EP2938952A2 - Procédé et dispositif de séparation de l'air à basse température - Google Patents

Procédé et dispositif de séparation de l'air à basse température

Info

Publication number
EP2938952A2
EP2938952A2 EP13826561.6A EP13826561A EP2938952A2 EP 2938952 A2 EP2938952 A2 EP 2938952A2 EP 13826561 A EP13826561 A EP 13826561A EP 2938952 A2 EP2938952 A2 EP 2938952A2
Authority
EP
European Patent Office
Prior art keywords
condenser
column
precolumn
pressure column
feed air
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP13826561.6A
Other languages
German (de)
English (en)
Inventor
Dimitri Goloubev
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP13826561.6A priority Critical patent/EP2938952A2/fr
Publication of EP2938952A2 publication Critical patent/EP2938952A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04006—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
    • F25J3/04151—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
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04442—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 at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/10—Boiler-condenser with superposed stages
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • the invention relates to a method according to the preamble of claim 1.
  • Methods and apparatus for the cryogenic separation of air are known, for example, from Hausen / Linde, Tiefftemperaturtechnik, 2nd edition 1985, Chapter 4 (pages 281 to 337).
  • the distillation column system of the invention comprises a two-column system (for example a classical Linde double column system) for nitrogen-oxygen
  • High pressure column and low pressure column is usually by a
  • Main condenser realized in the top gas of the high pressure column is liquefied against vaporizing bottom liquid of the low pressure column.
  • the distillation column system can have more
  • Devices for example for obtaining other air components, in particular of noble gases for example, an argon recovery comprising at least one crude argon column, or a krypton-xenon recovery.
  • Distillation columns system includes in addition to the distillation columns and the directly associated with this heat exchanger, which are usually designed as a condenser evaporator.
  • a "main heat exchanger” serves to cool the feed air in indirect heat exchange with return streams from the distillation column system. It can be composed of a single or multiple parallel and / or serial
  • Heat exchanger sections may be formed, for example, from one or more plate heat exchanger blocks.
  • a secondary condenser which is also designed as a condenser-evaporator, liquid from the low-pressure column of oxygen is evaporated at a slightly elevated oxygen pressure of 1, 5 to 6 bar, preferably 2.7 to 4 bar. Part of the cooled feed air is liquefied against the evaporating oxygen.
  • condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser evaporator has a
  • Condensing passages or evaporation passages exist.
  • the condensation (liquefaction) of a first fluid flow is performed, in the evaporation space the evaporation of a second fluid flow.
  • Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • a method is sought which is capable of generating, in addition to the oxygen under the slightly increased oxygen pressure, large amounts of pressurized nitrogen and thereby the number of externally driven
  • Machines in particular the compressor, which are not driven by a turbine of the process to keep as low as possible.
  • the oxygen is intended to be produced either as pure oxygen with a purity of more than 99.5 mol% or as unrefined oxygen with a lower purity, in particular with a purity of less than 98 mol%.
  • the most compact possible arrangement is to be achieved.
  • the liquid part of the feed air to be introduced into the distillation column system comprises not more than 29 mol% and in particular between 23 and 29 mol%.
  • the secondary condenser, the top condenser and the pre-column are arranged one above the other.
  • An arrangement of two elements "one above the other" is understood here to mean that the upper end of the lower of the two elements is at a lower geodetic height than the lower end of the upper of the two elements and the projections of the two elements overlap in a horizontal plane ,
  • the two elements can be arranged exactly one above the other, that is, the axes of the two elements run on the same vertical line.
  • the operating pressure of the precolumn is preferably selected so that it corresponds to the pressure of the second partial flow of the air, which is used for the evaporation of oxygen in the
  • the operating pressure of the precolumn in the sump is preferably 7.5 to 10.5 bar.
  • the first gaseous nitrogen product can be withdrawn under pre-column pressure (at the top of this column). This pressure is about 9 bar. Depending on
  • Nitrogen product is withdrawn from the low pressure column or from the high pressure column.
  • Nitrogen product is withdrawn from the low pressure column or from the high pressure column.
  • up to 30 mol%, preferably 5 to 25 mol% of the feed air quantity can be withdrawn from the precolumn as the first gaseous nitrogen product.
  • the main air compressor MAC - Main Air Compressor
  • the total feed air to the pressure of the pre-column MAC - Main Air Compressor
  • the invention relates to the field of relatively small plants with extensive prefabrication ("packaged units") in which the abandonment of additional compressors plays a key role both in terms of equipment expense and maintenance and energy consumption.
  • packet units extensive prefabrication
  • the abandonment of additional compressors plays a key role both in terms of equipment expense and maintenance and energy consumption.
  • small nitrogen booster which regularly have a relatively poor efficiency.
  • the secondary condenser is arranged above the pre-column, in a second below the pre-column.
  • the secondary condenser and the top condenser can be arranged in a common container.
  • the container is designed as a stationary cylinder and has a dense horizontal intermediate floor between the two apparatuses.
  • a second gaseous nitrogen product can be obtained directly from the high pressure column, for example, at 5 to 6.5 bar be, without the use of a product compressor (or without low pressure stages). This is particularly beneficial if the customer requires nitrogen at various pressures that correspond approximately to the operating pressures of the guard column and high pressure column.
  • both nitrogen products can be obtained with different purities.
  • first and second gaseous nitrogen product for example, up to 50 mol%, preferably 25 to 50 mol% of the amount of feed air can be obtained as compressed nitrogen product.
  • cooling is generated according to claim 3 by a Claude turbine, which is operated with a third partial flow of the feed air and expanded into the high-pressure column. This third partial flow is in the
  • Relaxation machine is preferably formed by an expansion turbine. This can be coupled to a booster (booster) in which in particular the turbine flow (third partial flow) is recompressed upstream of the work-performing expansion.
  • booster boost
  • the turbine flow third partial flow
  • a lower oxygen concentration in the crude oxygen fraction than in the bottom of the high-pressure column is preferably produced in the bottom of the precolumn in the process according to the invention.
  • the two crude oxygen fractions are therefore not mixed together, but fed separately according to claim 4 at various intermediate points in the low-pressure column, between the two feed points are, for example, 5 to 20, preferably 7 to 15 theoretical plates.
  • the invention also relates to a device for cryogenic separation of air according to claims 8 to 13.
  • the following variants are possible and can be made within the scope of the invention
  • All condenser-evaporator can be designed as a single-storey bath evaporator (see embodiment below).
  • other condenser-evaporator designs may be used.
  • the top condenser of the precolumn can be designed as a forced-flow evaporator and / or the secondary condenser as a reflux condenser with partial liquefaction of the second partial flow of air and / or the main condenser as a multi-storey bath evaporator (cascade evaporator).
  • the main condenser may also be designed as a falling film evaporator with an associated recycle pump. This pump can also be combined with the oxygen product pump, so that adjusting the desired vapor content at the exit from the falling film evaporator and pumping the product oxygen in the
  • Secondary condenser can be handled with only a single pump.
  • Figure 1 shows a first embodiment with Maucondesator on the
  • Figure 2 shows a second embodiment with secondary capacitor under the
  • Figure 3 shows a third embodiment with the arrangement of secondary capacitor and top condenser in a common container.
  • atmospheric air is supplied via line 201 from a
  • Main air compressor 202 sucked and compressed to a pressure of about 10 bar.
  • the compressed feed air 203 is cooled in a pre-cooler 204 and
  • a cleaning device 205 which contains molecular sieve adsorbers, that is to say freed in particular from water and carbon dioxide.
  • the compressed and cleaned feed air 206 is cooled to a first part 210 in a main heat exchanger 260 to its cold end. From this, the "first partial flow” 1 and the “second partial flow” 2a are formed.
  • a "third partial flow” 230 is recompressed in a secondary compressor 466 with aftercooler 467, also led via line 231 to the warm end of the main heat exchanger 260, where it is cooled to an intermediate temperature and removed again.
  • the cooled third partial stream 232 is expanded in an expansion turbine 465 to perform work and continued via line 233. Expansion turbine 465 and boosters 466 are mechanically coupled.
  • the distillation column system comprises in the embodiment, a precolumn 10, a high-pressure column 1 1 and a low-pressure column 12 and the condenser-evaporator associated therewith, the main capacitor 13 and the top condenser 14 of the precolumn.
  • the sub-condenser 46 is not part of the distillation column system.
  • the distillation column system may additionally comprise an argon portion containing in particular at least one crude argon column and its overhead condenser;
  • the argon part may have a pure argon column for argon-nitrogen separation.
  • the separation columns for nitrogen-oxygen separation have the following operating pressures in the example (in each case at the top):
  • High-pressure column 1 1 5.0 to 6.5 bar
  • Feed air from the cold end of the main heat exchanger 260 is under a pressure which is just above the operating pressure of the pre-column 10 and is introduced immediately above the sump into the pre-column.
  • the precolumn 10 has a top condenser 4, in whose liquefaction space a nitrogen stream 31 is introduced.
  • a liquid second substream 2b of the feed air (see below) is introduced into the evaporation space of the top condenser 14 of the precolumn 10.
  • the remaining feed air is gaseous or substantially gaseous introduced via the line 233 in the distillation column system, in particular in the high-pressure column 11. From the evaporation space of the top condenser 14, an oxygen-enriched gaseous stream 16 is withdrawn and with the
  • the streams 233 and 16 may be separately (optionally different locations) introduced into the high-pressure column 1.
  • the rest 5a, 5b of the bottom liquid of the precolumn is here supercooled in a supercooling countercurrent 37 and introduced into the low-pressure column 12, at an intermediate point above the feed of the high-pressure column bottom liquid 38.
  • the in the condensation space of the top condenser 14 from a part 31 of Head nitrogen 30 of the precolumn 10 generated liquid 6 is fed as head-return into the precolumn 10.
  • Part 8 of the reflux liquid can be taken out a little deeper (as shown) and led to the top of the high-pressure column 1 1.
  • the vaporized fraction 16 formed in the evaporation space of the top condenser 14 is fed via line 17 to the bottom of the high-pressure column 11, together with the third partial stream 233 of the feed air originating from the outlet of the Claude turbine 465.
  • the rinsing liquid 32a, 32b from the top condenser 14 of the pre-column 10 is supplied to the high-pressure column 11 at an intermediate point in the lower region.
  • the double column 1/12/13 works in the well-known manner. From the high-pressure column 11 liquid raw oxygen 33 at the bottom and liquid impure nitrogen 35 are cooled from a relatively high intermediate point in a supercooling countercurrent 37 in indirect heat exchange with return streams and via lines 38 and 40 at the appropriate locations in the low pressure column 12th initiated.
  • gaseous impurity nitrogen 44, 45, 47 from the top of the low pressure column 12 (a part of which can be used as a regeneration gas in the purifier 205 - not shown in the drawing). If necessary, in the Low-pressure column 12, a pure nitrogen section can be provided and it can also be obtained low-pressure pure nitrogen,
  • liquid oxygen (a "liquid oxygen fraction") 50a from the bottom of the low pressure column 12
  • the gaseous product streams are heated in the main heat exchanger 260 in indirect heat exchange with feed air.
  • the main heat exchanger may consist of one block or of two or more blocks connected in parallel and / or in series.
  • the liquid 50a drawn off from the low-pressure column in liquid form is brought to liquid pressure in a pump 55 to a pressure of for example 2 to 5 bar, preferably 2.7 to about 4.0 bar, and then passed via line 50b into the evaporation space of the secondary condenser 46.
  • Oxygen 50c in the main heat exchanger is warmed to about ambient temperature and finally recovered (50d) as a gaseous oxygen product under medium pressure (MP GOX).
  • MP GOX medium pressure
  • the second substream 2a of the feed air is essentially completely liquefied.
  • the liquefied second substream 2b is introduced into the evaporation space of the top condenser 14 of the pre-column 10.
  • Both capacitors 14 and 46 of the embodiments are designed as a bath evaporator, wherein at least one plate heat exchanger block in a
  • FIG. 2 differs from FIG. 1 in that the secondary capacitor 46 is arranged below the pre-column 10 and the top condenser 14.
  • FIG. 3 differs from FIG. 1 in that the secondary capacitor 46 and the top condenser 14 are arranged in a common container 301.
  • the container 301 is cylindrical and has a dense intermediate bottom 302. This variant is even more compact than that of Figure 1 and thus needs less space. It also allows even more cost-effective production, further prefabrication and even easier transport of the components.

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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)
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  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un procédé et un dispositif de séparation de l'air à basse température dans un système à colonnes de distillation comprenant une colonne haute pression (11) et une colonne basse pression (12). De l'air d'alimentation est comprimé dans un compresseur d'air principal. L'air d'alimentation comprimé est lavé dans un dispositif de lavage. L'air d'alimentation lavé est refroidi dans un échangeur thermique principal. Un premier flux partiel (1) de l'air d'alimentation refroidi est introduit sous forme gazeuse dans le système à colonnes de distillation Un deuxième flux partiel (2a; 2b) de l'air d'alimentation refroidi est introduit dans la chambre de liquéfaction d'un condenseur secondaire (46) conçu en tant que condenseur-évaporateur comportant une chambre de condensation et une chambre d'évaporation. Une fraction d'oxygène liquide issue de la colonne basse pression est introduite dans la chambre d'évaporation du condenseur secondaire. Une fraction de produit d'oxygène est extraite sous forme gazeuse de la chambre d'évaporation du condenseur secondaire, chauffée dans l'échangeur thermique principal puis produite en tant que produit d'oxygène gazeux. Une première fraction de produit d'azote gazeuse est soutirée du système à colonnes de distillation, chauffée dans l'échangeur thermique principal puis produite en tant que premier produit d'azote gazeux. Le système à colonnes de distillation comporte par ailleurs une précolonne (10). Le premier flux partiel (1) de l'air de charge refroidi est introduit dans la précolonne (10). La première fraction de produit d'azote gazeuse est soutirée de la précolonne. Cette précolonne (10) comprend un condenseur de tête (14) qui se présente sous la forme d'un condenseur-évaporateur à chambre de condensation et chambre d'évaporation. Une partie liquéfiée du second flux partiel est soutirée de la chambre de liquéfaction du condenseur secondaire et introduite dans la chambre d'évaporation du condenseur de tête (14). Une fraction gazeuse (30) provenant de la partie supérieure de la précolonne (10) est introduite dans la chambre de condensation du condenseur de tête (14). Le liquide (6) formé dans la chambre de condensation est acheminé au moins partiellement en tant que reflux (7) dans la précolonne (10). Le condenseur secondaire (46), le condenseur de tête (14) et la précolonne (10) sont superposés.
EP13826561.6A 2012-12-27 2013-12-20 Procédé et dispositif de séparation de l'air à basse température Withdrawn EP2938952A2 (fr)

Priority Applications (1)

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EP13826561.6A EP2938952A2 (fr) 2012-12-27 2013-12-20 Procédé et dispositif de séparation de l'air à basse température

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EP12008635 2012-12-27
EP13826561.6A EP2938952A2 (fr) 2012-12-27 2013-12-20 Procédé et dispositif de séparation de l'air à basse température
PCT/EP2013/003929 WO2014102014A2 (fr) 2012-12-27 2013-12-20 Procédé et dispositif de séparation de l'air à basse température

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EP (1) EP2938952A2 (fr)
AU (1) AU2013369596A1 (fr)
MX (1) MX2015008172A (fr)
RU (1) RU2015130628A (fr)
WO (1) WO2014102014A2 (fr)

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EP2980514A1 (fr) * 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air
KR20210077705A (ko) * 2018-10-23 2021-06-25 린데 게엠베하 저온 공기 분리를 위한 방법 및 유닛
FR3090831B1 (fr) * 2018-12-21 2022-06-03 L´Air Liquide Sa Pour L’Etude Et L’Exploitation Des Procedes Georges Claude Appareil et procédé de séparation d’air par distillation cryogénique
CN114041034B (zh) * 2019-07-10 2023-07-21 大阳日酸株式会社 空气分离装置及空气分离方法

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US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
EP0793069A1 (fr) * 1996-03-01 1997-09-03 Air Products And Chemicals, Inc. Générateur d'oxygène à deux degrés de pureté avec compresseur pour le rebouilleur
JPH1183309A (ja) * 1997-09-04 1999-03-26 Nippon Air Rikiide Kk アルゴン精製方法及び装置
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WO2014102014A3 (fr) 2015-05-28
MX2015008172A (es) 2015-09-16
AU2013369596A1 (en) 2015-07-02
RU2015130628A (ru) 2017-01-30
WO2014102014A2 (fr) 2014-07-03
US20150316317A1 (en) 2015-11-05

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