theoretische Böden oberhalb der Einführung der Hauptluft (Leitung 15). In the example in FIG. 1, a part 30 of the cleaned feed air is used as Process stream used, which is used for the evaporation of the internally compressed Liquid product supplies the required heat. It is in a first post-compressor 31 and a second post-compressor 33 to a pressure of 12 to 120 bar, preferably 15 brought up to 60 bar. The heat of compression is in each case in an aftercooler 32, 34 away. The post-compressed air condenses at least in the main heat exchanger 14 partially, preferably completely against the evaporating liquid oxygen and is throttled via line 35 into the pressure column 17. The entry point is located preferably some theoretical floors above the introduction of the main air (line 15).

Ein Teil 36 der nachverdichteten Luft wird zwischen den beiden Nachverdichtern 31, 33 abgezweigt, bei einer zwischen den Temperaturen am warmen und kalten Ende des Hauptwärmetauschers liegenden Temperatur einer Turbine 37 zugeführt und dort arbeitsleistend von 10 bis 60 bar, vorzugsweise 12 bis 50 bar auf etwa Drucksäulendruck entspannt. Die dabei erzeugte mechanische Energie wird zur Nachverdichtung 33 eingesetzt. Die entspannte Luft 38 wird gemeinsam mit der Hauptluft 15 zur Drucksäule 17 geführt.A portion 36 of the post-compressed air is between the two post-compressors 31, 33 branched off at a temperature between the warm and cold ends of the Main heat exchanger lying temperature supplied to a turbine 37 and there Working from 10 to 60 bar, preferably 12 to 50 bar to about Pressure column pressure relaxed. The mechanical energy generated thereby becomes Post-compression 33 is used. The relaxed air 38 is shared with the Main air 15 led to the pressure column 17.

Falls die in Turbine 37 gewonnene Kälte nicht benötigt wird, können der durch Turbine 37 führende Ast, der zweite Nachverdichter 33 und der Nachkühler 34 weggelassen werden. Der für die Verdampfung des Flüssigprodukts benötigte Druck muß dann bereits im ersten (und einzigen) Nachverdichter 31 erreicht werden.If the cold obtained in turbine 37 is not required, the turbine can 37 leading branch, the second post-compressor 33 and the after-cooler 34 omitted become. The pressure required for the evaporation of the liquid product must then can be achieved in the first (and only) post-compressor 31.

Das in Figur 2 dargestellte Ausführungsbeispiel unterscheidet sich von Figur 1 durch die Verwendung von Stickstoff 230 aus der Drucksäule 17 anstelle von Luft für die Verdampfung des flüssigen Drucksauerstoffs. Das Stickstoffgas 230 wird zunächst im Hauptwärmetauscher 14 auf etwa Umgebungstemperatur angewärmt und anschließend im ersten Nachverdichter 231 und im zweiten Nachverdichter 233 auf einen Druck von von 12 bis 120 bar, vorzugsweise 15 bis 60 bar gebracht. Ein Teil des nachverdichteten Stickstoffs wird im Hauptwärmetauscher 14 gegen den verdampfenden Flüssigsauerstoff mindestens teilweise, vorzugsweise vollständig kondensiert und über Leitung 235 in die Drucksäule 17 eingedrosselt; ein anderer Teil 236 wird in der Turbine 237, die den zweiten Nachverdichter 233 antreibt, auf etwa Drucksäulendruck entspannt und über Leitung 238 in den Kreislauf zurückgeführt. Ebenso wie beim ersten Ausführungsbeispiel ist es bei niedrigem oder anderweitig gedecktem Kältebedarf möglich, auf die Turbinen-Nachverdichter-Kombination 237/233 zu verzichten.The embodiment shown in Figure 2 differs from Figure 1 by Use of nitrogen 230 from the pressure column 17 instead of air for the Evaporation of the liquid pressurized oxygen. The nitrogen gas 230 is first in the Main heat exchanger 14 warmed to about ambient temperature and then in the first post-compressor 231 and in the second post-compressor 233 to a pressure of brought from 12 to 120 bar, preferably 15 to 60 bar. Part of the redensified Nitrogen is in the main heat exchanger 14 against the evaporating Liquid oxygen at least partially, preferably completely condensed and over Line 235 throttled in the pressure column 17; another part 236 is in the turbine 237, which drives the second post-compressor 233, relaxed to approximately pressure column pressure and returned to the circuit via line 238. Just like the first It is an embodiment with low or otherwise covered cooling requirements possible to do without the turbine-compressor combination 237/233.

Bei beiden Ausführungsbeispielen sitzen Gasturbine 9, Luftverdichter 3 und erster Nachverdichter 31/231 vorzugsweise auf einer gemeinsamen Welle. Je nachdem, ob die in der Gasturbine erzeugte mechanische Energie (unter Berücksichtigung des Wirkungsgrads der Maschinen) geringer oder größer als die von den angetriebenen Verdichtern 3, 31/231 benötigte Leistung ist, kann zusätzlich ein Motor oder Generator auf der gemeinsamen Welle sitzen.In both exemplary embodiments, gas turbine 9, air compressor 3 and first are seated Post-compressor 31/231, preferably on a common shaft. It depends on the mechanical energy generated in the gas turbine (taking into account the Efficiency of the machines) less or greater than that of the driven ones Compressors 3, 31/231 required power can also be a motor or generator sit on the common wave.

Die Stoffaustauschelemente in Drucksäule 17 und Niederdrucksäule 18 können aus konventionellen Destillierböden, Füllkörpern (ungeordneter Packung) und/oder geordneter Packung bestehen. Auch Kombinationen verschiedenartiger Elemente in einer Säule sind möglich. Wegen des geringen Druckverlusts werden geordnete Packungen in allen Säulen, insbesondere in der Niederdrucksäule, bevorzugt.The mass transfer elements in pressure column 17 and low pressure column 18 can be made from conventional still bottoms, packing (disordered pack) and / or orderly pack exist. Combinations of different types of elements in a column are possible. Because of the low pressure drop, orderly ones Packs in all columns, especially in the low pressure column, preferred.

Claims (8)

  1. Process for the fractionation of air by low-temperature rectification in a rectifier column system (16) which has at least one rectifier column (17, 18), comprising the following steps:
    (a) compression (3) of an air stream (1) to at least the highest pressure which prevails inside the rectifier column system (16),
    (b) splitting of the compressed air stream into a first part-stream (4), which serves as the charge air stream for the rectifier column system, and a second part-stream (5), which is fed to a chemical reaction (6) to act as an oxidizing agent,
    (c) work-performing expansion (9) of at least some of the off-gas (8) from the chemical reaction (7),
    (d) cooling (14) of the first part-stream (4) to approximately the due point temperature, and introduction (15) thereof into the or one of the rectifier columns (17),
    (e) removal of a liquid-product stream (27) from the or one of the rectifier columns (18),
    (f) increasing (28) the pressure in the liquid-product stream (27),
    (g) recompression (31, 33; 231, 233) of a process stream (30; 230) of the low-temperature rectification to a pressure which is significantly above the highest pressure which occurs in the rectifier column system (16), and
    (h) evaporation of the liquid-product stream by indirect heat exchange (15) with at least part (35, 235) of the recompressed process stream,
    characterized in that
       (i) at least some of the mechanical energy which is generated during the work-performing expansion (9) of the off-gas (8) from the chemical reaction (7) in step (c) is used for the recompression (31) of the process stream (30; 230) in step (g).
  2. Process according to Claim 1, characterized in that some of the mechanical energy which is generated during the work-performing expansion (9) of the off-gas (8) from the chemical reaction (7) in step (c) is used for the compression (3) of the air stream (1) in step (a).
  3. Process according to Claim 1 or 2, characterized in that the process stream is formed by part (30) of the first part-stream (4) of the compressed air.
  4. Process according to Claim 1 or 2, characterized in that the process stream is formed by a nitrogen product stream (230) from the or one of the rectifier columns (17).
  5. Process according to one of Claims 1 to 4, characterized in that part (36; 236) of the recompressed process stream, which is not brought into indirect heat exchange with the evaporating liquid-product stream (27), is expanded (37; 237) so as to perform work.
  6. Process according to Claim 5, characterized in that at least some of the mechanical energy which is generated during the work-performing expansion (37; 237) of the part (36; 236) of the process stream is used for the recompression (33) of the process stream.
  7. Process according to one of Claims 1 to 6, characterized in that the rectifier column system has a pressure column (17) and a low-pressure column (18), the liquid-product stream (27) being removed from the lower part of the low-pressure column (18).
  8. Apparatus for the fractionation of air by low-temperature rectification, having a rectifier column system (16), which has at least one rectifier column (17, 18), and
    (a) an air compressor (3),
    (b) a first air line (4) which leads from the outlet of the air compressor (3), through a principal heat exchanger (14), to the rectifier column system (16),
    (c) a second air line (5), which leads from the outlet of the air compressor (3) to a chemical reaction apparatus (6),
    (d) a gas turbine (9), the inlet of which is connected to the outlet of the chemical reaction device (6),
    (e) a liquid-product line (27) for removing a liquid-product stream from the or one of the rectifier columns (18),
    (f) a means (28) for increasing the pressure in the liquid-product stream,
    (g) means (33, 31; 231; 233) for the recompression of a process stream (30; 230) of the low-temperature rectification to a pressure which is significantly above the highest pressure which occurs in the rectifier column system (16), and
    (h) means (14) for the evaporation of the liquid-product stream by indirect heat exchange with at least part of the recompressed process stream,
    characterized by
       (i) means for transferring at least some of the mechanical energy which is generated in the gas turbine (9) to the means (31; 231) for the recompression of the process stream.
EP96112620A 1995-08-11 1996-08-05 Air separation process and apparatus by low temperature rectification Expired - Lifetime EP0758733B1 (en)

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DE19529681 1995-08-11
DE19529681A DE19529681C2 (en) 1995-08-11 1995-08-11 Method and device for air separation by low-temperature rectification

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EP0758733A3 EP0758733A3 (en) 1997-07-30
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DE59606078D1 (en) 2000-12-07
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US5845517A (en) 1998-12-08
EP0758733A2 (en) 1997-02-19
EP0758733A3 (en) 1997-07-30

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