EP1189002A1 - Procédé et dispositif d'obtention de produit gazeux d'une installation de séparation d'air cryogenique - Google Patents

Procédé et dispositif d'obtention de produit gazeux d'une installation de séparation d'air cryogenique Download PDF

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Publication number
EP1189002A1
EP1189002A1 EP00124032A EP00124032A EP1189002A1 EP 1189002 A1 EP1189002 A1 EP 1189002A1 EP 00124032 A EP00124032 A EP 00124032A EP 00124032 A EP00124032 A EP 00124032A EP 1189002 A1 EP1189002 A1 EP 1189002A1
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European Patent Office
Prior art keywords
pressure column
feed air
stream
low
liquid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP00124032A
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German (de)
English (en)
Inventor
Gerhard Dipl.-Ing. Pompl
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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
    • F25J3/04151—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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • 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 for obtaining a gaseous product Cryogenic decomposition of air according to the preamble of claim 1.
  • the second feed air stream is evaporated, it is preferably any oxygen product from the lower area of the low pressure column Purity (e.g. 90 to 99.8%, preferably 98 to 99.8%).
  • preferred Field of application of the invention are methods in which the second Feed air flow, which is used to evaporate the liquid product flow, has a pressure that is not or only slightly higher than the operating pressure of the High pressure column (for example up to twice the high pressure column pressure). In In this case, all pressures are clearly in the subcritical range; the terms In this context, "evaporate” and “condense” are in the sense of one Understand phase transition.
  • a liquid circulation with rinsing can be set up there, of operational and safety problems due to the loss of more volatile ones Components prevented.
  • the invention has for its object a method of the type mentioned as well as specify a corresponding device that is particularly economical economically are.
  • This task is solved in that the work-related relaxation of the second feed air flow is carried out in one stage. This is the pressure difference between the condensation pressure of the second feed air flow and Low pressure column pressure in a particularly efficient and simple manner exploited.
  • the work relaxation is carried out in a turbine with a Brake device is coupled.
  • the braking device can be, for example Have a generator or an oil brake.
  • a third stream of feed air is directed to a Cooled intermediate temperature between ambient and rectification temperature, relaxed workload and the low pressure column is fed.
  • condensed second feed air stream is thus another gaseous air stream inserted directly into the low pressure column.
  • relaxation steps second and third feed air flow
  • the Relaxation machine for the third feed air flow is also with one Brake device coupled; this is preferably done by a generator or formed by a post-compressor.
  • the post-compressor can, for example Post-compression of the second feed air flow used for Evaporation of the liquid product stream is used; this post-compression can Take place warm or cold.
  • the work-relieved relaxed second feed air stream can be completely or partially be introduced directly into the low pressure column. In many relevant procedures however, following the nitrogen-oxygen separation in high and Low pressure column also won argon. For this purpose, an argon-containing fraction from the Low pressure column fed to a crude argon rectification. In this case, it is convenient the work-relieved, relaxed second airflow before it is introduced into the Low pressure column in the evaporation chamber of the condenser-evaporator to initiate the generation of liquid reflux for crude argon rectification serves and can for example be designed as a top capacitor.
  • the method according to the invention is particularly advantageous for moderate Product pressures in the product stream to be evaporated.
  • there is pressure of the second feed air flow in the indirect heat exchange with the evaporating product stream for example less than or equal to 1.5 times the Operating pressure at the bottom of the high pressure column.
  • the indirect heat exchange to vaporize the liquid product in one Secondary condenser is carried out, which is separate from a main heat exchanger, in which the first feed air stream is cooled.
  • the product stream can according to its Evaporation in the secondary condenser is introduced into the main heat exchanger and there be warmed up.
  • the first feed air stream and the second feed air stream and if necessary, the third feed air flow together to about the operating pressure of the High pressure column compressed. This leaves the equipment costs for air compression relatively low.
  • the second feed air stream can flow downstream of it if necessary joint compression can be further compressed warm or cold.
  • the invention also relates to a device according to claims 9 and 10th
  • Pre-cooled and cleaned feed air 1 flows to a main heat exchanger 2 which is formed as a single block in the example. In practice, he can also by two or more heat exchangers connected in parallel or in series can be realized. Part 3 of the feed air is led to the cold end of the main heat exchanger 2 and then into a first feed air stream 4 and a second Airflow 5 divided. The first feed air stream 4 is in the gaseous state blown into the lower area of a high pressure column 6.
  • the high pressure column 6 is Part of a rectification system, which also has a low pressure column 7.
  • the two columns 6, 7 are via a main condenser 8 in heat exchanging Connection.
  • the operating pressure at the bottom of the high pressure column 6 is, for example 5 to 7 bar, preferably 5.5 to 6 bar, that at the bottom of the low-pressure column 7 for example 1.3 to 1.7 bar, preferably 1.3 to 1.4 bar.
  • the air pressure in line 1 is approximately equal to the high pressure column pressure plus line losses.
  • the blowing turbine 10 is in the example with a generator 11 braked.
  • the second feed air stream 5 is complete in a secondary condenser 13 condensed. All of the condensed air is fed to a liquid turbine 15 which has a single relaxation level. Here the condensed air 14 becomes about High pressure column pressure relaxed to about low pressure column pressure.
  • the Liquid turbine 15 is braked by means of a generator 16.
  • the relaxed one Liquid air 17 is completely or for the first part in the low pressure column fed (18), namely at an intermediate point, which is above the point at which the gaseous air 12 is introduced from the blowing turbine 10.
  • the relaxed liquid air 17 can completely or to a second part via an evaporation chamber
  • Condenser-evaporator 61 are passed into the low-pressure column (lines 62; 47b - 48; 49b - 50); the condenser-evaporator 61 is described in more detail below.
  • Gaseous nitrogen 19 from the top of the high pressure column is wholly or partially introduced via line 20 into the main capacitor 8 and there in indirect Heat exchange with evaporating oxygen from the sump Low pressure column 7 condensed.
  • a first part 22 of the condensate 21 is the High pressure column given as return; a second part 23 serves - after Subcooling in a subcooling countercurrent 24 and throttling 25 as Return for the low pressure column 7.
  • Liquid raw oxygen 26 from the bottom of the High pressure column is also introduced into the supercooling counterflow 24.
  • On first part 28 of the supercooled raw oxygen is fed directly into the low pressure column throttled, between the blowing air 12 and that below described argon transition 29/30.
  • Oxygen 52 becomes a liquid product stream from the bottom of the low pressure column 7 withdrawn and brought to a product pressure in a pump 53, the for example 1.3 times the operating pressure at the bottom of the low pressure column is.
  • the liquid 54 pressurized liquid is in the secondary condenser 13 - except for a rinse, not shown - completely evaporated and via line 55 the main heat exchanger 2 supplied.
  • the at about ambient temperature warmed oxygen 56 is obtained as a gaseous printed product (GOX).
  • the process can also produce gaseous pressurized nitrogen 58 (PGAN) by a portion 57 of the gaseous nitrogen 19 from the top of the High pressure column 6 is withdrawn directly and heated in the main heat exchanger 2.
  • Pressureless nitrogen 59, 60 from the top of the low pressure column 7 can also be used as Product obtained and / or as a regeneration gas in a facility, not shown be used to clean the feed air.
  • Embodiment a step to obtain argon.
  • the Low-pressure column 7 communicates at a further intermediate point (Argon transition) via lines 29 and 30 with a crude argon rectification, which in the example is carried out in two serially connected raw argon columns 31 and 32 (see European patent EP 628777).
  • the gas line 33 and the liquid line 34 with pump 35 establish the connection between the two columns 31, 32.
  • the return for the crude argon rectification is in a condenser-evaporator 61 generated, which is designed as a top capacitor of the column 32.
  • top gas is 36 the crude argon rectification liquefied and a first part 37 on the head of the second crude argon column 32 abandoned.
  • the remaining gaseous raw argon 38 flows in a pure argon column 39 and there is freed from more volatile impurities, which are withdrawn overhead (line 41) and discarded (ATM). Via line 40 the pure argon product (LAR) becomes liquid from the bottom of the pure argon column 39 dissipated.
  • the sump heater 42 of the pure argon column 39 is subcooled with part 43 liquid raw oxygen 27 operated from the high pressure column 6 (see European patent EP 669509).
  • Part 44 of the further supercooled raw oxygen 43 provides the cold for the top condenser 45 of the pure argon column 39; the rest 46 flows into the evaporation space of the condenser-evaporator 61 Crude argon rectification 31/32 and is possibly replaced by part 62 of the relaxed working liquid air 17 added.
  • the one in the evaporation rooms of the two top condensers generated steam 47a, 47b is via line 48
  • the method of the embodiment with a cold or warm Post-compressors can be equipped for the second feed air flow (in the drawing not shown).
  • line 5 is used Cold compressor installed.
  • a separator installed as a phase separator (also in the Drawing not shown).
  • the proportion of the second feed air flow which may have remained in gaseous form during the condensation in the secondary condenser, separated and via a throttle valve in the high pressure column 6 and / or in the Low pressure column 7 passed.
  • Only the liquid part of the (possibly partial) condensed second feed air stream 14 is fed to the liquid turbine 15.
  • the Separators can also be used to control the liquid turbine 15 by a liquid level controller on the separator acts on the speed of the liquid turbine; The pressure can be adjusted via the throttle valve for the gas drawn from the separator be regulated in the separator.

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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)
EP00124032A 2000-09-13 2000-11-04 Procédé et dispositif d'obtention de produit gazeux d'une installation de séparation d'air cryogenique Withdrawn EP1189002A1 (fr)

Applications Claiming Priority (2)

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DE10045121A DE10045121A1 (de) 2000-09-13 2000-09-13 Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Produkts durch Tieftemperaturzerlegung von Luft
DE10045121 2000-09-13

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EP1189002A1 true EP1189002A1 (fr) 2002-03-20

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US (1) US6568210B2 (fr)
EP (1) EP1189002A1 (fr)
DE (1) DE10045121A1 (fr)

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Publication number Priority date Publication date Assignee Title
RU2659698C2 (ru) * 2013-03-06 2018-07-03 Линде Акциенгезелльшафт Установка разделения воздуха, способ получения продукта, содержащего аргон, и способ изготовления установки разделения воздуха
WO2018042336A2 (fr) * 2016-08-30 2018-03-08 8 Rivers Capital, Llc Procédé de séparation d'air cryogénique pour produire de l'oxygène à des pressions élevées
US10663224B2 (en) * 2018-04-25 2020-05-26 Praxair Technology, Inc. System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit
US11933539B2 (en) * 2021-08-11 2024-03-19 Praxair Technology, Inc. Cryogenic air separation unit with argon condenser vapor recycle
US11933541B2 (en) * 2021-08-11 2024-03-19 Praxair Technology, Inc. Cryogenic air separation unit with argon condenser vapor recycle

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US4702757A (en) * 1986-08-20 1987-10-27 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4704147A (en) * 1986-08-20 1987-11-03 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4817394A (en) * 1988-02-02 1989-04-04 Erickson Donald C Optimized intermediate height reflux for multipressure air distillation
US5765396A (en) * 1997-03-19 1998-06-16 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure nitrogen and high pressure oxygen
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion

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US5114452A (en) * 1990-06-27 1992-05-19 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system for producing elevated pressure product gas
GB9100814D0 (en) * 1991-01-15 1991-02-27 Boc Group Plc Air separation
US5475980A (en) * 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
FR2761762B1 (fr) 1997-04-03 1999-05-07 Air Liquide Procede et installation de separation d'air par distillation cryogenique

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Publication number Priority date Publication date Assignee Title
US4702757A (en) * 1986-08-20 1987-10-27 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4704147A (en) * 1986-08-20 1987-11-03 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4817394A (en) * 1988-02-02 1989-04-04 Erickson Donald C Optimized intermediate height reflux for multipressure air distillation
US5765396A (en) * 1997-03-19 1998-06-16 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure nitrogen and high pressure oxygen
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion

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US6568210B2 (en) 2003-05-27
US20020029587A1 (en) 2002-03-14
DE10045121A1 (de) 2002-03-21

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