[go: up one dir, main page]

EP1150082A1 - Method and apparatus for heat exchange - Google Patents

Method and apparatus for heat exchange Download PDF

Info

Publication number
EP1150082A1
EP1150082A1 EP00115776A EP00115776A EP1150082A1 EP 1150082 A1 EP1150082 A1 EP 1150082A1 EP 00115776 A EP00115776 A EP 00115776A EP 00115776 A EP00115776 A EP 00115776A EP 1150082 A1 EP1150082 A1 EP 1150082A1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
exchanger block
heat exchange
gas streams
blocks
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Withdrawn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
EP00115776A
Other languages
German (de)
French (fr)
Inventor
Horst Dipl.-Ing. Corduan
Dietrich Dipl.-Ing. Rottmann
Karl Leibl
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1150082A1 publication Critical patent/EP1150082A1/en
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • 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
    • F25J3/04084—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work 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
    • F25J3/04763—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
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/50—Arrangement of multiple equipments fulfilling the same process step in parallel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/902—Apparatus
    • Y10S62/903—Heat exchange structure

Definitions

  • the invention relates to a method for indirect heat exchange of several Gas flows with a heat / coolant in heat exchanger blocks, in which the Gas flows are passed through a variety of heat exchange passages only one of the gas streams is passed through at least one heat exchanger block. Furthermore, the invention relates to a heat exchange device for indirect Heat exchange of at least two gas flows with a heat / coolant in Heat exchanger blocks, which have a variety of heat exchange passages have.
  • the main heat exchanger is usually designed as a plate heat exchanger which has a large number of heat exchange passages for the streams to be treated. In air separation plants in which large amounts of air are processed, several such heat exchanger blocks are necessary to process the air and product quantities.
  • the main heat exchanger is usually divided into two blocks from about 20,000 to 30,000 Nm 3 / h of air.
  • collectors / distributors necessary to the gas flows from the respective inlet nozzle on the to distribute assigned heat exchange passages or from the Heat exchange passages emerging gas flows into the corresponding Merge outlet connection.
  • the collectors / distributors have so far been integrated into the heat exchanger block Distribution zones realized. In these distribution zones there are at least some of the slats that delimit the individual heat exchange passages from one another, arranged obliquely, so that the gas flowing in through the inlet connection into the Heat exchange passages is performed or that from the Heat exchange passages exiting gas flow to the outlet port is redirected.
  • the object of the present invention is to provide a method and an apparatus for to develop indirect heating or cooling of multiple gas flows which the pressure loss in the heat exchanger is as low as possible.
  • the heat exchange device for indirect heat exchange of at least two gas streams with a heat / coolant in Heat exchanger blocks, which have a variety of heat exchange passages own, is characterized in that the heat exchange passages one Heat exchanger blocks intended for one of the gas flows on two opposite end faces of the heat exchanger block and end with are in flow communication with a collector / distributor, the Collector / distributor over the entire end face of the heat exchanger block extend.
  • At least one gas flow is as low as possible Should experience pressure loss, passed through a heat exchanger block through which otherwise no further of the gas flows are carried. Stream of course through this heat exchanger block one or more heat or cold carriers with where the gas flow exchanges its heat.
  • Heat exchange passages of this heat exchanger block extend from one Face of the block to the opposite face and run essentially parallel. On the two end faces where the heat exchange passages end a collector / distributor attached to the outside of the heat exchanger block, which the covers the entire end face and a connecting piece for the supply and discharge having.
  • the heat exchange passages thus go in without a cross-sectional taper the supply and discharge via and the flow deflection in the collector / distributor takes place slowly.
  • the pressure loss in the heat exchanger block and the associated one This minimizes collectors / distributors.
  • the invention is particularly suitable in processes in which gas streams, one Have pressure of less than 3.5 bar, preferably between 1.1 and 1.8 bar, in hereinafter referred to as low pressure flows, in indirect heat exchange with a Heat or cold carriers are to be brought. According to the invention, this is done by one heat exchanger block only one of these low-pressure gas flows, i.e. for each of the gas streams that have a pressure of less than 3.5 bar its own heat exchanger block used.
  • the method according to the invention is preferably used in low-temperature decomposition of application air application.
  • the product of a low pressure column Gas streams withdrawn from the double column rectifier have only a small amount Overpressure of about 0.1 to 0.8 bar above atmospheric pressure, so that a reduction the pressure drop is of great importance. This applies analogously to gaseous Argon product, since the crude argon column also operated under relatively low pressure becomes.
  • the gas flows with the feed air in indirect are particularly preferred Heat exchange brought.
  • the feed air can be divided into several flows through the heat exchanger blocks at different pressure levels be performed.
  • the air supply can be below Pressure column pressure passed through the heat exchanger block and then into the Pressure column can be fed, on the other hand, the feed air can before Heat exchanger block recompressed and after cooling for cooling be relaxed while working.
  • the gas stream is passed through the heat exchanger blocks so that it suffers a pressure drop of 120 to 300 mbar, preferably 120 to 200 mbar.
  • a pressure drop of 120 to 300 mbar, preferably 120 to 200 mbar.
  • Figure 1 shows a process scheme known from the prior art of a large air separation plant for processing about 100,000 Nm 3 / h of air, in which it is necessary to implement the main heat exchanger by means of several separate heat exchanger blocks 3.
  • Compressed and cleaned feed air 1 becomes part 2 directly several in parallel mutually arranged heat exchanger blocks 3a - 3e supplied, in part 4 by means of of a compressor 5 post-compressed, cooled in an after-cooler 6 and then into the Heat exchanger blocks 3a - 3e directed.
  • This in the following as turbine air flow 7 designated compressed air is at an intermediate point the heat exchanger blocks 3a - 3e removed, relaxed in a turbine 8 and one in the low pressure column 10 Rectification unit 11, which has a pressure column 9 and a low pressure column 10 includes, initiated.
  • the heat exchanger blocks 3a - 3e form the main heat exchanger of the Air separation plant.
  • the supply air 2 cooled in blocks 3a - 3e becomes the Pressure column 9 of the rectification unit 11 supplied.
  • the low pressure column 10 will gaseous oxygen 14, gaseous nitrogen 15 and gaseous impure nitrogen 16 taken as regeneration gas at a pressure of about 1.3 bar. Further it is possible to use oxygen and nitrogen as liquid in the rectification unit 11 Products 12, 13 to win.
  • the gas streams 14, 15, 16 are in each of the Heat exchanger blocks 3a - 3e guided and against the feed air flow 2 and Turbine airflow 7 warmed by indirect heat exchange.
  • FIG. 1 A method diagram corresponding to FIG. 1 is shown in FIG. in contrast to the known method shown in Figure 1, the Heat exchanger blocks 3 are divided according to the invention according to products.
  • the Air flow 2 and the turbine air 7 are the same as in the method according to FIG 1 supplied to all heat exchanger blocks 23a - 23e.
  • the gaseous Gas flows 14, 15, 16 no longer in all heat exchanger blocks 23, but in in each case specifically heated to the gas streams 14, 15, 16 blocks 23.
  • the Heat exchanger blocks 23 are dimensioned so that the gaseous Oxygen stream 14 and the impure nitrogen stream 16 each have blocks 23a, 23e Result in maximum dimensions, i.e. blocks 23a and 23e are exactly on that expected oxygen or nitrogen amounts. From manufacturing technology For this reason, all blocks 23a-23e are executed with the same size, so that for the pure nitrogen flow 15, three heat exchanger blocks 23b-23d are required.
  • the heat exchanger block 23a thus only oxygen 14 against the Air flows 2 and 7 guided through the blocks 23b to 23d pure nitrogen 15 against air 2, 7 and by the heat exchanger block 23e impure nitrogen 16 against air 2, 7. Die
  • the number of heat exchanger blocks 23 thus remains in relation to the method Figure 1 the same, since the same product quantities with the same in both methods Air volumes have to exchange their heat.
  • Every heat exchanger block 23 are only three streams, two air streams 2, 7 and a gas stream 14, 15 or 16, supplied, whereby each block 23 only six collectors / distributors with the appropriate connection piece required.
  • the heat exchanger blocks 23 are in accordance with the figures 7 and 8 executed.
  • the structure of a Heat exchanger blocks 3 shown the usual way.
  • Figure 3 shows the Lamella arrangement in the distribution zones 31 for the oxygen passages 34, Figure 4 for the pure nitrogen passages 35 and Figure 5 accordingly for the Impure nitrogen passages 36.
  • Figure 6 the arrangement of all inputs and Outlet nozzle to see.
  • the distribution zones 31, 32, 33 both lead to a change in the direction of flow as well as cross-sectional changes, which in turn changes the Cause flow velocity. Both have a negative impact on the Block flow and creates an undesirable pressure drop across the Heat exchanger block 3.
  • the pressure drop affects in particular the gas flows, which have a relatively low pressure between 1.1 and 1.8 bar.
  • FIGS. 7 and 8 show the new block configuration.
  • a key feature of the The inventive method is that in each heat exchanger block 23 only one of the gas streams 14, 15, 16 is guided in countercurrent with air 2, 7. With the End faces of the heat exchanger block 23 become collectors / distributors 43, also as Dome headers are referred to as inlets and outlets for the respective gas stream 14, 15, 16 connected.
  • the collectors / distributors 43 are semi-cylindrical and have a connecting piece for the product feed or discharge.
  • the one in the new Heat exchanger block 23 introduced gas flow does not experience anything Cross-sectional change and no significant change in current direction.
  • the Pressure drop across the heat exchanger block 23 is greater than the pressure drop a usual block 3, as it was explained with reference to FIGS. 3 to 6, by approximately 30% reduced. Furthermore, the costs for the heat exchanger blocks 23 are reduced, since on the elaborate lamella cuts for the distribution zones 32 in Figures 3 to 5 can be dispensed with.
  • the new Heat exchanger blocks preferably only have a narrow distribution zone 42 at the inlet and exit area of the heat exchange passages are provided.
  • the slats in the narrow distribution zone 42 are parallel to the slats below or above the heat exchange passages are arranged, but have a smaller distance from each other.
  • the gas entering the collector 41 easily builds up in front of the Distribution zone 42, which ensures an even distribution of the gas over all passages the distribution zone 42 and thus is reached on all heat exchange passages.
  • FIGS Procedure Another advantage of the invention is shown in FIGS Procedure clearly.
  • the piping in the new process much easier.
  • the number of block sockets from ten to six per heat exchanger block are also fewer manifolds and Pipe bends necessary to block the gas flows 14, 15, 16 feed.
  • the method according to the invention is not restricted to such processes only where all products are obtained in gaseous form, but also, for example Internal compression processes in which liquid products from the rectification unit subtracted from.
  • Figure 9 shows the scheme of an air separation process in which in addition gaseous pure nitrogen 15 and gaseous impure nitrogen 16 liquid nitrogen 51 removed from the main capacitor of the rectification unit 11 and by means of an internal compression pump 52 is brought to increased pressure.
  • the liquid and Nitrogen 51 brought to increased pressure is then in the heat exchanger block 56 against air 7 and compressed by the compressor 59 high pressure air evaporates and warmed up.
  • the oxygen 12 is also in liquid form from the Low pressure column 10 is withdrawn and using the two pumps 54 and 55 internally compressed.
  • the pure nitrogen stream 15 and the impure nitrogen stream 16 are in the heat exchanger blocks 23b, c, d and block 23e, respectively, respectively 7 and 8 are constructed, heated.
  • internally compressed streams 57, 58 find a high-pressure heat exchanger block 56 Application.
  • the high-pressure heat exchanger block 56 corresponds at first glance the heat exchanger block explained with reference to Figures 3 to 6, but has one significantly higher strength to withstand the high pressures of internal compression flows to be able to withstand. Those occurring in the heat exchanger block 56 Pressure losses have a far less effect on the internal compression flows 57, 58 negative than in the gaseous gas streams 15, 16 from the low pressure column 10.
  • FIG. 10 A method similar to that in FIG. 9 is shown in FIG. 10, in which likewise liquid oxygen 12 is internally compressed 54, 55, but not against high pressure air, but is vaporized and heated against high pressure nitrogen.
  • the Pressure column 9 removed gaseous nitrogen at 61 through which Heat exchanger block 62 out, compressed by means of the compressor 63 and in Countercurrent passed through the heat exchanger block 62 back into the pressure column 9.
  • the construction of the heat exchanger block 62 corresponds essentially to that Heat exchanger block 56 in FIG. 9. There is no internal compression of nitrogen this variant, since 63 high-pressure nitrogen 64 are drawn off after the compressor can.
  • FIG. 11 shows a further application of the method according to the invention.
  • liquid oxygen is removed from the rectification column 11 at 12 and by means of the two pumps 54, 55 internally compressed.
  • the evaporation of liquid oxygen takes place in this embodiment against circulating nitrogen, which at 61 from the Pressure column 9 removed, warmed in the heat exchanger block 77, with the compressors 71, 72, 73 compressed and in the heat exchanger block 77 against the Internal compression products cooled and passed into the pressure column 9 76.
  • a part of the nitrogen is expanded after the compressor 71 (74) and into the Nitrogen cycle returned.
  • Another part of the nitrogen is released Compression in compressors 71, 72, 73 and subsequent cooling in Heat exchanger block 77 at an intermediate point from the heat exchanger block 77 deducted, relaxed at 75 and returned to the nitrogen cycle.

Landscapes

  • 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)

Abstract

Process for the indirect heat exchange of gas streams (14, 15, 16) with a hot/cold carrier in heat exchanger blocks (23a, 23b, 23c, 23d, 23e) comprises passing the gas streams through a number of heat exchange passages which terminate at two front surfaces of the heat exchange blocks. The gas streams are introduced via a collector/distributor which extends over the whole front surface of the blocks. An Independent claim is also included for a heat exchanger for the indirect heat exchange of gas streams with a hot/cold carrier in heat exchanger blocks. Preferred Features: Each of the gas streams are introduced through a separate heat exchanger block. The gas streams are under a pressure of 1.1-1.8 bar. The gas streams are obtained by the low temperature decomposition of process air.

Description

Die Erfindung betrifft ein Verfahren zum indirekten Wärmeaustausch von mehreren Gasströmen mit einem Wärme-/Kälteträger in Wärmetauscherblöcken, in denen die Gasströme durch eine Vielzahl von Wärmeaustauschpassagen geleitet werden, wobei durch mindestens einen Wärmetauscherblock nur einer der Gasströme geleitet wird. Ferner bezieht sich die Erfindung auf eine Wärmeaustauschvorrichtung zum indirekten Wärmeaustausch von mindestens zwei Gasströmen mit einem Wärme-/Kälteträger in Wärmetauscherblöcken, welche eine Vielzahl von Wärmeaustauschpassagen besitzen.The invention relates to a method for indirect heat exchange of several Gas flows with a heat / coolant in heat exchanger blocks, in which the Gas flows are passed through a variety of heat exchange passages only one of the gas streams is passed through at least one heat exchanger block. Furthermore, the invention relates to a heat exchange device for indirect Heat exchange of at least two gas flows with a heat / coolant in Heat exchanger blocks, which have a variety of heat exchange passages have.

Bei der Tieftemperaturzerlegung von Luft muß die zu zerlegende Einsatzluft auf die Verfahrenstemperatur abgekühlt werden. Dies erfolgt üblicherweise im Hauptwärmetauscher durch indirekten Wärmeaustausch der Einsatzluft mit den gewonnenen Gasströmen. Der Hauptwärmetauscher ist in der Regel als Plattenwärmetauscher ausgebildet, der eine Vielzahl von Wärmeaustauschpassagen für die zu behandelnden Ströme besitzt. Bei Luftzerlegungsanlagen, in denen große Luftmengen verarbeitet werden, sind mehrere solcher Wärmetauscherblöcke notwendig, um die Luft- und Produktmengen zu verarbeiten. Üblicherweise wird der Hauptwärmetauscher ab etwa 20000 bis 30000 Nm3/h Luft in zwei Blöcke aufgeteilt.When air is decomposed at low temperatures, the feed air to be separated must be cooled to the process temperature. This is usually done in the main heat exchanger by indirect heat exchange of the feed air with the gas flows obtained. The main heat exchanger is usually designed as a plate heat exchanger which has a large number of heat exchange passages for the streams to be treated. In air separation plants in which large amounts of air are processed, several such heat exchanger blocks are necessary to process the air and product quantities. The main heat exchanger is usually divided into two blocks from about 20,000 to 30,000 Nm 3 / h of air.

Üblicherweise werden bisher durch jeden der einzelnen Wärmetauscherblöcke alle Gasströme sowie der Einsatzluftstrom und gegebenenfalls weitere Ströme geleitet. Werden einer Luftzerlegungsanlage beispielsweise zwei Luftströme unterschiedlichen Drucks zugeführt und als gasförmige Produkte Sauerstoff, Reinstickstoff und unreiner Stickstoff gewonnen, müssen durch jeden Wärmetauscherblock fünf Ströme geleitet werden. Jeder Wärmetauscherblock muß daher zehn Anschlußstutzen für diese Ströme, je fünf für den Gasein- und fünf für den Gasaustritt, aufweisen.Up to now, all of the individual heat exchanger blocks have usually been used for all Gas streams as well as the feed air flow and possibly further streams are passed. For example, an air separation plant will have two different air flows Pressure supplied and as gaseous products oxygen, pure nitrogen and impure Nitrogen recovered, five flows have to be passed through each heat exchanger block become. Each heat exchanger block must therefore have ten connecting pieces for this Currents, five for the gas inlet and five for the gas outlet.

Dementsprechend sind zehn Vorrichtungen, im folgenden als Sammler/Verteiler bezeichnet, notwendig, um die Gasströme von dem jeweiligen Eintrittsstutzen auf die zugeordneten Wärmeaustauschpassagen zu verteilen beziehungsweise die aus den Wärmeaustauschpassagen austretenden Gasströme in die entsprechenden Austrittsstutzen zusammenzuführen.Accordingly, there are ten devices, hereinafter referred to as collectors / distributors referred to, necessary to the gas flows from the respective inlet nozzle on the to distribute assigned heat exchange passages or from the Heat exchange passages emerging gas flows into the corresponding Merge outlet connection.

Die Sammler/Verteiler werden bisher durch in den Wärmetauscherblock integrierte Verteilzonen realisiert. In diesen Verteilzonen sind zumindest ein Teil der Lamellen, die die einzelnen Wärmeaustauschpassagen voneinander abgrenzen, schräg angeordnet, so daß das über den Eintrittsstutzen einströmende Gas in die Wärmeaustauschpassagen geführt wird bzw. daß die aus den Wärmeaustauschpassagen austretende Gasströmung zu dem Austrittsstutzen umgelenkt wird.The collectors / distributors have so far been integrated into the heat exchanger block Distribution zones realized. In these distribution zones there are at least some of the slats that delimit the individual heat exchange passages from one another, arranged obliquely, so that the gas flowing in through the inlet connection into the Heat exchange passages is performed or that from the Heat exchange passages exiting gas flow to the outlet port is redirected.

Die Strömungsbedingungen werden allerdings in den Verteilzonen derartiger Sammler/Verteiler stark geändert. Zum einen tritt durch die schräge Ausrichtung der Lamellen eine Änderung der Stromrichtung auf, zum anderen sind die Querschnitte der Wärmeaustauschpassagen in dem Verteilbereich deutlich verringert, wodurch Geschwindigkeitswechsel des durchströmenden Gases verursacht werden. Beide Effekte erzeugen einen unerwünschten Druckabfall in den Wärmetauscherblöcken.However, the flow conditions in the distribution zones become more such Collectors / distributors changed significantly. Firstly, due to the oblique orientation of the Slats change the current direction on the other are the cross sections of the Heat exchange passages in the distribution area significantly reduced, which Changes in speed of the gas flowing through are caused. Both Effects create an undesirable pressure drop in the heat exchanger blocks.

Aus der DE-A-42 04 172 ist bekannt, den Hauptwärmetauscher einer Luftzerlegungsanlage verfahrensseitig in mehrere Blöcke aufzuteilen, wobei jeder in der Luftzerlegungsanlage gewonnene Produktstrom über einen eigenen Wärmetauscherblock gegen Einsatzluft geführt wird. Das Verfahren zielt darauf ab, den Regelaufwand für die einzelnen Wärmetauscherblöcke zu verringern. Die Schrift befaßt sich dagegen nicht mit dem durch die Verteilzonen der Blöcke hervorgerufenen Druckverlust und beinhaltet dementsprechend auch keine Maßnahmen, die geeignet wären, diesen Druckverlust zu verringern.From DE-A-42 04 172 it is known that the main heat exchanger On the process side, the air separation plant is divided into several blocks, each in the air separation plant won product stream over its own Heat exchanger block is guided against feed air. The process aims to Reduce the control effort for the individual heat exchanger blocks. The Scriptures are concerned on the other hand, not with that caused by the distribution zones of the blocks Pressure loss and accordingly does not include any measures that are suitable would be to reduce this pressure drop.

Aufgabe vorliegender Erfindung ist es, ein Verfahren und eine Vorrichtung zur indirekten Erwärmung oder Abkühlung von mehreren Gasströmen zu entwickeln, bei dem der Druckverlust in dem Wärmetauscher möglichst gering ist.The object of the present invention is to provide a method and an apparatus for to develop indirect heating or cooling of multiple gas flows which the pressure loss in the heat exchanger is as low as possible.

Diese Aufgabe wird erfindungsgemäß durch ein Verfahren der eingangs genannten Art gelöst, wobei die Wärmeaustauschpassagen für den einen Gasstrom des mindestens einen Wärmetauscherblocks an zwei Stirnflächen des Wärmetauscherblocks enden und der eine Gasstrom den Wärmeaustauschpassagen des mindestens einen Wärmetauscherblocks über jeweils einen mit dem Wärmetauscherblock verbundenen Sammler/Verteiler zugeführt und entnommen wird, welcher sich jeweils über die gesamte Stirnfläche des Wärmetauscherblocks erstreckt.This object is achieved by a method of the type mentioned solved, the heat exchange passages for the one gas stream of the at least a heat exchanger block end on two end faces of the heat exchanger block and the one gas flow the heat exchange passages of the at least one Heat exchanger blocks each connected to the heat exchanger block Collector / distributor is supplied and removed, which is in each case on the entire end face of the heat exchanger block extends.

Die erfindungsgemäße Wärmeaustauschvorrichtung zum indirekten Wärmeaustausch von mindestens zwei Gasströmen mit einem Wärme-/Kälteträger in Wärmetauscherblöcken, welche eine Vielzahl von Wärmeaustauschpassagen besitzen, zeichnet sich dadurch aus, daß die Wärmeaustauschpassagen eines Wärmetauscherblocks, die für einen der Gasströme vorgesehen sind, an zwei gegenüberliegenden Stirnflächen des Wärmetauscherblocks enden und jeweils mit einem Sammler/Verteiler in Strömungsverbindung stehen, wobei sich die Sammler/Verteiler jeweils über die gesamte Stirnfläche des Wärmetauscherblocks erstrecken.The heat exchange device according to the invention for indirect heat exchange of at least two gas streams with a heat / coolant in Heat exchanger blocks, which have a variety of heat exchange passages own, is characterized in that the heat exchange passages one Heat exchanger blocks intended for one of the gas flows on two opposite end faces of the heat exchanger block and end with are in flow communication with a collector / distributor, the Collector / distributor over the entire end face of the heat exchanger block extend.

Erfindungsgemäß wird zumindest ein Gasstrom, der einen möglichst geringen Druckverlust erfahren soll, durch einen Wärmetauscherblock geleitet, durch den ansonsten keine weiteren der Gasströme geführt werden. Selbstverständlich strömen durch diesen Wärmetauscherblock ein oder mehrere Wärme- oder Kälteträger, mit denen der Gasstrom seine Wärme austauscht. Die für diesen Gasstrom vorgesehenen Wärmeaustauschpassagen dieses Wärmetauscherblocks erstrecken sich von einer Stirnseite des Blocks zur gegenüberliegenden Stirnseite und verlaufen im wesentlichen parallel. An den beiden Stirnseiten, an denen die Wärmeaustauschpassagen enden, ist jeweils außen an dem Wärmetauscherblock ein Sammler/Verteiler angebracht, der die gesamte Stirnfläche abdeckt und einen Anschlußstutzen für die Zu- bzw. Ableitung aufweist. Die Wärmeaustauschpassagen gehen somit ohne Querschnittsverjüngung in die Zu- bzw. Ableitung über und die Strömungsumlenkung in dem Sammler/Verteiler erfolgt langsam. Der Druckverlust in dem Wärmetauscherblock und den zugehörigen Sammler/Verteilern wird dadurch minimiert.According to the invention, at least one gas flow is as low as possible Should experience pressure loss, passed through a heat exchanger block through which otherwise no further of the gas flows are carried. Stream of course through this heat exchanger block one or more heat or cold carriers with where the gas flow exchanges its heat. The intended for this gas stream Heat exchange passages of this heat exchanger block extend from one Face of the block to the opposite face and run essentially parallel. On the two end faces where the heat exchange passages end a collector / distributor attached to the outside of the heat exchanger block, which the covers the entire end face and a connecting piece for the supply and discharge having. The heat exchange passages thus go in without a cross-sectional taper the supply and discharge via and the flow deflection in the collector / distributor takes place slowly. The pressure loss in the heat exchanger block and the associated one This minimizes collectors / distributors.

Mit dem erfindungsgemäßen Verfahren und der entsprechenden Vorrichtung lassen sich Druckabfälle in den Wärmetauscherblöcken, gemessen vom Eintrittsstutzen bis zum Austrittsstutzen, von etwa 70 mbar erzielen. Demgegenüber tritt bei den herkömmlichen Wärmetauschern, bei denen die Verteilung und Zusammenführung der Gasströme zwischen dem Ein- bzw. Austrittsstutzen und den Wärmeaustauschpassagen durch eine in den Wärmetauscherblock integrierte Verteilzone mit schräg angeordneten Lamellen ein Druckabfall von etwa 100 mbar auf, wenn die Gasströme mit einem Druck zwischen 1,2 und 1,8 bar aus der Niederdrucksäule entnommen wurden. Auf der drucklosen Seite erreicht man durch die Erfindung eine Verringerung des Druckabfalls von etwa 30 mbar. Das bedeutet, daß die Niederdruckströme mit einem um 30 mbar niedrigeren Druck als sonst gewonnen werden können. Zur Aufrechterhaltung der Wärmeaustauschverhältnisse am Hauptkondensator reicht es dann aus, wenn die Luft nach dem Luftverdichter auf einen etwa 90 mbar niedrigeren Druck verdichtet wird.Leave with the inventive method and the appropriate device pressure drops in the heat exchanger blocks, measured from the inlet connection to to the outlet nozzle, of about 70 mbar. In contrast, the conventional heat exchangers in which the distribution and merging of Gas flows between the inlet and outlet nozzle and the Heat exchange passages through an integrated in the heat exchanger block Distribution zone with slanted slats a pressure drop of about 100 mbar, if the gas flows with a pressure between 1.2 and 1.8 bar from the Low pressure column were removed. On the unpressurized side you can reach through the Invention a reduction in pressure drop of about 30 mbar. It means that the low pressure flows are obtained at a pressure 30 mbar lower than usual can be. To maintain the heat exchange conditions on Main condenser, it is sufficient if the air after the air compressor on one about 90 mbar lower pressure is compressed.

Vorzugsweise ist für jeden Gasstrom jeweils ein separater Wärmetauscherblock vorgesehen. Dies hat einerseits den oben beschriebenen Vorteil des geringen Druckverlustes, andererseits wird der Verrohrungsaufwand verringert. Hinzu kommt noch die Kostenreduzierung der Wärmeaustauschblöcke, da die Verteilzonen wesentlich einfacher gestaltet sind. Bei dem üblichen Verfahren, bei dem durch jeden Wärmetauscherblock alle Gasströme fließen, sind für jeden Gasstrom sowohl auf der kalten als auch auf der warmen Seite des Hauptwärmetauschers je eine Sammelleitung als Zu- bzw. Ableitung mit mehreren Abzweigungen zu jedem Wärmetauscherblock notwendig. Wird dagegen jeder Gasstrom durch einen eigenen Wärmetauscherblock geführt, so können die Abzweigungen entfallen und die Verrohrung wird wesentlich vereinfacht.There is preferably a separate heat exchanger block for each gas stream intended. On the one hand, this has the small advantage described above Pressure loss, on the other hand, the piping effort is reduced. Come in addition nor the cost reduction of the heat exchange blocks because of the distribution zones are much simpler. In the usual procedure, in which everyone Heat exchanger block all gas flows are flowing for each gas flow on both cold as well as on the warm side of the main heat exchanger Bus line as feed or discharge with several branches to each Heat exchanger block necessary. In contrast, each gas stream is replaced by its own Out heat exchanger block, the branches can be omitted and the Piping is significantly simplified.

Sofern die Gasmenge, die über einen separaten Wärmetauscherblock geführt werden soll, so groß ist, daß diese in einem Block nicht verarbeitet werden kann, so werden zwei oder mehr Wärmetauscherblöcke vorgesehen, durch die jeweils Teilströme dieses Gases geleitet werden.If the amount of gas that is passed through a separate heat exchanger block should be so large that it cannot be processed in a block two or more heat exchanger blocks are provided, through the respective partial flows of this Gases are routed.

Besonders geeignet ist die Erfindung bei Verfahren, bei denen Gasströme, die einen Druck von weniger als 3,5 bar, bevorzugt zwischen 1,1 und 1,8 bar, aufweisen, im folgenden als Niederdruckströme bezeichnet, in indirekten Wärmeaustausch mit einem Wärme- oder Kälteträger gebracht werden sollen. Erfindungsgemäß wird hierbei durch einen Wärmertauscherblock jeweils nur einer dieser Niederdruckgasströme geführt, d.h. für jeden der Gasströme, die einen Druck von weniger als 3,5 bar aufweisen, wird ein eigener Wärmetauscherblock eingesetzt. The invention is particularly suitable in processes in which gas streams, one Have pressure of less than 3.5 bar, preferably between 1.1 and 1.8 bar, in hereinafter referred to as low pressure flows, in indirect heat exchange with a Heat or cold carriers are to be brought. According to the invention, this is done by one heat exchanger block only one of these low-pressure gas flows, i.e. for each of the gas streams that have a pressure of less than 3.5 bar its own heat exchanger block used.

Bei Gasströmen mit einem Druck von mehr als ca. 4 bar spielt der Druckverlust in dem Wärmetauscherblock nur eine untergeordnete Rolle bzw. kann vemachlässigt werden. Es ist daher manchmal vorteilhaft, durch mindestens einen der Wärmetauscherblöcke, durch den einer der Niederdruckgasströme geleitet wird, zusätzlich einen solchen Strom mit erhöhtem Druck zu führen.With gas flows with a pressure of more than approx. 4 bar, the pressure loss plays in the Heat exchanger block only a subordinate role or can be neglected. It is therefore sometimes advantageous to use at least one of the heat exchanger blocks, through which one of the low-pressure gas streams is passed, additionally one Conduct electricity with increased pressure.

Das erfindungsgemäße Verfahren findet bevorzugt bei der Tieftemperaturzerlegung von Einsatzluft Anwendung. Die als Produkt aus der Niederdrucksäule eines Doppelsäulenrektifikators abgezogenen Gasströme besitzen lediglich einen geringen Überdruck von etwa 0,1 bis 0,8 bar über Atmosphärendruck, sodaß eine Verringerung des Druckabfalls von hoher Bedeutung ist. Dies gilt in analoger Weise für gasförmiges Argonprodukt, da die Rohargonsäule ebenfalls unter relativ niedrigem Druck betrieben wird.The method according to the invention is preferably used in low-temperature decomposition of application air application. The product of a low pressure column Gas streams withdrawn from the double column rectifier have only a small amount Overpressure of about 0.1 to 0.8 bar above atmospheric pressure, so that a reduction the pressure drop is of great importance. This applies analogously to gaseous Argon product, since the crude argon column also operated under relatively low pressure becomes.

Besonders bevorzugt werden die Gasströme mit der Einsatzluft in indirekten Wärmeaustausch gebracht. Die Einsatzluft kann hierbei in mehreren auf unterschiedlichem Druckniveau liegenden Strömen durch die Wärmetauscherblöcke geführt werden. So kann die Einsatzluft beispielsweise zum einen unter Drucksäulendruck durch den Wärmetauscherblock geleitet und anschließend in die Drucksäule eingespeist werden, zum anderen kann die Einsatzluft vor dem Wärmetauscherblock nachverdichtet und nach Abkühlung zur Kälteerzeugung arbeitsleistend entspannt werden.The gas flows with the feed air in indirect are particularly preferred Heat exchange brought. The feed air can be divided into several flows through the heat exchanger blocks at different pressure levels be performed. For example, the air supply can be below Pressure column pressure passed through the heat exchanger block and then into the Pressure column can be fed, on the other hand, the feed air can before Heat exchanger block recompressed and after cooling for cooling be relaxed while working.

In Ländern mit relativ niedrigen Energiekosten bringt eine Verringerung der Druckabfälle keinen Vorteil, da die mit der Energieeinsparung verbundenen Kosten hoch sind. Bei diesen Anwendungen ist es daher günstiger, nicht die Druckverluste zu minimieren, sondern die Strömungsgeschwindigkeiten zu erhöhen, um höhere Druckabfälle zu erzielen, wodurch letztlich kleinere Wärmetauscherblöcke erforderlich sind.In countries with relatively low energy costs brings a reduction in Pressure drops are not an advantage because of the costs associated with saving energy are high. In these applications it is therefore cheaper not to lose pressure minimize, but rather increase the flow velocities to higher ones To achieve pressure drops, which ultimately requires smaller heat exchanger blocks are.

Vorzugsweise wird der Gasstrom so durch die Wärmetauscherblöcke geleitet, daß er einen Druckabfall von 120 bis 300 mbar, bevorzugt 120 bis 200 mbar, erleidet. Durch Anhebung des Druckabfalls wird eine größere Strömungsgeschwindigkeit als in den herkömmlichen Wärmetauschern erreicht, wodurch die Wärmeübergangszahlen verbessert werden, was letztlich dazu führt, daß das Blockvolumen des Wärmetauschers verringert werden kann. Bei gleichem Druckabfall im Wärmetauscherblock ermöglicht das erfindungsgemäße Verfahren gegenüber den bekannten Verfahren eine Reduktion der Blockvolumina um etwa 15%, woraus eine beträchtliche Kosteneinsparung resultiert.Preferably, the gas stream is passed through the heat exchanger blocks so that it suffers a pressure drop of 120 to 300 mbar, preferably 120 to 200 mbar. By Raising the pressure drop will result in a greater flow rate than in the conventional heat exchangers achieved, reducing the heat transfer coefficients be improved, which ultimately leads to the block volume of the Heat exchanger can be reduced. At the same pressure drop in Heat exchanger block enables the inventive method compared to the known methods a reduction in block volumes by about 15%, resulting in a considerable cost savings result.

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

Figur 1
die Anordnung und Ausführung der Hauptwärmetauscherblöcke einer großen Luftzerlegungsanlage mit mehreren Hauptwärmetauscherblöcken gemäß dem Stand der Technik,
Figur 2
die erfindungsgemäße Konfiguration der Hauptwärmetauscherblöcke einer großen Luftzerlegungsanlage,
Figuren 3 bis 6
die herkömmliche Anordnung der Lamellen im Ein- und Austrittsbereich der Wärmeaustauschpassagen,
Figuren 7 und 8
die erfindungsgemäßen Sammler/Verteiler im Ein- und Austrittsbereich der Wärmeaustauschpassagen,
Figur 9
ein erfindungsgemäßes Verfahren mit Sauerstoff- und Stickstoffinnenverdichtung,
Figur 10
ein erfindungsgemäßes Verfahren mit Sauerstoffinnenverdichtung und
Figur 11
ein Luftzerlegungsverfahren mit Stickstoffkreislauf.
The invention and further details of the invention are explained in more detail below with reference to exemplary embodiments shown in the drawings. Here show:
Figure 1
the arrangement and design of the main heat exchanger blocks of a large air separation plant with several main heat exchanger blocks according to the prior art,
Figure 2
the inventive configuration of the main heat exchanger blocks of a large air separation plant,
Figures 3 to 6
the conventional arrangement of the fins in the entry and exit area of the heat exchange passages,
Figures 7 and 8
the collectors / distributors according to the invention in the entry and exit area of the heat exchange passages,
Figure 9
a method according to the invention with internal oxygen and nitrogen compression,
Figure 10
an inventive method with internal oxygen compression and
Figure 11
an air separation process with a nitrogen cycle.

Figur 1 zeigt ein aus dem Stand der Technik bekanntes Verfahrensschema einer großen Luftzerlegungsanlage zur verarbeitung von etwa 100.000 Nm3/h Luft, bei der es notwendig ist, den Hauptwärmetauscher durch mehrere separate Wärmetauscherblöcke 3 zu realisieren.Figure 1 shows a process scheme known from the prior art of a large air separation plant for processing about 100,000 Nm 3 / h of air, in which it is necessary to implement the main heat exchanger by means of several separate heat exchanger blocks 3.

Verdichtete und gereinigte Einsatzluft 1 wird zum Teil 2 direkt mehreren parallel zueinander angeordneten Wärmetauscherblöcken 3a - 3e zugeführt, zum Teil 4 mittels eines Verdichters 5 nachverdichtet, in einem Nachkühler 6 gekühlt und dann in die Wärmetauscherblöcke 3a - 3e geleitet. Diese im folgenden als Turbinenluftstrom 7 bezeichnete Druckluft wird an einer Zwischenstelle den Wärmetauscherblöcken 3a - 3e entnommen, in einer Turbine 8 entspannt und in die Niederdrucksäule 10 einer Rektifikationseinheit 11, welche eine Drucksäule 9 und eine Niederdrucksäule 10 umfaßt, eingeleitet.Compressed and cleaned feed air 1 becomes part 2 directly several in parallel mutually arranged heat exchanger blocks 3a - 3e supplied, in part 4 by means of of a compressor 5 post-compressed, cooled in an after-cooler 6 and then into the Heat exchanger blocks 3a - 3e directed. This in the following as turbine air flow 7 designated compressed air is at an intermediate point the heat exchanger blocks 3a - 3e removed, relaxed in a turbine 8 and one in the low pressure column 10 Rectification unit 11, which has a pressure column 9 and a low pressure column 10 includes, initiated.

Die Wärmetauscherblöcke 3a - 3e bilden den Hauptwärmetauscher der Luftzerlegungsanlage. Die in den Blöcken 3a - 3 e abgekühlte Einsatzluft 2 wird der Drucksäule 9 der Rektifikationseinheit 11 zugeführt. Der Niederdrucksäule 10 werden gasförmiger Sauerstoff 14, gasförmiger Stickstoff 15 sowie gasförmiger UnreinStickstoff 16 als Regeneriergas mit einem Druck von etwa 1,3 bar entnommen. Ferner ist es möglich, in der Rektifikationseinheit 11 Sauerstoff und Stickstoff als flüssige Produkte 12, 13 zu gewinnen. Die Gasströme 14, 15, 16 werden in jeden der Wärmetauscherblöcke 3a - 3e geführt und gegen den Einsatzluftstrom 2 und den Turbinenluftstrom 7 durch indirekten Wärmeaustausch angewärmt.The heat exchanger blocks 3a - 3e form the main heat exchanger of the Air separation plant. The supply air 2 cooled in blocks 3a - 3e becomes the Pressure column 9 of the rectification unit 11 supplied. The low pressure column 10 will gaseous oxygen 14, gaseous nitrogen 15 and gaseous impure nitrogen 16 taken as regeneration gas at a pressure of about 1.3 bar. Further it is possible to use oxygen and nitrogen as liquid in the rectification unit 11 Products 12, 13 to win. The gas streams 14, 15, 16 are in each of the Heat exchanger blocks 3a - 3e guided and against the feed air flow 2 and Turbine airflow 7 warmed by indirect heat exchange.

Da durch jeden der Wärmetauscherblöcke 3a - 3e alle gasförmigen Ströme 14, 15, 16 sowie im Gegenstrom die beiden Luftströme 2, 7, d.h. insgesamt fünf verschiedene Ströme, geleitet werden, sind pro Wärmetauscherblock 3 zehn Sammler/Verteiler mit den dazugehörigen Ein- bzw. Austrittsstutzen notwendig, über die jeweils die Verbindung zwischen dem Zu- bzw. Ableitungsrohr und der entsprechenden Wärmeaustauschpassage hergestellt wird.Since all of the gaseous streams 14, 15, 16. Through each of the heat exchanger blocks 3a - 3e as well as in counterflow the two air flows 2, 7, i.e. a total of five different ones Currents that are conducted are ten heat collectors / distributors with each heat exchanger block the associated inlet and outlet connection necessary, via which the Connection between the supply or discharge pipe and the corresponding Heat exchange passage is established.

In Figur 2 ist ein Figur 1 entsprechendes Verfahrensschema dargestellt, wobei jedoch, im Gegensatz zu dem in Figur 1 gezeigten bekannten Verfahren, die Wärmetauscherblöcke 3 erfindungsgemäß nach Produkten aufgeteilt sind. Der Luftstrom 2 und der Turbinenluft 7 werden ebenso wie bei dem Verfahren gemäß Figur 1 allen Wärmetauscherblöcken 23a - 23e zugeführt. Dagegen werden die gasförmigen Gasströme 14, 15, 16 nicht mehr in allen Wärmetauscherblöcken 23, sondern in jeweils speziell den Gasströmen 14, 15, 16 zugeordneten Blöcken 23 angewärmt.A method diagram corresponding to FIG. 1 is shown in FIG. in contrast to the known method shown in Figure 1, the Heat exchanger blocks 3 are divided according to the invention according to products. The Air flow 2 and the turbine air 7 are the same as in the method according to FIG 1 supplied to all heat exchanger blocks 23a - 23e. In contrast, the gaseous Gas flows 14, 15, 16 no longer in all heat exchanger blocks 23, but in in each case specifically heated to the gas streams 14, 15, 16 blocks 23.

Jeweils etwa 20% der insgesamt zugeführten Luft 1 werden in der Rektifikationseinheit 11 durch Tieftemperaturzerlegung der Luft 1 in gasförmigen Sauerstoff 14 und UnreinStickstoff 16 umgesetzt. Die verbleibenden 60 % der Luft 1 werden als gasförmiger Reinstickstoff 15 aus der Rektifikationseinheit 11 abgezogen. Die Wärmetauscherblöcke 23 sind so bemessen, daß sich für den gasförmigen Sauerstoffstrom 14 und den Unreinstickstoffstrom 16 jeweils Blöcke 23a, 23e mit Maximalabmessungen ergeben, d.h. die Blöcke 23a und 23e sind genau auf die erwarteten Sauerstoff- bzw. Stickstoffmengen ausgelegt. Aus herstellungstechnischen Gründen werden alle Blöcke 23a - 23e mit identischer Größe ausgeführt, sodaß für den Reinstickstoffstrom 15 drei Wärmetauscherblöcke 23b - 23d benötigt werden.About 20% of the total air 1 supplied is in the rectification unit 11 by low-temperature decomposition of air 1 into gaseous oxygen 14 and impure nitrogen 16 implemented. The remaining 60% of air 1 are considered gaseous Pure nitrogen 15 is withdrawn from the rectification unit 11. The Heat exchanger blocks 23 are dimensioned so that the gaseous Oxygen stream 14 and the impure nitrogen stream 16 each have blocks 23a, 23e Result in maximum dimensions, i.e. blocks 23a and 23e are exactly on that expected oxygen or nitrogen amounts. From manufacturing technology For this reason, all blocks 23a-23e are executed with the same size, so that for the pure nitrogen flow 15, three heat exchanger blocks 23b-23d are required.

Durch den Wärmetauscherblock 23a wird somit lediglich Sauerstoff 14 gegen die Luftströme 2 und 7 geführt, durch die Blöcke 23b bis 23d Reinstickstoff 15 gegen Luft 2, 7 und durch den Wärmetauscherblock 23e Unreinstickstoff 16 gegen Luft 2, 7. Die Anzahl der Wärmetauscherblöcke 23 bleibt somit gegenüber dem Verfahren nach Figur 1 gleich, da bei beiden Verfahren dieselben Produktmengen mit denselben Luftmengen ihre Wärme austauschen müssen.The heat exchanger block 23a thus only oxygen 14 against the Air flows 2 and 7 guided through the blocks 23b to 23d pure nitrogen 15 against air 2, 7 and by the heat exchanger block 23e impure nitrogen 16 against air 2, 7. Die The number of heat exchanger blocks 23 thus remains in relation to the method Figure 1 the same, since the same product quantities with the same in both methods Air volumes have to exchange their heat.

Die Blockkonfiguration vereinfacht sich jedoch wesentlich. Jedem Wärmetauscherblock 23 werden nur noch drei Ströme, zwei Luftströme 2, 7 und ein Gasstrom 14, 15 oder 16, zugeführt, wodurch jeder Block 23 lediglich sechs Sammler/Verteiler mit den entsprechenden Anschlußstutzen benötigt.However, the block configuration is simplified considerably. Every heat exchanger block 23 are only three streams, two air streams 2, 7 and a gas stream 14, 15 or 16, supplied, whereby each block 23 only six collectors / distributors with the appropriate connection piece required.

Die Wärmeaustauscherblöcke 23 werden erfindungsgemäß entsprechend den Figuren 7 und 8 ausgeführt. Zum Vergleich ist in den Figuren 3 bis 6 der Aufbau eines Wärmetauscherblocks 3 der bisher üblichen Art dargestellt. Figur 3 zeigt die Lamellenanordnung in den Verteilzonen 31 für die Sauerstoffpassagen 34, Figur 4 für die Reinstickstoffpassagen 35 und Figur 5 entsprechend für die Unreinstickstoffpassagen 36. In Figur 6 ist die Anordnung aller Ein- und Austrittsstutzen zu sehen.According to the invention, the heat exchanger blocks 23 are in accordance with the figures 7 and 8 executed. For comparison, the structure of a Heat exchanger blocks 3 shown the usual way. Figure 3 shows the Lamella arrangement in the distribution zones 31 for the oxygen passages 34, Figure 4 for the pure nitrogen passages 35 and Figure 5 accordingly for the Impure nitrogen passages 36. In Figure 6, the arrangement of all inputs and Outlet nozzle to see.

Bei dem Verfahren gemäß Figur 1 werden in dem Wärmetauscherblock 3 drei unterschiedliche Produkte 14, 15, 16 gegen den Luftstrom 2 und den Turbinenluftstrom 7 geführt. Die Verteilung des jeweiligen gasförmigen Produktes auf die entsprechenden Wärmeaustauschpassagen 34, 35, 36 erfolgt über Verteilzonen 31, 32, 33, die schräg angeordnete Lamellen aufweisen, um das Gas 14, 15, 16 aus der Zufuhrleitung 37a, 38a, 39a auf die Passagen 31, 32, 33 zu verteilen beziehungsweise um das aus den Passagen 31, 32, 33 austretende Gas in die Abzugsleitung 37b, 38b, 39b zusammenzuführen. In the method according to FIG. 1, three are in the heat exchanger block 3 different products 14, 15, 16 against the air flow 2 and the turbine air flow 7 led. The distribution of the respective gaseous product on the corresponding Heat exchange passages 34, 35, 36 take place via distribution zones 31, 32, 33, which are inclined arranged slats to the gas 14, 15, 16 from the supply line 37a, 38a, 39a to distribute the passages 31, 32, 33 or in order to Passages 31, 32, 33 escaping gas into the exhaust line 37b, 38b, 39b merge.

Die Verteilzonen 31, 32, 33 führen sowohl zu einer Änderung der Strömungsrichtung als auch zu Querschnittsveränderungen, welche wiederum Änderungen der Strömungsgeschwindigkeit verursachen. Beides wirkt sich negativ auf die Blockdurchströmung aus und erzeugt einen unerwünschten Druckabfall über dem Wärmetauscherblock 3. Der Druckabfall wirkt sich insbesondere bei den Gasströmen, die einen relativ niedrigen Druck zwischen 1,1 und 1,8 bar besitzen, negativ aus. Auch eine Vertauschung der Passagen 34, 35, 36 für die Gasströme 14, 15, 16 mit denen für die Luft 2 oder die Turbinenluft 7, welche seitlich angeordnete Ein- und Austrittsstutzen 40a, 40b, 41a, 41b besitzen (siehe Figur 6), bringt keine Verbesserung, da die Verteilung der Luft 2, 7 auf die zugehörigen Wärmeaustauschpassagen über ähnliche Verteilpassagen, wie die in den Figuren 3 bis 5 dargestellten, erfolgt und damit ähnliche Strömungsknicke und Querschnittsänderungen auftreten.The distribution zones 31, 32, 33 both lead to a change in the direction of flow as well as cross-sectional changes, which in turn changes the Cause flow velocity. Both have a negative impact on the Block flow and creates an undesirable pressure drop across the Heat exchanger block 3. The pressure drop affects in particular the gas flows, which have a relatively low pressure between 1.1 and 1.8 bar. Also an exchange of the passages 34, 35, 36 for the gas streams 14, 15, 16 with those for the air 2 or the turbine air 7, which laterally arranged inlet and outlet ports 40a, 40b, 41a, 41b (see Figure 6), brings no improvement, since the Distribution of air 2, 7 over the associated heat exchange passages via similar Distribution passages, such as those shown in Figures 3 to 5, takes place and thus Similar flow kinks and cross-sectional changes occur.

Die Figuren 7 und 8 zeigen die neue Blockkonfiguration. Ein Hauptmerkmal des erfindungsgemäßen Verfahrens liegt darin, daß in jedem Wärmetauscherblock 23 nur noch einer der Gasströme 14, 15, 16 im Gegenstrom mit Luft 2, 7 geführt wird. Mit den Stirnflächen des Wärmetauscherblocks 23 werden Sammler/Verteiler 43, auch als Domheader bezeichnet, als Ein- und Austritte für den jeweiligen Gasstrom 14, 15, 16 verbunden. Die Sammler/Verteiler 43 sind halbzylindrisch ausgeführt und besitzen einen Anschlußstutzen für die Produktzu- bzw. -ableitung. Der in den neuen Wärmetauscherblock 23 eingeleitete Gasstrom erfährt keinerlei Querschnittsveränderung und keine wesentliche Stromrichtungsänderung. Der Druckabfall über dem Wärmetauscherblock 23 ist gegenüber dem Druckabfall über einem üblichen Block 3, wie er anhand der Figuren 3 bis 6 erläutert wurde, um etwa 30% verringert. Ferner werden die Kosten für die Wärmetauscherblöcke 23 reduziert, da auf die aufwendigen Lamellenzuschnitte für die Verteilzonen 32 in den Figuren 3 bis 5 verzichtet werden kann.Figures 7 and 8 show the new block configuration. A key feature of the The inventive method is that in each heat exchanger block 23 only one of the gas streams 14, 15, 16 is guided in countercurrent with air 2, 7. With the End faces of the heat exchanger block 23 become collectors / distributors 43, also as Dome headers are referred to as inlets and outlets for the respective gas stream 14, 15, 16 connected. The collectors / distributors 43 are semi-cylindrical and have a connecting piece for the product feed or discharge. The one in the new Heat exchanger block 23 introduced gas flow does not experience anything Cross-sectional change and no significant change in current direction. The Pressure drop across the heat exchanger block 23 is greater than the pressure drop a usual block 3, as it was explained with reference to FIGS. 3 to 6, by approximately 30% reduced. Furthermore, the costs for the heat exchanger blocks 23 are reduced, since on the elaborate lamella cuts for the distribution zones 32 in Figures 3 to 5 can be dispensed with.

Anstelle der aufwendigen Verteilzonen 32 mit schrägen Lamellen in den bekannten Wärmetauscherblöcken (siehe Figuren 3 bis 5) ist bei den neuen Wärmetauscherblöcken bevorzugt lediglich eine schmale Verteilzone 42 am Eintritts- und Austrittsbereich der Wärmeaustauschpassagen vorgesehen. Die Lamellen in der schmalen Verteilzone 42 sind parallel zu den darunter bzw. darüberliegenden Lamellen der Wärmeaustauschpassagen angeordnet, besitzen jedoch einen geringeren Abstand voneinander. Das in den Sammler 41 eintretende Gas staut sich dadurch leicht vor der Verteilzone 42, wodurch eine gleichmäßige Verteilung des Gases auf alle Passagen der Verteilzone 42 und damit auf alle Wärmeaustauschpassagen erreicht wird.Instead of the complex distribution zones 32 with oblique lamellae in the known Heat exchanger blocks (see Figures 3 to 5) is in the new Heat exchanger blocks preferably only have a narrow distribution zone 42 at the inlet and exit area of the heat exchange passages are provided. The slats in the narrow distribution zone 42 are parallel to the slats below or above the heat exchange passages are arranged, but have a smaller distance from each other. As a result, the gas entering the collector 41 easily builds up in front of the Distribution zone 42, which ensures an even distribution of the gas over all passages the distribution zone 42 and thus is reached on all heat exchange passages.

Anhand der Figuren 1 und 2 wird ein weiterer Vorteil des erfindungsgemäßen Verfahrens deutlich. Zusätzlich zu dem deutlich verringerten Druckabfall über den Wärmertauscherblöcken 23 stellt sich bei dem neuen Verfahren die Verrohrung wesentlich einfacher dar. Neben der Reduzierung der Blockstutzenzahl von zehn auf sechs pro Wärmetauscherblock sind auch weniger Sammelleitungen und Rohrverzeigungen notwendig, um die Gasströme 14, 15, 16 den Blöcken 23 zuzuführen.Another advantage of the invention is shown in FIGS Procedure clearly. In addition to the significantly reduced pressure drop across the Heat exchanger blocks 23 are the piping in the new process much easier. In addition to reducing the number of block sockets from ten to six per heat exchanger block are also fewer manifolds and Pipe bends necessary to block the gas flows 14, 15, 16 feed.

In Figur 1 ist zu erkennen, daß beispielsweise von der Stickstoffproduktleitung 15 vier Rohrverzweigungen 17a -17d abgehen, um den Stickstoff auf die fünf Wärmetauscherblöcke 3 zu verteilen. Umgekehrt sind vier Rohrverzeigungen 18a - 18d notwendig, um den angewärmten Stickstoff wieder in die Sammelleitung 19 zusammenzuführen. Für jeden der fünf durch die Wärmetauscherblöcke geleiteten Ströme müssen somit acht Rohrverzweigungen vorgesehen werden, insgesamt also 40 Rohrverzweigungen beziehungsweise Rohrvereinigungen.It can be seen in FIG. 1 that, for example, four of the nitrogen product line 15 Pipe branches 17a-17d go off to the nitrogen on the five Distribute heat exchanger blocks 3. Conversely, four pipe branches 18a - 18d necessary to return the heated nitrogen to the manifold 19 merge. For each of the five routed through the heat exchanger blocks Streams must therefore be provided for eight pipe branches, in total 40 pipe branches or pipe unions.

Im Gegensatz dazu werden bei dem erfindungsgemäßen Verfahren gemäß Figur 2 lediglich der Luftstrom 2 und der Turbinenluftstrom 7 auf alle fünf Wärmetauscherblöcke 23 verteilt, wofür entsprechend 16 Rohrverzweigungen notwendig sind. Hierzu kommen zwei Verzweigungen 20a, b und zwei Rohrvereinigungen 21a, b zur Verteilung des Stickstoffstromes 15 auf die Blöcke 23b, c, e und anschließenden Zusammenführung in die Abzugsleitung 19.In contrast, in the method according to the invention according to FIG. 2 only airflow 2 and turbine airflow 7 on all five Distributed heat exchanger blocks 23, for which purpose 16 pipe branches are necessary. In addition there are two branches 20a, b and two Pipe assemblies 21a, b for distributing the nitrogen stream 15 to the blocks 23b, c, e and subsequent merging into the discharge line 19.

Bei dem erfindungsgemäßen Verfahren stehen an Verrohrungsaufwand insgesamt 20 Verzweigungen einem Aufwand von 40 Verzweigungen bei dem herkömmlichen Verfahren gemäß Figur 1 gegenüber. Diese Reduktion um 50% ist ein deutlicher Beleg für die Vereinfachung der Verrohrungskomplexität.In the method according to the invention, there is a total of 20 piping costs Branches an effort of 40 branches in the conventional The method according to FIG. 1 compared. This 50% reduction is clear evidence to simplify piping complexity.

Das erfindungsgemäße Verfahren ist nicht nur auf solche Prozesse beschränkt, bei denen alle Produkte gasförmig gewonnen werden, sondern beispielsweise auch auf Innenverdichtungsverfahren, bei denen Flüssigprodukte aus der Rektifikationseinheit abgezogen werden. The method according to the invention is not restricted to such processes only where all products are obtained in gaseous form, but also, for example Internal compression processes in which liquid products from the rectification unit subtracted from.

Figur 9 zeigt das Schema eines Luftzerlegungsverfahrens, bei dem neben gasförmigem Reinstickstoff 15 und gasförmigem Unreinstickstoff 16 flüssiger Stickstoff 51 aus dem Hauptkondensator der Rektifikationseinheit 11 entnommen und mittels einer Innenverdichtungspumpe 52 auf erhöhten Druck gebracht wird. Der flüssige und auf erhöhten Druck gebrachte Stickstoff 51 wird dann im Wärmetauscherblock 56 gegen Luft 7 und mittels des Verdichters 59 komprimierte Hochdruckluft verdampft und erwärmt.Figure 9 shows the scheme of an air separation process in which in addition gaseous pure nitrogen 15 and gaseous impure nitrogen 16 liquid nitrogen 51 removed from the main capacitor of the rectification unit 11 and by means of an internal compression pump 52 is brought to increased pressure. The liquid and Nitrogen 51 brought to increased pressure is then in the heat exchanger block 56 against air 7 and compressed by the compressor 59 high pressure air evaporates and warmed up.

Der Sauerstoff 12 wird bei diesem Verfahren ebenfalls in flüssiger Form aus der Niederdrucksäule 10 abgezogen und mit Hilfe der beiden Pumpen 54 und 55 innenverdichtet. Der Reinstickstoffstrom 15 und der Unreinstickstoffstrom 16 werden in den Wärmetauscherblöcken 23b, c, d bzw. dem Block 23e, die jeweils entsprechend den Figuren 7 und 8 aufgebaut sind, erwärmt. Zur Verdampfung und Erwärmung der innenverdichteten Ströme 57, 58 findet dagegen ein Hochdruckwärmetauscherblock 56 Anwendung. Der Hochdruckwärmetauscherblock 56 entspricht auf den ersten Blick dem anhand der Figuren 3 bis 6 erläuterteten Wärmetauscherblock, besitzt jedoch eine deutlich höhere Festigkeit, um den hohen Drücken der Innenverdichtungsströme standhalten zu können. Die in dem Wärmetauscherblock 56 auftretenden Druckverluste wirken sich bei den Innenverdichtungsströmen 57, 58 weitaus weniger negativ aus als bei den gasförmigen Gasströmen 15, 16 aus der Niederdrucksäule 10.The oxygen 12 is also in liquid form from the Low pressure column 10 is withdrawn and using the two pumps 54 and 55 internally compressed. The pure nitrogen stream 15 and the impure nitrogen stream 16 are in the heat exchanger blocks 23b, c, d and block 23e, respectively, respectively 7 and 8 are constructed, heated. For evaporation and heating of the on the other hand, internally compressed streams 57, 58 find a high-pressure heat exchanger block 56 Application. The high-pressure heat exchanger block 56 corresponds at first glance the heat exchanger block explained with reference to Figures 3 to 6, but has one significantly higher strength to withstand the high pressures of internal compression flows to be able to withstand. Those occurring in the heat exchanger block 56 Pressure losses have a far less effect on the internal compression flows 57, 58 negative than in the gaseous gas streams 15, 16 from the low pressure column 10.

Ein ähnliches Verfahren wie in Figur 9 ist in Figur 10 dargestellt, bei dem ebenfalls flüssiger Sauerstoff 12 innenverdichtet wird 54, 55, jedoch nicht gegen Hochdruckluft, sondern gegen Hochdruckstickstoff verdampft und erwärmt wird. Hierzu wird der Drucksäule 9 gasförmiger Stickstoff bei 61 entnommen, durch den Wärmetauscherblock 62 geführt, mittels des Verdichters 63 verdichtet und im Gegenstrom durch den Wärmetauscherblock 62 zurück in die Drucksäule 9 geleitet. Der Wärmetauscherblock 62 entspricht in seinem Aufbau im wesentlichen dem Wärmetauscherblock 56 in Figur 9. Eine Innenverdichtung von Stickstoff entfällt bei dieser Variante, da nach dem Verdichter 63 Hochdruckstickstoff 64 abgezogen werden kann.A method similar to that in FIG. 9 is shown in FIG. 10, in which likewise liquid oxygen 12 is internally compressed 54, 55, but not against high pressure air, but is vaporized and heated against high pressure nitrogen. For this, the Pressure column 9 removed gaseous nitrogen at 61 through which Heat exchanger block 62 out, compressed by means of the compressor 63 and in Countercurrent passed through the heat exchanger block 62 back into the pressure column 9. The construction of the heat exchanger block 62 corresponds essentially to that Heat exchanger block 56 in FIG. 9. There is no internal compression of nitrogen this variant, since 63 high-pressure nitrogen 64 are drawn off after the compressor can.

Figur 11 zeigt eine weitere Anwendung des erfindungsgemäßen Verfahrens. Hierbei wird flüssiger Sauerstoff bei 12 der Rektifikationssäule 11 entnommen und mittels der beiden Pumpen 54, 55 innenverdichtet. Die Verdampfung des Flüssigsauerstoffs erfolgt in diesem Ausführungsbeispiel gegen Kreislaufstickstoff, der bei 61 aus der Drucksäule 9 abgezogen, im Wärmetauscherblock 77 angewärmt, mit den Verdichtern 71, 72, 73 verdichtet und im Wärmetauscherblock 77 gegen die Innenverdichtungsprodukte abgekühlt und in die Drucksäule 9 geleitet wird 76. Ein Teil des Stickstoffs wird nach dem Verdichter 71 entspannt (74) und in den Stickstoffkreislauf zurückgeführt. Ein weiterer Teil des Stickstoffs wird nach Verdichtung in den Verdichtern 71, 72, 73 und anschließender Abkühlung im Wärmetauscherblock 77 an einer Zwischenstelle aus dem Wärmetauscherblock 77 abgezogen, bei 75 entspannt und in den Stickstoffkreislauf zurückgeleitet.FIG. 11 shows a further application of the method according to the invention. Here liquid oxygen is removed from the rectification column 11 at 12 and by means of the two pumps 54, 55 internally compressed. The evaporation of liquid oxygen takes place in this embodiment against circulating nitrogen, which at 61 from the Pressure column 9 removed, warmed in the heat exchanger block 77, with the compressors 71, 72, 73 compressed and in the heat exchanger block 77 against the Internal compression products cooled and passed into the pressure column 9 76. A part of the nitrogen is expanded after the compressor 71 (74) and into the Nitrogen cycle returned. Another part of the nitrogen is released Compression in compressors 71, 72, 73 and subsequent cooling in Heat exchanger block 77 at an intermediate point from the heat exchanger block 77 deducted, relaxed at 75 and returned to the nitrogen cycle.

Claims (12)

Verfahren zum indirekten Wärmeaustausch von mehreren Gasströmen mit einem Wärme-/Kälteträger in Wärmetauscherblöcken, in denen die Gasströme durch eine Vielzahl von Wärmeaustauschpassagen geleitet werden, wobei durch mindestens einen Wärmetauscherblock nur einer der Gasströme geleitet wird, dadurch gekennzeichnet, daß die Wärmeaustauschpassagen für den einen Gasstrom (14, 15, 16) des mindestens einen Wärmetauscherblocks (23a, b, c, d, e) an zwei Stirnflächen des Wärmetauscherblocks (23a, b, c, d, e) enden und der eine Gasstrom (14, 15, 16) den Wärmeaustauschpassagen des mindestens einen Wärmetauscherblocks (23a, b, c, d, e) über jeweils einen mit dem Wärmetauscherblock (23a, b, c, d, e) verbundenen Sammler/Verteiler (41) zugeführt und entnommen wird, welcher sich jeweils über die gesamte Stirnfläche des Wärmetauscherblocks (23a, b, c, d, e) erstreckt.Process for the indirect heat exchange of several gas streams with a heat / coolant in heat exchanger blocks, in which the gas streams are passed through a plurality of heat exchange passages, only one of the gas streams being passed through at least one heat exchanger block, characterized in that the heat exchange passages for the one gas stream (14, 15, 16) of the at least one heat exchanger block (23a, b, c, d, e) end at two end faces of the heat exchanger block (23a, b, c, d, e) and the one gas stream (14, 15, 16) the heat exchange passages of the at least one heat exchanger block (23a, b, c, d, e) are supplied and removed via a respective collector / distributor (41) connected to the heat exchanger block (23a, b, c, d, e), which is in each case via the entire end face of the heat exchanger block (23a, b, c, d, e) extends. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß jeder der Gasströme (14, 15, 169 durch einen separaten Wärmetauscherblock (23a, b, c, d, e) geleitet wird.Method according to claim 1, characterized in that each of the gas streams (14, 15, 169) is passed through a separate heat exchanger block (23a, b, c, d, e). Verfahren nach einem der Ansprüche 1 oder 2, dadurch gekennzeichnet, daß der eine Gasstrom (14, 15, 16) mit einem Druck von weniger als 3,5 bar, vorzugsweise 1,1 bis 1,8 bar, durch den Wärmetauscherblock (23a, b, c, d, e) geleitet wird.Method according to one of claims 1 or 2, characterized in that the one gas stream (14, 15, 16) with a pressure of less than 3.5 bar, preferably 1.1 to 1.8 bar, through the heat exchanger block (23a, b, c, d, e) is conducted. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die Gasströme (14, 15, 16) jeweils einen Druck von weniger als 3,5 bar, bevorzugt zwischen 1,1 und 1,8 bar, aufweisen.Method according to one of claims 1 to 3, characterized in that the gas streams (14, 15, 16) each have a pressure of less than 3.5 bar, preferably between 1.1 and 1.8 bar. Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß ein weiterer Strom mit einem Druck von mehr als 4 bar durch den mindestens einen Wärmetauscherblock geleitet wird.A method according to claim 4, characterized in that a further stream with a pressure of more than 4 bar is passed through the at least one heat exchanger block. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß die Gasströme durch Tieftemperaturzerlegung von Einsatzluft (1) gewonnen werden. Method according to one of claims 1 to 5, characterized in that the gas streams are obtained by low-temperature separation of feed air (1). Verfahren nach Anspruch 6, dadurch gekennzeichnet, daß die Gasströme (14, 15, 16) mit der Einsatzluft (2, 7) in indirekten Wärmeaustausch gebracht werden.Method according to claim 6, characterized in that the gas streams (14, 15, 16) are brought into indirect heat exchange with the feed air (2, 7). Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß der eine Gasstrom so durch den Wärmetauscherblock (23a, b, c, d, e) geleitet wird, daß der Druckabfall im Wärmetauscherblock (23a, b, c, d, e) weniger als 100 mbar, bevorzugt weniger als 80 mbar beträgt.Method according to one of claims 1 to 7, characterized in that the one gas stream is passed through the heat exchanger block (23a, b, c, d, e) in such a way that the pressure drop in the heat exchanger block (23a, b, c, d, e) is less than 100 mbar, preferably less than 80 mbar. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß der eine Gasstrom (14, 15, 16) so durch den Wärmetauscherblock (23a, b, c, d, e) geleitet wird, daß der Druckabfall im Wärmetauscherblock zwischen 80 und 300 mbar, bevorzugt zwischen 100 und 250 mbar beträgt.Method according to one of claims 1 to 8, characterized in that the one gas stream (14, 15, 16) is passed through the heat exchanger block (23a, b, c, d, e) such that the pressure drop in the heat exchanger block is between 80 and 300 mbar, preferably between 100 and 250 mbar. Verfahren nach einem der Ansprüche 7 bis 9, dadurch gekennzeichnet, daß mehr als 50.000 Nm3/h Einsatzluft, bevorzugt mehr als 100.000 Nm3/h Einsatzluft verarbeitet werden.Method according to one of claims 7 to 9, characterized in that more than 50,000 Nm 3 / h feed air, preferably more than 100,000 Nm 3 / h feed air, are processed. Wärmeaustauschvorrichtung zum indirekten Wärmeaustausch von mindestens zwei Gasströmen mit einem Wärme-/Kälteträger in Wärmetauscherblöcken, welche eine Vielzahl von Wärmeaustauschpassagen besitzen, dadurch gekennzeichnet, daß die Wärmeaustauschpassagen eines Wärmetauscherblocks (23a, b, c, d, e), die für einen der Gasströme (14, 154, 16) vorgesehen sind, an zwei gegenüberliegenden Stirnflächen des Wärmetauscherblocks (23a, b, c, d, e) enden und jeweils mit einem Sammler/Verteiler (41) in Strömungsverbindung stehen, wobei sich die Sammler/Verteiler jeweils über die gesamte Stirnfläche des Wärmetauscherblocks (23a, b, c, d, e) erstrecken.Heat exchange device for the indirect heat exchange of at least two gas streams with a heat / coolant in heat exchanger blocks which have a plurality of heat exchange passages, characterized in that the heat exchange passages of a heat exchanger block (23a, b, c, d, e) which are necessary for one of the gas streams ( 14, 154, 16) are provided, end at two opposite end faces of the heat exchanger block (23a, b, c, d, e) and are each in flow connection with a collector / distributor (41), the collectors / distributors in each case via the extend the entire end face of the heat exchanger block (23a, b, c, d, e). Wärmeaustauschvorrichtung nach Anspruch 11, dadurch gekennzeichnet, daß der Sammler/Verteiler (41) im wesentlichen halbzylindrisch ausgebildet ist und einen Anschlußstutzen aufweist.Heat exchange device according to claim 11, characterized in that the collector / distributor (41) is essentially semi-cylindrical and has a connecting piece.
EP00115776A 2000-04-28 2000-07-21 Method and apparatus for heat exchange Withdrawn EP1150082A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10021081A DE10021081A1 (en) 2000-04-28 2000-04-28 Heat exchange method and apparatus
DE10021081 2000-04-28

Publications (1)

Publication Number Publication Date
EP1150082A1 true EP1150082A1 (en) 2001-10-31

Family

ID=7640352

Family Applications (1)

Application Number Title Priority Date Filing Date
EP00115776A Withdrawn EP1150082A1 (en) 2000-04-28 2000-07-21 Method and apparatus for heat exchange

Country Status (6)

Country Link
US (1) US6629433B2 (en)
EP (1) EP1150082A1 (en)
JP (1) JP2001355963A (en)
KR (1) KR20010098779A (en)
CN (1) CN1202400C (en)
DE (1) DE10021081A1 (en)

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2867262A1 (en) * 2004-03-02 2005-09-09 Air Liquide Separation of air by cryogenic distillation and installation using thermally interconnected medium and low pressure columns
WO2005085728A1 (en) * 2004-03-02 2005-09-15 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Cryogenic distillation method for air separation and installation used to implement same
DE102007031759A1 (en) 2007-07-07 2009-01-08 Linde Ag Method and apparatus for producing gaseous pressure product by cryogenic separation of air
DE102007031765A1 (en) 2007-07-07 2009-01-08 Linde Ag Process for the cryogenic separation of air
DE102009034979A1 (en) 2009-04-28 2010-11-04 Linde Aktiengesellschaft Method for producing pressurized oxygen by evaporating liquid oxygen using a copper and nickel heat exchanger block
EP2312248A1 (en) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Method and device for obtaining pressurised oxygen and krypton/xenon
EP2458311A1 (en) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
DE102010052544A1 (en) 2010-11-25 2012-05-31 Linde Ag Process for obtaining a gaseous product by cryogenic separation of air
EP2520886A1 (en) 2011-05-05 2012-11-07 Linde AG Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air
EP2568242A1 (en) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Method and device for generating of steel
EP2600090A1 (en) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Method and device for generating pressurised oxygen by cryogenic decomposition of air
DE102011121314A1 (en) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator
DE102013017590A1 (en) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer
DE102012017488A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements
EP2784420A1 (en) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Method for air separation and air separation plant
WO2014154339A2 (en) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Method for air separation and air separation plant
EP2801777A1 (en) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Air separation plant with main compressor drive
EP2963370A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
EP2963367A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for cryogenic air separation with variable power consumption
EP2963371A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for creating a pressurised gas product by the cryogenic decomposition of air
EP2963369A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
EP3006875A1 (en) 2014-10-09 2016-04-13 Linde Aktiengesellschaft Method for regulating a coupled heat exchanger system and heat exchanger system
WO2018206886A1 (en) * 2017-05-11 2018-11-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchange apparatus

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7188492B2 (en) * 2002-01-18 2007-03-13 Linde Aktiengesellschaft Plate heat exchanger
JP4820721B2 (en) * 2006-09-07 2011-11-24 オリオン機械株式会社 Chemical heat exchanger
US9222725B2 (en) * 2007-06-15 2015-12-29 Praxair Technology, Inc. Air separation method and apparatus
EP2236964B1 (en) * 2009-03-24 2019-11-20 Linde AG Method and device for low-temperature air separation
US8397535B2 (en) * 2009-06-16 2013-03-19 Praxair Technology, Inc. Method and apparatus for pressurized product production
DE102009040561A1 (en) 2009-09-08 2011-03-10 Linde Aktiengesellschaft Heat exchanger e.g. direct-current heat exchanger, for use as e.g. condenser in rectification column during low-temperature analysis of air for obtaining oxygen, has fluid channels formed by gaps between radially arranged tubes
JP6738126B2 (en) * 2015-02-03 2020-08-12 エア・ウォーター・クライオプラント株式会社 Air separation device
RU178401U1 (en) * 2018-01-24 2018-04-03 федеральное государственное бюджетное образовательное учреждение высшего образования "Нижегородский государственный технический университет им. Р.Е. Алексеева" (НГТУ) Heat and mass transfer device
US12287145B2 (en) 2020-03-13 2025-04-29 Air Products And Chemicals, Inc. Heat exchanger apparatus, manifold arrangement for a heat exchanger apparatus, and methods relating to same

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5035284A (en) * 1987-12-24 1991-07-30 Sumitomo Presicion Products Co. Ltd. Plate-fin-type heat exchanger
DE4204172A1 (en) * 1992-02-13 1993-08-19 Linde Ag Process to treat flow of warm fluid e.g. in distillation - reduces cost by lowering complexity of control and instrumentation equipment
US5333683A (en) * 1991-12-11 1994-08-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Indirect heat exchanger
US5979182A (en) * 1997-03-13 1999-11-09 Kabushiki Kaisha Kobe Seiko Sho Method of and apparatus for air separation
FR2778971A1 (en) * 1998-05-20 1999-11-26 Air Liquide Installation for supplying at least one gas which is a component of air under a high pressure
EP0971189A1 (en) * 1998-07-10 2000-01-12 Praxair Technology, Inc. Cryogenic air separation system with high ratio turboexpansion

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5035284A (en) * 1987-12-24 1991-07-30 Sumitomo Presicion Products Co. Ltd. Plate-fin-type heat exchanger
US5333683A (en) * 1991-12-11 1994-08-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Indirect heat exchanger
DE4204172A1 (en) * 1992-02-13 1993-08-19 Linde Ag Process to treat flow of warm fluid e.g. in distillation - reduces cost by lowering complexity of control and instrumentation equipment
US5979182A (en) * 1997-03-13 1999-11-09 Kabushiki Kaisha Kobe Seiko Sho Method of and apparatus for air separation
FR2778971A1 (en) * 1998-05-20 1999-11-26 Air Liquide Installation for supplying at least one gas which is a component of air under a high pressure
EP0971189A1 (en) * 1998-07-10 2000-01-12 Praxair Technology, Inc. Cryogenic air separation system with high ratio turboexpansion

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2867262A1 (en) * 2004-03-02 2005-09-09 Air Liquide Separation of air by cryogenic distillation and installation using thermally interconnected medium and low pressure columns
WO2005085728A1 (en) * 2004-03-02 2005-09-15 L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Cryogenic distillation method for air separation and installation used to implement same
DE102007031759A1 (en) 2007-07-07 2009-01-08 Linde Ag Method and apparatus for producing gaseous pressure product by cryogenic separation of air
DE102007031765A1 (en) 2007-07-07 2009-01-08 Linde Ag Process for the cryogenic separation of air
EP2015013A2 (en) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Process and device for producing a gaseous pressurised product by cryogenic separation of air
EP2015012A2 (en) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Process for the cryogenic separation of air
DE102009034979A1 (en) 2009-04-28 2010-11-04 Linde Aktiengesellschaft Method for producing pressurized oxygen by evaporating liquid oxygen using a copper and nickel heat exchanger block
EP2312248A1 (en) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Method and device for obtaining pressurised oxygen and krypton/xenon
EP2458311A1 (en) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
DE102010052545A1 (en) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Method and apparatus for recovering a gaseous product by cryogenic separation of air
DE102010052544A1 (en) 2010-11-25 2012-05-31 Linde Ag Process for obtaining a gaseous product by cryogenic separation of air
EP2466236A1 (en) 2010-11-25 2012-06-20 Linde Aktiengesellschaft Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air
EP2520886A1 (en) 2011-05-05 2012-11-07 Linde AG Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air
DE102011112909A1 (en) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Process and apparatus for recovering steel
EP2568242A1 (en) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Method and device for generating of steel
EP2600090A1 (en) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Method and device for generating pressurised oxygen by cryogenic decomposition of air
DE102011121314A1 (en) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator
DE102012017488A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements
EP2784420A1 (en) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Method for air separation and air separation plant
WO2014154339A2 (en) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Method for air separation and air separation plant
EP2801777A1 (en) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Air separation plant with main compressor drive
DE102013017590A1 (en) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer
EP2963370A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
EP2963367A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for cryogenic air separation with variable power consumption
EP2963371A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for creating a pressurised gas product by the cryogenic decomposition of air
EP2963369A1 (en) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
WO2016005031A1 (en) 2014-07-05 2016-01-14 Linde Aktiengesellschaft Method and device for the low-temperature separation of air at variable energy consumption
EP3006875A1 (en) 2014-10-09 2016-04-13 Linde Aktiengesellschaft Method for regulating a coupled heat exchanger system and heat exchanger system
WO2018206886A1 (en) * 2017-05-11 2018-11-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchange apparatus
FR3066265A1 (en) * 2017-05-11 2018-11-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude HEAT EXCHANGE APPARATUS

Also Published As

Publication number Publication date
DE10021081A1 (en) 2002-01-03
CN1321868A (en) 2001-11-14
CN1202400C (en) 2005-05-18
US6629433B2 (en) 2003-10-07
US20020124596A1 (en) 2002-09-12
KR20010098779A (en) 2001-11-08
JP2001355963A (en) 2001-12-26

Similar Documents

Publication Publication Date Title
EP1150082A1 (en) Method and apparatus for heat exchange
EP0093448B1 (en) Process and apparatus for obtaining gaseous oxygen at elevated pressure
EP0384483B1 (en) Air rectification process and apparatus
EP1672301B1 (en) Apparatus for the cryogenic separation of a gaseous mixture in particular of air
EP1994344A1 (en) Method and apparatus for fractionating air at low temperatures
EP1284404A1 (en) Process and device for recovering a product under pressure by cryogenic air separation
DE4109945A1 (en) METHOD FOR DEEP TEMPERATURE DISPOSAL OF AIR
EP1067345A1 (en) Process and device for cryogenic air separation
DE102010052545A1 (en) Method and apparatus for recovering a gaseous product by cryogenic separation of air
EP3059536A1 (en) Method and device for obtaining a pressurised nitrogen product
EP2313724A2 (en) Process and device for cryogenic air fractionation
DE10013073A1 (en) Low temperature separation of air in distillation column system uses integrated heat exchanger system for cooling e.g. air supply by indirect heat exchange during vaporization of first liquid fraction
EP1544559A1 (en) Process and device for the cryogenic separation of air
EP1146301A1 (en) Process and apparatus for the production of high pressure nitrogen from air separation
DE10238282A1 (en) Process for the low temperature decomposition of air comprises feeding a first process air stream into a high pressure column, producing a first oxygen-enriched fraction in the high pressure column, and further processing
EP0768503B1 (en) Triple column air separation process
EP0795727A1 (en) Process and apparatus for liquefying a low-boiling gas
DE102004016931A1 (en) Method and apparatus for variably producing a printed product by cryogenic separation of air
EP1329680B1 (en) Plate-type heat exchanger
DE10045128A1 (en) Method and device for producing high-purity nitrogen by low-temperature air separation
DE10052180A1 (en) Three-column system for the low-temperature separation of air
DE10147047A1 (en) Production of liquid product, especially nitrogen, involves compressing gas stream in circulation compressor, and cooling partial streams produced before liquefying and withdrawing
WO2023030689A1 (en) Method for recovering one or more air products, and air separation plant
DE10339224A1 (en) Method for cryogenic decomposition of air in rectifier system for separating nitrogen and oxygen involves compressing a third air current with first air current in secondary compressor
EP1209431A1 (en) Process and apparatus for the production of nitrogen and oxygen

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

AX Request for extension of the european patent

Free format text: AL;LT;LV;MK;RO;SI

17P Request for examination filed

Effective date: 20020408

AKX Designation fees paid

Free format text: AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

17Q First examination report despatched

Effective date: 20040510

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20041123