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EP1189002A1 - Process and apparatus for obtaining a gaseous product from cryogenic air separation - Google Patents

Process and apparatus for obtaining a gaseous product from cryogenic air separation 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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EP
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.)
Withdrawn
Application number
EP00124032A
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German (de)
French (fr)
Inventor
Gerhard Dipl.-Ing. Pompl
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
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1189002A1 publication Critical patent/EP1189002A1/en
Withdrawn legal-status Critical Current

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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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Abstract

Das Verfahren und die Vorrichtung dienen zur Gewinnung eines gasförmigen Produkts durch Tieftemperatur-Zerlegung von Luft in einem Rektifiziersystem, das eine Hochdrucksäule (6) und eine Niederdrucksäule (7) aufweist. Ein erster gereinigter und abgekühlter Einsatzfuftstrom (1, 3, 4) wird der Hochdrucksäule (6) zugeführt. Mindestens ein flüssiger Strom (26, 27, 28; 23, 25) aus der Hochdrucksäule (6) wird in die Niederdrucksäule (7) eingeleitet. Ein Produktstrom (52) wird flüssig aus der Niederdrucksäule abgezogen und in flüssigem Zustand auf einen erhöhten Druck gebracht (53). Der flüssige Produktstrom (54) wird unter dem erhöhten Druck in indirektem Wärmeaustausch (13) mit einem zweiten gereinigten Einsatzluftstrom (1, 3, 5) verdampft. Der bei dem indirekten Wärmeaustausch (13) mindestens teilweise kondensierte zweite Einsatzluftstrom (14) wird mindestens teilweise arbeitsleistend entspannt (15) und in die Niederdrucksäule (7) eingeleitet (17, 18, 62, 47b, 48, 49b, 50). Der Druck des zweiten Einsatzluftstroms (17) am Austritt der arbeitsleistenden Entspannung (15) ist niedriger als der Betriebsdruck am Sumpf der Hochdrucksäule (6). Die arbeitsleistende Entspannung (15) des zweiten Einsatzluftstroms (14) wird einstufig durchgeführt. <IMAGE>The method and the device serve to obtain a gaseous product by low-temperature separation of air in a rectification system which has a high-pressure column (6) and a low-pressure column (7). A first cleaned and cooled feed air stream (1, 3, 4) is fed to the high pressure column (6). At least one liquid stream (26, 27, 28; 23, 25) from the high pressure column (6) is introduced into the low pressure column (7). A product stream (52) is withdrawn in liquid form from the low-pressure column and brought to an increased pressure (53) in the liquid state. The liquid product stream (54) is evaporated under the increased pressure in indirect heat exchange (13) with a second cleaned feed air stream (1, 3, 5). The second feed air stream (14), which is at least partially condensed in the indirect heat exchange (13), is at least partially relaxed (15) while working and introduced into the low-pressure column (7) (17, 18, 62, 47b, 48, 49b, 50). The pressure of the second feed air stream (17) at the outlet of the work relaxation (15) is lower than the operating pressure at the bottom of the high pressure column (6). The work-related relaxation (15) of the second feed air flow (14) is carried out in one stage. <IMAGE>

Description

Die Erfindung betrifft ein Verfahren zur Gewinnung eines gasförmigen Produkts durch Tieftemperatur-Zerlegung von Luft gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to a method for obtaining a gaseous product Cryogenic decomposition of air according to the preamble of claim 1.

Bei dem flüssigen Produktstrom, der bei dem Verfahren gegen einen Teil der Einsatzluft, den zweiten Einsatzluftstrom, verdampft wird, handelt es sich vorzugsweise um ein Sauerstoffprodukt aus dem unteren Bereich der Niederdrucksäule beliebiger Reinheit (beispielsweise 90 bis 99,8 %, vorzugsweise 98 bis 99,8 %). Bevorzugtes Anwendungsgebiet der Erfindung sind Verfahren, bei denen der zweite Einsatzluftstrom, der zum Verdampfen des flüssigen Produktstroms eingesetzt wird, einen Druck aufweist, der nicht oder nur geringfügig höher ist als der Betriebsdruck der Hochdrucksäule (zum Beispiel bis zum Zweifachen des Hochdrucksäulen-Drucks). In diesem Fall liegen sämtliche Drücke deutlich im unterkritischen Bereich; die Begriffe "verdampfen" und "kondensieren" sind in diesem Zusammenhang im Sinne eines Phasenübergangs zu verstehen. Wird Sauerstoff unter einem derartigen relativ niedrigen Druck verdampft, wird dieser Verfahrensschritt in der Regel nicht in einem Hauptwärmetauscher durchgeführt, der zur Abkühlung von Einsatzluft von Umgebungs- auf Rektifiziertemperatur dient, sondern in einem separaten Nebenkondensator. Dort kann ein Flüssigkeitsumlauf mit Spülung eingerichtet werden, der Betriebs- und Sicherheitsprobleme durch Ausfallen schwerer flüchtiger Bestandteile verhindert.In the case of the liquid product stream which is used in the process against part of the Feed air, 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. Oxygen becomes relative under such evaporates low pressure, this process step is usually not in one Main heat exchanger carried out to cool the feed air from Ambient to rectification temperature is used, but in a separate Besides capacitor. 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.

Daneben ist die Erfindung jedoch grundsätzlich auch auf höhere Produktdrücke anwendbar, die sogar oberhalb des kritischen Drucks liegen können. Insofern schließen also die Begriffe "verdampfen" und "kondensieren" auch "pseudoverdampfen" und "pseudo-kondensieren" ein. Ein derartiges Verfahren ist aus der EP 869322 A1 (Figur 3) bekannt. Hier wird flüssige oder überkritische Luft in zwei Stufen arbeitsleistend entspannt, zunächst in einer ersten Stufe auf etwa Hochdrucksäulendruck und anschließend teilweise weiter in einer zweiten Stufe auf Niederdrucksäulendruck. In addition, however, the invention is fundamentally applicable to higher product pressures applicable, which can even be above the critical pressure. insofar the terms "evaporate" and "condense" also include "pseudo-vaporization" and "pseudo-condense" on. Such a method is known from the EP 869322 A1 (Figure 3) is known. Here liquid or supercritical air is divided into two Steps work relaxed, initially in a first step to about High-pressure column pressure and then partly in a second stage Low-pressure column pressure.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art sowie eine entsprechende Vorrichtung anzugeben, die wirtschaftlich besonders günstig sind.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.

Diese Aufgabe wird dadurch gelöst, dass die arbeitsleistende Entspannung des zweiten Einsatzluftstroms einstufig durchgeführt wird. Hiermit wird die Druckdifferenz zwischen Kondensationsdruck des zweiten Einsatzluftstroms und Niederdrucksäulendruck auf besonders effiziente und apparativ einfache Weise ausgenutzt.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.

Die arbeitsleistende Entspannung wird in einer Turbine durchgeführt, die mit einer Bremsvorrichtung gekoppelt ist. Die Bremsvorrichtung kann beispielsweise einen Generator oder eine Ölbremse aufweisen.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.

Bei dem Verfahren ist es günstig, wenn ein dritter Einsatzluftstrom auf eine Zwischentemperatur zwischen Umgebungs- und Rektifiziertemperatur abgekühlt, arbeitsleistend entspannt und der Niederdrucksäule zugeleitet wird. Zusätzlich zu dem kondensierten zweiten Einsatzluftstrom wird also ein weiterer, gasförmiger Luftstrom direkt in die Niederdrucksäule eingeführt. Mit Hilfe der beiden arbeitsleistend durchgeführten Entspannungsschritte (zweiter und dritter Einsatzluftstrom) wird das "natürliche" Druckgefälle zwischen Hochdrucksäule und Niederdrucksäule optimal ausgenützt. Es ist in vielen Fällen damit möglich, die gesamte für das Verfahren benötigte Kälte zu gewinnen, ohne dass externe Energie zur Verdichtung von Luft auf deutlich über den Betriebsdruck der Hochdrucksäule verbraucht wird. Die Entspannungsmaschine für den dritten Einsatzluftstrom ist ebenfalls mit einer Bremsvorrichtung gekoppelt; diese wird vorzugsweise durch einen Generator oder durch einen Nachverdichter gebildet. Der Nachverdichter kann beispielsweise zur Nachverdichtung des zweiten Einsatzluftstroms eingesetzt werden, der zur Verdampfung des flüssigen Produktstroms dient; diese Nachverdichtung kann im Warmen oder im Kalten stattfinden.In the method, it is advantageous if 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. In addition to that condensed second feed air stream is thus another gaseous air stream inserted directly into the low pressure column. With the help of the two working carried out relaxation steps (second and third feed air flow) will "Natural" pressure drop between high pressure column and low pressure column optimal exploited. In many cases it is possible to use the entire procedure to obtain the required cold without using external energy to compress air is consumed significantly above the operating pressure of the high pressure column. 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.

Der arbeitsleistend entspannte zweite Einsatzluftstrom kann vollständig oder teilweise direkt in die Niederdrucksäule eingeleitet werden. In vielen einschlägigen Verfahren wird jedoch im Anschluss an die Stickstoff-Sauerstoff-Trennung in Hoch- und Niederdrucksäule auch Argon gewonnen. Dazu wird eine argonhaltige Fraktion aus der Niederdrucksäule einer Rohargonrektifikation zugeleitet. In diesen Fall ist es günstig, den arbeitsleistend entspannten zweiten Einsatzluftstrom vor seiner Einführung in die Niederdrucksäule in den Verdampfungsraum des Kondensator-Verdampfers einzuleiten, der zur Erzeugung von flüssigem Rücklauf für die Rohargonrektifikation dient und beispielsweise als Kopfkondensator ausgebildet sein kann.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.

Besonders vorteilhaft ist das erfindungsgemäße Verfahren bei mäßigen Produktdrücken im zu verdampfenden Produktstrom. In solchen Fällen ist der Druck des zweiten Einsatzluftstroms bei dem indirekten Wärmeaustausch mit dem verdampfenden Produktstrom beispielsweise kleiner oder gleich dem 1,5-Fachen des Betriebsdrucks am Sumpf der Hochdrucksäule. Hierbei ist es günstig, wenn der indirekte Wärmeaustausch zur Verdampfung des Flüssigprodukts in einem Nebenkondensator durchgeführt wird, der getrennt von einem Hauptwärmetauscher ist, in dem der erste Einsatzluftstrom abgekühlt wird. Der Produktstrom kann nach seiner Verdampfung im Nebenkondensator in den Hauptwärmetauscher eingeführt und dort angewärmt werden.The method according to the invention is particularly advantageous for moderate Product pressures in the product stream to be evaporated. In such cases 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. It is advantageous if 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.

Vorzugsweise werden der erste Einsatzluftstrom und der zweite Einsatzluftstrom und gegebenenfalls der dritte Einsatzluftstrom gemeinsam auf etwa den Betriebsdruck der Hochdrucksäule verdichtet. Damit bleibt der apparative Aufwand für die Luftverdichtung relativ niedrig. Der zweite Einsatzluftstrom kann bei Bedarf stromabwärts dieser gemeinsamen Verdichtung warm oder kalt weiterverdichtet werden.Preferably, 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.

Die Erfindung betrifft außerdem eine Vorrichtung gemäß den Patentansprüchen 9 und 10.The invention also relates to a device according to claims 9 and 10th

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand eines in der Zeichnung dargestellten Ausführungsbeispiels näher erläutert.The invention and further details of the invention are described below of an embodiment shown in the drawing.

Vorgekühlte und gereinigte Einsatzluft 1 strömt einem Hauptwärmetauscher 2 zu, der in dem Beispiel als ein einziger Block ausgebildet ist. In der Praxis kann er auch durch zwei oder mehrere parallel oder seriell verbundene Wärmetauscher realisiert werden. Ein Teil 3 der Einsatzluft wird bis zum kalten Ende des Hauptwärmetauschers 2 geführt und anschließend in einen ersten Einsatzluftstrom 4 und einen zweiten Einsatzluftstrom 5 aufgeteilt. Der erste Einsatzluftstrom 4 wird in gasförmigem Zustand in den unteren Bereich einer Hochdrucksäule 6 eingeblasen. Die Hochdrucksäule 6 ist Teil eines Rektifiziersystems, das außerdem eine Niederdrucksäule 7 aufweist. Die beiden Säulen 6, 7 stehen über einen Hauptkondensator 8 in wärmetauschender Verbindung. Der Betriebsdruck am Sumpf der Hochdrucksäule 6 beträgt beispielsweise 5 bis 7 bar, vorzugsweise 5,5 bis 6 bar, derjenige am Sumpf der Niederdrucksäule 7 beispielsweise 1,3 bis 1,7 bar, vorzugsweise 1,3 bis 1,4 bar. Der Luftdruck in Leitung 1 ist etwa gleich dem Hochdrucksäulen-Druck plus Leitungsverlusten. Vorzugsweise wird die Gesamtluft gemeinsam in einem einzigen Luftverdichter (nicht dargestellt) verdichtet.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. Preferably the total air together in a single air compressor (not shown) compacted.

Bei einer Zwischentemperatur des Hauptwärmetauschers 2 wird ein dritter Einsatzluftstrom 9 abgezweigt und in einer Einblaseturbine 10 arbeitsleistend auf etwa den Betriebsdruck der Niederdrucksäule entspannt und an einer Zwischenstelle in die Niederdrucksäule eingeblasen (12). Die Einblaseturbine 10 wird in dem Beispiel mit einem Generator 11 gebremst.At an intermediate temperature of the main heat exchanger 2, a third Feed air flow 9 branched off and in a blow-in turbine 10 to approximately relaxed the operating pressure of the low pressure column and at an intermediate point in the Blown in low pressure column (12). The blowing turbine 10 is in the example with a generator 11 braked.

Der zweite Einsatzluftstrom 5 wird in einem Nebenkondensator 13 vollständig kondensiert. Die gesamte kondensierte Luft wird einer Flüssigturbine 15 zugeleitet, die eine einzige Entspannungsstufe aufweist. Hier wird die kondensierte Luft 14 von etwa Hochdrucksäulendruck auf etwa Niederdrucksäulen-Druck entspannt. Die Flüssigturbine 15 wird mittels eines Generators 16 gebremst. Die entspannte Flüssigluft 17 wird vollständig oder zu einem ersten Teil in die Niederdrucksäule eingespeist (18), und zwar an einer Zwischenstelle, die oberhalb der Stelle liegt, an der die gasförmige Luft 12 aus der Einblaseturbine 10 eingeführt wird. Alternativ beziehungsweise zusätzlich kann die entspannte Flüssigluft 17 vollständig beziehungsweise zu einem zweiten Teil über einen Verdampfungsraum eines Kondensator-Verdampfers 61 in die Niederdrucksäule geleitet werden (Leitungen 62; 47b - 48; 49b - 50); der Kondensator-Verdampfer 61 wird unten näher beschrieben.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. alternative or in addition, 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.

Gasförmiger Stickstoff 19 vom Kopf der Hochdrucksäule wird vollständig oder teilweise über Leitung 20 in den Hauptkondensator 8 eingeführt und dort in indirektem Wärmeaustausch mit verdampfendem Sauerstoff aus dem Sumpf der Niederdrucksäule 7 kondensiert. Ein erster Teil 22 des Kondensats 21 wird der Hochdrucksäule als Rücklauf aufgegeben; ein zweiter Teil 23 dient - nach Unterkühlung in einem Unterkühlungs-Gegenströmer 24 und Drosselung 25 als Rücklauf für die Niederdrucksäule 7. Flüssiger Rohsauerstoff 26 vom Sumpf der Hochdrucksäule wird ebenfalls in den Unterkühlungs-Gegenströmer 24 eingeführt. Ein erster Teil 28 des unterkühlten Rohsauerstoffs wird direkt in die Niederdrucksäule eingedrosselt, und zwar zwischen der Einblaseluft 12 und dem weiter unten beschriebenen Argonübergang 29/30.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.

Sauerstoff 52 wird als Produktstrom flüssig vom Sumpf der Niederdrucksäule 7 abgezogen und in einer Pumpe 53 auf einen Produktdruck gebracht, der beispielsweise das 1,3-Fache des Betriebsdrucks am Sumpf der Niederdrucksäule beträgt. Der flüssig auf Druck gebrachte Sauerstoff 54 wird in dem Nebenkondensator 13 - bis auf eine nicht dargestellte Spülung - vollständig verdampft und über Leitung 55 dem Hauptwärmetauscher 2 zugeführt. Der auf etwa Umgebungstemperatur angewärmte Sauerstoff 56 wird als gasförmiges Druckprodukt (GOX) gewonnen.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).

Bei dem Verfahren kann außerdem gasförmiges Druckstickstoff 58 (PGAN) erzeugt werden, indem ein Teil 57 des gasförmigen Stickstoffs 19 vom Kopf der Hochdrucksäule 6 direkt abgezogen und im Hauptwärmetauscher 2 angewärmt wird. Druckloser Stickstoff 59, 60 vom Kopf der Niederdrucksäule 7 kann ebenfalls als Produkt gewonnen und/oder als Regeneriergas in einer nicht dargestellten Einrichtung zur Reinigung der Einsatzluft eingesetzt werden.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.

Zusätzlich zur Sauerstoff-Stickstoff-Trennung weist das Verfahren des Ausführungsbeispiels einen Schritt zur Gewinnung von Argon auf. Die Niederdrucksäule 7 kommuniziert hierzu an einer weiteren Zwischenstelle (Argonübergang) über die Leitungen 29 und 30 mit einer Rohargonrektifikation, die in dem Beispiel in zwei seriell verbundenen Rohargonsäulen 31 und 32 durchgeführt wird (vergleiche europäisches Patent EP 628777). Die Gasleitung 33 und die Flüssigleitung 34 mit Pumpe 35 stellen die Verbindung zwischen den beiden Säulen 31, 32 her. Rücklauf für die Rohargonrektifikation wird in einem Kondensator-Verdampfer 61 erzeugt, der als Kopfkondensator der Säule 32 ausgebildet ist. Hier wird Kopfgas 36 der Rohargonrektifikation verflüssigt und zu einem ersten Teil 37 auf den Kopf der zweiten Rohargonsäule 32 aufgegeben. Das übrige gasförmige Rohargon 38 strömt zu einer Reinargonsäule 39 und wird dort von leichter flüchtigen Verunreinigungen befreit, die über Kopf (Leitung 41) abgezogen und verworfen (ATM) werden. Über Leitung 40 wird das Reinargon-Produkt (LAR) flüssig vom Sumpf der Reinargonsäule 39 abgeführt.In addition to oxygen-nitrogen separation, the process of 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. Here 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.

Die Sumpfheizung 42 der Reinargonsäule 39 wird mit einem Teil 43 des unterkühlten flüssigen Rohsauerstoffs 27 aus der Hochdrucksäule 6 betrieben (vergleiche europäisches Patent EP 669509). Ein Teil 44 des weiter unterkühlten Rohsauerstoffs 43 liefert die Kälte für den Kopfkondensator 45 der Reinargonsäule 39; der Rest 46 strömt in den Verdampfungsraum des Kondensator-Verdampfers 61 der Rohargonrektifikation 31/32 und wird gegebenenfalls durch einen Teil 62 der arbeitsleistend entspannten Flüssigluft 17 ergänzt. Der in den Verdampfungsräumen der beiden Kopfkondensatoren erzeugte Dampf 47a, 47b wird über Leitung 48 der Niederdrucksäule 7 zugeleitet, ebenso deren Spülflüssigkeit 49a, 49b über Leitung 50.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 Low pressure column 7 fed, as well as its rinsing liquid 49a, 49b via line 50.

Zur Erhöhung des Produktdrucks des gasförmigen Sauerstoff-Druckprodukts 55, 56 auf beispielsweise das 1,4- bis Zweifache des Betriebsdrucks der Niederdrucksäule kann das Verfahren des Ausführungsbeispiels mit einem kalten oder warmen Nachverdichter für den zweiten Einsatzluftstrom ausgestattet werden (in der Zeichnung nicht dargestellt). Im Falle einer kalten Nachverdichtung wird in Leitung 5 ein Kaltverdichter eingebaut. Bei einer warmen Weiterverdichtung wird der zweite Einsatzluftstrom bereits stromaufwärts des Hauptwärmetauschers 2 von der Gesamtluft 1 abgetrennt, einem Nachverdichter mit Nachkühlung zugeleitet, in einer eigenen Passage des Hauptwärmetauschers 2 separat abgekühlt und schließlich analog zu Leitung 5 dem Verflüssigungsraum des Nebenkondensators 13 zugeführt.To increase the product pressure of the gaseous oxygen pressure product 55, 56 to, for example, 1.4 to twice the operating pressure of the low pressure column can 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). In the case of a cold recompression, line 5 is used Cold compressor installed. In the case of a warm further compression, the second Feed air flow already upstream of the main heat exchanger 2 from the Total air 1 separated, fed to a post-compressor with after-cooling, in one own passage of the main heat exchanger 2 cooled separately and finally Analog to line 5, the liquefaction chamber of the secondary condenser 13 is supplied.

In die Leitung 14 zwischen Nebenkondensator 13 und Flüssigturbine 15 ist vorzugsweise ein Abscheider als Phasentrenneinrichtung eingebaut (ebenfalls in der Zeichnung nicht dargestellt). Hier wird derjenige Anteil des zweiten Einsatzluftstroms, der bei der Kondensation im Nebenkondensator eventuell gasförmig verblieben ist, abgetrennt und über ein Drosselventil in die Hochdrucksäule 6 und/oder in die Niederdrucksäule 7 geleitet. Nur der flüssige Anteil des (gegebenfalls partiell) kondensierten zweiten Einsatzluftstroms 14 wird zur Flüssigturbine 15 geführt. Der Abscheider kann auch zur Steuerung der Flüssigturbine 15 eingesetzt werden, indem ein Flüssigkeitsstand-Regler am Abscheider auf die Drehzahl der Flüssigturbine wirkt; über das Drosselventil für das aus dem Abscheider abgezogene Gas kann der Druck im Abscheider geregelt werden.In line 14 between secondary condenser 13 and liquid turbine 15 preferably a separator installed as a phase separator (also in the Drawing not shown). Here 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.

Claims (10)

Verfahren zur Gewinnung eines gasförmigen Produkts durch Tieftemperatur-Zerlegung von Luft in einem Rektifiziersystem, das eine Hochdrucksäule (6) und eine Niederdrucksäule (7) aufweist, wobei bei dem Verfahren a. ein erster gereinigter und abgekühlter Einsatzluftstrom (1, 3, 4) der Hochdrucksäule (6) zugeführt wird, b. mindestens ein flüssiger Strom (26, 27, 28; 23, 25) aus der Hochdrucksäule (6) in die Niederdrucksäule (7) eingeleitet wird, c. ein Produktstrom (52) flüssig aus der Niederdrucksäule abgezogen und in flüssigem Zustand auf einen erhöhten Druck gebracht (53) wird, d. der flüssige Produktstrom (54) unter dem erhöhten Druck in indirektem Wärmeaustausch (13) mit einem zweiten gereinigten Einsatzluftstrom (1, 3, 5) verdampft wird und e. der bei dem indirekten Wärmeaustausch (13) mindestens teilweise kondensierte zweite Einsatzluftstrom (14) mindestens teilweise arbeitsleistend entspannt (15) und in die Niederdrucksäule (7) eingeleitet (17, 18, 62, 47b, 48, 49b, 50) wird, f. wobei der Druck des zweiten Einsatzluftstroms (17) am Austritt der arbeitsleistenden Entspannung (15) niedriger als der Betriebsdruck am Sumpf der Hochdrucksäule (6) ist, dadurch gekennzeichnet, dass die arbeitsleistende Entspannung (15) des zweiten Einsatzluftstroms (14) einstufig durchgeführt wird.A method of recovering a gaseous product by cryogenic air separation in a rectification system comprising a high pressure column (6) and a low pressure column (7), the method a. a first cleaned and cooled feed air stream (1, 3, 4) is fed to the high pressure column (6), b. at least one liquid stream (26, 27, 28; 23, 25) is introduced from the high-pressure column (6) into the low-pressure column (7), c. a product stream (52) is withdrawn in liquid form from the low-pressure column and brought to an increased pressure (53) in the liquid state, d. the liquid product stream (54) is evaporated under the increased pressure in indirect heat exchange (13) with a second cleaned feed air stream (1, 3, 5) and e. the second feed air stream (14), which is at least partially condensed in the indirect heat exchange (13), is at least partially relaxed (15) while performing work and is introduced (17, 18, 62, 47b, 48, 49b, 50) into the low-pressure column (7), f. wherein the pressure of the second feed air flow (17) at the outlet of the work relaxation (15) is lower than the operating pressure at the bottom of the high pressure column (6), characterized in that the work-relieving relaxation (15) of the second feed air flow (14) is carried out in one stage. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass ein dritter Einsatzluftstrom (1, 9) auf eine Zwischentemperatur zwischen Umgebungs- und Rektifiziertemperatur abgekühlt (2), arbeitsleistend entspannt (10) und der Niederdrucksäule (7) zugeleitet (12) wird.A method according to claim 1, characterized in that a third feed air stream (1, 9) is cooled (2) to an intermediate temperature between ambient and rectification temperature, relaxed (10) to perform work and is fed (12) to the low-pressure column (7). Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass eine argonhaltige Fraktion (29) aus der Niederdrucksäule einer Rohargonrektifikation (31, 32) zugeleitet wird.Method according to claim 1 or 2, characterized in that an argon-containing fraction (29) from the low pressure column is fed to a crude argon rectification (31, 32). Verfahren nach Anspruch 3, dadurch gekennzeichnet, dass argonreiches Gas (36) aus der Rohargonrektifikation (32) in dem Kondensationsraum eines Kondensator-Verdampfers (61) kondensiert wird, wobei mindestens ein Teil (62) des arbeitsleistend entspannten zweiten Einsatzluftstroms (17) vor seiner Einleitung in die Niederdrucksäule (7) in den Verdampfungsraum des Kondensator-Verdampfers (61) eingeleitet wird.A method according to claim 3, characterized in that argon-rich gas (36) from the crude argon rectification (32) is condensed in the condensation space of a condenser-evaporator (61), at least part (62) of the work-relieved second feed air stream (17) before it Introduction into the low pressure column (7) in the evaporation chamber of the condenser-evaporator (61) is introduced. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass der Druck des zweiten Einsatzluftstroms (5) bei dem indirekten Wärmeaustausch (13) mit dem verdampfenden Produktstrom (52, 54) kleiner oder gleich dem Zweifachen des Betriebsdrucks am Sumpf der Hochdrucksäule (6) ist.Method according to one of claims 1 to 4, characterized in that the pressure of the second feed air stream (5) in the indirect heat exchange (13) with the evaporating product stream (52, 54) is less than or equal to twice the operating pressure at the bottom of the high pressure column (6 ) is. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass der indirekte Wärmeaustausch zur Verdampfung des Flüssigprodukts (52, 54) in einem Nebenkondensator (13) durchgeführt wird, der getrennt von einem Hauptwärmetauscher (2) ist, in dem der erste Einsatzluftstrom (1, 3, 4) abgekühlt wird.Method according to one of claims 1 to 5, characterized in that the indirect heat exchange for evaporating the liquid product (52, 54) is carried out in a secondary condenser (13) which is separate from a main heat exchanger (2) in which the first feed air stream ( 1, 3, 4) is cooled. Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass der Produktstrom (55) nach seiner Verdampfung im Nebenkondensator (13) in den Hauptwärmetauscher (2) eingeführt wird.A method according to claim 6, characterized in that the product stream (55) after its evaporation in the secondary condenser (13) is introduced into the main heat exchanger (2). Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass der erste Einsatzluftstrom und der zweite Einsatzluftstrom und gegebenenfalls der dritte Einsatzluftstrom gemeinsam (1) auf etwa den Betriebsdruck der Hochdrucksäule (6) verdichtet werden.Method according to one of claims 1 to 7, characterized in that the first feed air stream and the second feed air stream and optionally the third feed air stream are compressed together (1) to approximately the operating pressure of the high pressure column (6). Vorrichtung zur Gewinnung eines gasförmigen Produkts durch Tieftemperatur-Zerlegung von Luft mit einem Rektifiziersystem, das eine Hochdrucksäule (6) und eine Niederdrucksäule (7) aufweist, und mit a. einer ersten Einsatzluftleitung (1, 3, 4) zur Einleitung eines ersten gereinigten und abgekühlten Einsatzluftstroms in die Hochdrucksäule (6); b. mindestens einer Flüssigkeitseinsatzleitung (26, 27, 28; 23, 25) zur Einleitung eines flüssigen Stroms aus der Hochdrucksäule (6) in die Niederdrucksäule (7), c. einer Flüssigproduktleitung (52, 54) zur Entnahme eines flüssigen Produktstroms aus der Niederdrucksäule (7), die ein Mittel (53) zur Erhöhung des Drucks des flüssigen Produktstroms aufweist und d. zu einem Mittel (13) zum Verdampfen des flüssigen Produktstroms durch indirekten Wärmeaustausch führt, das mit einer zweiten Einsatzluftleitung (1, 3, 5) verbunden ist, e. mit einer Flüssigluftleitung (14, 17), die von dem Mittel (13) zum Verdampfen des flüssigen Produktstroms durch eine Entspannungsmaschine (15) in die Niederdrucksäule (7) führt, f. wobei die Entspannungsmaschine (15) so ausgebildet ist, dass ihr Austrittsdruck im Betrieb der Vorrichtung niedriger als der Betriebsdruck am Sumpf der Hochdrucksäule (6) ist, dadurch gekennzeichnet, dass die Entspannungsmaschine (15) einstufig ausgeführt ist.Device for obtaining a gaseous product by low-temperature separation of air with a rectification system, which has a high-pressure column (6) and a low-pressure column (7), and with a. a first feed air line (1, 3, 4) for introducing a first cleaned and cooled feed air stream into the high pressure column (6); b. at least one liquid feed line (26, 27, 28; 23, 25) for introducing a liquid stream from the high pressure column (6) into the low pressure column (7), c. a liquid product line (52, 54) for withdrawing a liquid product stream from the low pressure column (7), which has a means (53) for increasing the pressure of the liquid product stream and d. leads to a means (13) for evaporating the liquid product stream by indirect heat exchange, which is connected to a second feed air line (1, 3, 5), e. with a liquid air line (14, 17) leading from the means (13) for evaporating the liquid product stream through a flash machine (15) into the low pressure column (7), f. the expansion machine (15) being designed such that its outlet pressure during operation of the device is lower than the operating pressure at the bottom of the high-pressure column (6), characterized in that the relaxation machine (15) is designed in one stage. Vorrichtung nach Anspruch 9, dadurch gekennzeichnet, dass das Mittel zum Verdampfen des flüssigen Produktstroms durch indirekten Wärmeaustausch als Nebenkondensator (13) ausgebildet ist, der getrennt von einem Hauptwärmetauscher (2) ist, durch den die erste Einsatzluftleitung (1, 3, 4) führt.Apparatus according to claim 9, characterized in that the means for evaporating the liquid product stream by indirect heat exchange is designed as a secondary condenser (13) which is separate from a main heat exchanger (2) through which the first feed air line (1, 3, 4) leads ,
EP00124032A 2000-09-13 2000-11-04 Process and apparatus for obtaining a gaseous product from cryogenic air separation Withdrawn EP1189002A1 (en)

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