EP0895045A2 - Air separation process - Google Patents

Air separation process Download PDF

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Publication number
EP0895045A2
EP0895045A2 EP98113793A EP98113793A EP0895045A2 EP 0895045 A2 EP0895045 A2 EP 0895045A2 EP 98113793 A EP98113793 A EP 98113793A EP 98113793 A EP98113793 A EP 98113793A EP 0895045 A2 EP0895045 A2 EP 0895045A2
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
liquid
liquid fraction
pressure
tank
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.)
Granted
Application number
EP98113793A
Other languages
German (de)
French (fr)
Other versions
EP0895045B1 (en
EP0895045A3 (en
Inventor
Horst Dipl.-Ing. Corduan
Stefan Dipl.-Ing. Lochner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP0895045A2 publication Critical patent/EP0895045A2/en
Publication of EP0895045A3 publication Critical patent/EP0895045A3/en
Application granted granted Critical
Publication of EP0895045B1 publication Critical patent/EP0895045B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—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
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/0423—Subcooling of liquid process streams
    • 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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated 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
    • F25J3/04406—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
    • F25J3/04763—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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a method and an apparatus for obtaining a Product gas under increased pressure by low temperature separation of air by means of Rectification, providing emergency care.
  • the product gas obtained in an air separation plant is often under increased pressure needed.
  • the pressure is increased either by post-compression of the gaseous product by means of a compressor or by increasing the pressure of the product obtained in the liquid state and subsequent evaporation.
  • the latter method is also known as internal compression and has the advantage of less than gaseous product compression Apparatus costs.
  • additional Components essentially require a storage tank, in which during the Part of the liquid product is routed during normal operation, as well as an emergency evaporator and a pump, with the help of which, if necessary, liquid from the tank to the Emergency evaporator can be pumped and evaporated there.
  • the main heat exchanger is usually used as the main heat carrier serving high pressure air flow, which after the main heat exchanger on a lower pressure is throttled and therefore in the following as a throttle current is referred to, and a stream referred to below as separation air stream is passed.
  • the latter is cooled down to its dew point and in the gaseous state State of the pressure column supplied, while the throttle current is mostly fluid in the Rectification.
  • the chosen designation does not mean that the choke current is not also broken down by rectification.
  • the object of the present invention is to make it inexpensive and technically simple implementing method of the type mentioned and a corresponding Show device, which with an emergency supply and an internal compression are provided and can be operated as flexibly as possible.
  • the feed air to be broken down is compressed and then in a main heat exchanger system in indirect Heat exchange cooled with one or more streams.
  • the cooled air is fed to a rectification system in which one or more fractions be won.
  • At least one liquid fraction is in a tank cached.
  • a corresponding part of the liquid is made removed from the tank and the pressure of this liquid with a suitable Device increased.
  • it is under increased pressure standing liquid preheated in a preheater and then in the main heat exchanger system evaporates.
  • the resulting gaseous The printed product is then used for its intended purpose.
  • the term preheater refers to the function of a Heat exchanger block or a section of a heat exchanger block.
  • Pre-heat exchanger and the main heat exchanger do not necessarily have to be two be different components, but can be both as separate Heat exchanger blocks can be run as well as in a common Heat exchanger block can be integrated. It is essential that in the preheater such heating of the liquid under increased pressure is achieved, that liquefaction of the decomposition air, which is passed in gaseous form into the pressure column should be avoided at the cold end of the main heat exchanger.
  • the liquid stored in the tank by means of the device for increasing the pressure not pumped into the preheater, but into an emergency evaporator and there evaporates.
  • the gaseous product obtained in the emergency evaporator can then on the appropriate locations are forwarded to the emergency care ensure.
  • An operating fault should be understood to mean all operating states at to whom the quantity or quality of the decomposition products produced does not meet the needs on these products. This can be caused by failures or Malfunction of system components. But also temporarily increased demand for one or more rectification products is in this Context referred to as a disruption to the normal operation of the plant. The Emergency care is guaranteed in times when the currently gained Amount of product does not meet requirements, adequate supply with gaseous product.
  • Any liquid storage device can serve as a tank. This can both inside and outside the cryogenic air separation plant be arranged.
  • the pressure increase of the liquid fraction can, for example, with a pump located downstream of the tank or by changing the static height of the liquid can be achieved.
  • the invention combines a method for generating gaseous Printed product by internal compression using a procedure for emergency supply.
  • the internal compression and emergency care are independent of each other, are used for the internal compression of the liquid product and the emergency supply each has its own pump and corresponding lines and Valves needed.
  • the liquid fraction brought to increased pressure is preferably indirect Heat exchange is heated with a fraction obtained in the rectification system.
  • the temperature of the pressures brought to increased pressure is particularly preferred.
  • a nitrogen-rich or oxygen-rich fraction e.g. of the Bottom fluid of the pressure column
  • the main heat exchanger often turns into a choke flow and other gaseous separation air passed. Conveniently, the on increased liquid pressure brought about by the from the main heat exchanger emerging choke current heated. For smaller quantities to be heated up, the gaseous liquid can also be subjected to increased pressure Separation air flow downstream of the main heat exchanger as a heat carrier to serve.
  • Pre-heat exchangers are particularly advantageous when the temperature of the feed air downstream of the main heat exchanger is higher than that of the product flows. are conversely, the product flows from the rectification system warmer than that Feed air flow, the internally compressed liquid products are advantageous in indirect heat exchange heated with these product streams.
  • the liquid product flows are removed from the rectification system obtained above atmospheric pressure and then in the under normal pressure standing tanks initiated. With the relaxation that occurs, evaporates Part of the liquid products and is therefore lost as a liquid. In the Heating of the internally compressed liquids in the heat exchange with the Product flows from the rectification system are the latter before being introduced in the tanks cooled, causing the losses described in the relaxation of the Liquids, the so-called flash losses, are lower.
  • Oxygen and / or nitrogen are preferred as liquid products from the Rectification system withdrawn, fed into a tank, at least partially again removed from the tank, compressed in the liquid state and then heated and evaporated.
  • the liquid fraction brought to increased pressure becomes indirect Heat exchange with the feed air emerging from the main heat exchanger, heated especially with the inductor current, so are stronger Temperature increases possible.
  • part of the liquid fraction is removed according to the invention removed from the tank and fed to an emergency evaporator.
  • the emergency evaporator liquid fraction advantageous with ambient air or water as a heat transfer medium evaporates.
  • a rectification system with a Feed air line includes that in a main heat exchanger and from this into the Rectification system with a line for the removal of a liquid fraction the rectification system and for its introduction into a tank, with a Liquid product line for the liquid fraction from the tank to one Preheater, a connection between the preheater and the Main heat exchanger, a product line to extract the vaporized liquid Fraction as a gaseous pressure product, one in the liquid product line arranged device for increasing the pressure of the liquid fraction, and one downstream of the device for increasing the pressure of the liquid fraction branching line to an evaporation device for emergency supply.
  • the preheater in the line for removing the is advantageous Liquid product arranged from the rectification system, so that by means of Device for increasing the pressure brought to increased pressure liquid product the product fed into the tank by the rectification system is heated.
  • the preheater and the main heat exchanger into one to summarize a single component, i.e. to provide a heat exchanger block in the different sections the functions of the preheater and that of Perceive main heat exchanger.
  • the cleaned feed air is in a throttle flow 1 with a pressure of 5 to 70 bar and a separation air stream 31 compressed to pressure column pressure and introduced into the main heat exchanger system 2.
  • the maximum pressure on the the operational air can be compressed is carried out by the execution of the Main heat exchanger 2 determined.
  • gaseous decomposition air 31 cooled to about its dew point and via line 3 fed to the pressure column 4 of the rectification system.
  • the throttle air flow 1 is, as far if the Q-T curve allows, also cooled.
  • the rectification system includes: another a low-pressure column 5, which at a pressure between 1.1 and 3 bar, preferably between 1.3 and 1.7 bar, is operated.
  • the pressure column 4 and the Low pressure column 5 are in thermal contact via the main condenser 6.
  • Gaseous nitrogen 7 from the top of the pressure column 4 is in the main condenser 6 in heat exchange with liquid oxygen, the bottom of line 8 Low pressure column 5 is removed, liquefied.
  • the evaporating oxygen is introduced back into the low pressure column 5 via line 15.
  • the liquid On the one hand, nitrogen is applied to the pressure column 4 as reflux liquid 9, on the other hand, via the preheater 10, a liquid separator 11 fed. A part of the liquid accumulating in the separator 11 is called Return liquid 14 used for the low pressure column 5, the remaining liquid Nitrogen, which is under the top pressure of the low pressure column 5, is via line 12 relaxed in a liquid nitrogen tank 13.
  • the liquid nitrogen is in tank 13 preferably under atmospheric pressure. In the preheater 10 Temperature of the nitrogen lowered, so that due to the pressure drop arising when the liquid nitrogen is introduced into the tank 13 Evaporation losses are very low.
  • Liquid oxygen 8 is taken from the bottom of the low-pressure column 5 and partly fed to the main capacitor 6, partly in one Preheat exchanger 16 subcooled.
  • the supercooled liquid oxygen is converted into one Liquid oxygen tank 17 introduced, in which the oxygen is under atmospheric pressure is stored.
  • the liquid nitrogen from the tank 13 is pumped to a pressure of brought up to 200 bar and then passed to the preheater 10 (Line 19).
  • the pressure nitrogen the temperature of 80 K, for example, in countercurrent to that from the main capacitor 6 stripped nitrogen heated to about 95 K.
  • the pressure nitrogen heated in this way is passed via line 20 to the main heat exchanger 2.
  • line 20 branches into that in heat exchanger 2 leading lines 21a and 21b.
  • the line 21a is under high pressure standing nitrogen is passed directly into the heat exchanger 2, where it evaporates and can then via line 22a as a high pressure product with a pressure of preferably up to 60 bar.
  • the pressure of the in the Main heat exchanger 2 directed nitrogen can also be higher than 60 bar However, maximum pressure is due to the pressure resistance of the heat exchanger 2 certainly. A portion of the pressure nitrogen 20 can then be relaxed in line 21b evaporated and via line 22b as a gaseous product of medium pressure be removed.
  • At least part of the oxygen stored in the tank 17 is produced in an analogous manner internally compressed by the two pumps 23a and 23b.
  • the two oxygen flows brought to increased pressure through Heat exchange with that obtained from the bottom of the low pressure column 5 Oxygen flow warmed. After the evaporation of the internally compressed oxygen in the main heat exchanger 2 becomes more gaseous via the lines 24a and 24b Deducted oxygen of increased pressure.
  • FIG. 2 shows a variant of the air separation plant according to the invention, wherein in Figures 1 and 2, the same parts of the system are designated by the same reference numerals.
  • the system according to FIG. 2 differs from the system shown in FIG. 1 essentially in that now with the pumps 18 and 23rd internally compressed product flows in the preheater 30 against the cold Leaving the main heat exchanger 2 emerging throttle air flow 1 are heated.
  • the preheater 10 and 16 for heating the internally compressed nitrogen or oxygen against the corresponding ones from the low pressure column 5 withdrawn product flows are eliminated.
  • the variant described with reference to FIG. 2 is particularly advantageous if when the compressed throttle air emerging from the main heat exchanger 2 is warmer than the rectification products. This will improve the preheating of the achieved liquid products under increased pressure and the equipment effort becomes lower, since instead of two preheater exchangers, only one preheater exchanger necessary is

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Abstract

Air separation process in which incoming compressed air is cooled in a principal heat exchanger (2) and passed from there into the rectification system. A liquefied fraction is passed into a storage tank for subsequent compression, warmed in a pre-heat exchanger (10) and evaporated in the principal heat exchanger. Hence product at an elevated pressure is gained. In case of process failure the liquefied product is drawn off, evaporated and passed to the emergency system. Also claimed is the equipment required for this process.

Description

Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur Gewinnung eines Produktgases unter erhöhtem Druck durch Tieftemperaturzerlegung von Luft mittels Rektifikation, wobei eine Notversorgung vorgesehen ist.The invention relates to a method and an apparatus for obtaining a Product gas under increased pressure by low temperature separation of air by means of Rectification, providing emergency care.

Häufig wird das in einer Luftzerlegungsanlage gewonnene Produktgas unter erhöhtem Druck benötigt. Die Druckerhöhung erfolgt entweder durch Nachverdichtung des gasförmigen Produktes mittels eines Kompressors oder durch Druckerhöhung des gewonnenen Produktes im flüssigen Zustand und anschließende Verdampfung. Letzteres Verfahren ist auch unter der Bezeichnung Innenverdichtung bekannt und hat gegenüber der gasförmigen Produktverdichtung den Vorteil geringerer Apparatekosten.The product gas obtained in an air separation plant is often under increased pressure needed. The pressure is increased either by post-compression of the gaseous product by means of a compressor or by increasing the pressure of the product obtained in the liquid state and subsequent evaporation. The latter method is also known as internal compression and has the advantage of less than gaseous product compression Apparatus costs.

Ebenfalls bekannt sind Luftzerlegungsanlagen, die bei einer Betriebsstörung, beispielsweise einem Defekt einer Pumpe oder einem Betriebsausfall, eine Notversorgung mit Produktgas gewährleisten. Hierfür sind als zusätzliche Komponenten im wesentlichen ein Speichertank nötig, in den während des Normalbetriebes ein Teil des Flüssigproduktes geleitet wird, sowie ein Notverdampfer und eine Pumpe, mit deren Hilfe im Bedarfsfall Flüssigkeit aus dem Tank zu dem Notverdampfer gepumpt werden und dort verdampft werden kann.Also known are air separation plants which, in the event of a malfunction, for example a defect in a pump or a breakdown, a Ensure emergency supply with product gas. For this are as additional Components essentially require a storage tank, in which during the Part of the liquid product is routed during normal operation, as well as an emergency evaporator and a pump, with the help of which, if necessary, liquid from the tank to the Emergency evaporator can be pumped and evaporated there.

Aus der US-5,566,556 ist ein Verfahren zur Gewinnung von gasförmigen Druckprodukten durch Innenverdichtung bekannt. Hierzu wird beispielsweise flüssiger Sauerstoff aus dem Sumpf der Niederdruckkolonne entnommen und entweder in einem Flüssigsauerstofftank zwischengelagert oder mittels einer Pumpe auf einen erhöhten Druck gebracht und im Hauptwärmetauscher verdampft und auf Umgebungstemperatur erwärmt. Der im Tank gespeicherte Sauerstoff kann gegebenenfalls auch in einem Hilfsverdampfer verdampft und zur Notversorgung herangezogen werden.From US-5,566,556 is a process for the extraction of gaseous Known print products by internal compression. For example, this becomes more fluid Oxygen taken from the bottom of the low pressure column and either in temporarily stored in a liquid oxygen tank or by means of a pump on one brought increased pressure and evaporated in the main heat exchanger and on Ambient temperature warmed. The oxygen stored in the tank can if necessary also evaporated in an auxiliary evaporator and for emergency supply be used.

Durch den Hauptwärmetauscher werden in der Regel ein als Hauptwärmeträger dienender Hochdruckluftstrom, der nach dem Hauptwärmetauscher auf einen niedrigeren Druck gedrosselt wird und daher im folgenden als Drosselstrom bezeichnet wird, und ein im folgenden Zerlegungsluftstrom genannter Strom geleitet. The main heat exchanger is usually used as the main heat carrier serving high pressure air flow, which after the main heat exchanger on a lower pressure is throttled and therefore in the following as a throttle current is referred to, and a stream referred to below as separation air stream is passed.

Letzterer wird bis maximal auf seinen Taupunkt abgekühlt und im gasförmigen Zustand der Drucksäule zugeführt, während der Drosselstrom meist flüssig in die Rektifikation geleitet wird. Die gewählte Bezeichnungsweise bedeutet aber nicht, daß der Drosselstrom nicht auch durch Rektifikation zerlegt wird.The latter is cooled down to its dew point and in the gaseous state State of the pressure column supplied, while the throttle current is mostly fluid in the Rectification. The chosen designation does not mean that the choke current is not also broken down by rectification.

Sind die innenverdichteten Flüssigkeitsströme wesentlich kälter als die entsprechenden Produktströme aus der Rektifikation, kann bei der Verdampfung der innenverdichteten Ströme im Hauptwärmetauscher das Problem auftreten, daß sich die Zerlegungsluft, die gasförmig in die Drucksäule geleitet werden soll, am kalten Ende des Hauptwärmetauschers verflüssigt. Dadurch wird die Rektifikation negativ beeinflußt.Are the internally compressed liquid flows much colder than that corresponding product streams from the rectification, can be used in the evaporation of the internally compressed flows in the main heat exchanger the problem may arise the separation air, which is to be passed in gaseous form into the pressure column, is cold Liquefied at the end of the main heat exchanger. This makes the rectification negative influenced.

Aufgabe vorliegender Erfindung ist es, ein kostengünstiges und technisch einfach zu realisierendes Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung aufzuzeigen, welche mit einer Notversorgung und einer Innenverdichtung versehen sind und möglichst flexibel betrieben werden können.The object of the present invention is to make it inexpensive and technically simple implementing method of the type mentioned and a corresponding Show device, which with an emergency supply and an internal compression are provided and can be operated as flexibly as possible.

Verfahrensseitig wird diese Aufgabe durch die Merkmale des Anspruch 1 gelöst.In terms of the method, this object is achieved by the features of claim 1.

Bei dem erfindungsgemäßen Verfahren wird die zu zerlegende Einsatzluft verdichtet und anschließend in einem Hauptwärmetauschersystem in indirektem Wärmeaustausch mit einem oder mehreren Strömen abgekühlt. Die abgekühlte Luft wird einem Rektifiziersystem zugeführt, in dem eine oder mehrere Fraktionen gewonnen werden. Zumindest eine flüssige Fraktion wird in einem Tank zwischengespeichert. Je nach Bedarf wird ein entsprechender Teil der Flüssigkeit aus dem Tank entnommen und der Druck dieser Flüssigkeit mit einer geeigneten Vorrichtung erhöht. Im Normalbetrieb der Anlage wird die unter erhöhtem Druck stehende Flüssigkeit in einem Vorwärmetauscher vorgewärmt und anschließend in dem Hauptwärmetauschersystem verdampft. Das entstehende gasförmige Druckprodukt wird dann seinem Verwendungszweck zugeführt.In the method according to the invention, the feed air to be broken down is compressed and then in a main heat exchanger system in indirect Heat exchange cooled with one or more streams. The cooled air is fed to a rectification system in which one or more fractions be won. At least one liquid fraction is in a tank cached. Depending on the need, a corresponding part of the liquid is made removed from the tank and the pressure of this liquid with a suitable Device increased. In normal operation of the system, it is under increased pressure standing liquid preheated in a preheater and then in the main heat exchanger system evaporates. The resulting gaseous The printed product is then used for its intended purpose.

Der Begriff Vorwärmetauscher bezieht sich auf die Funktion eines Wärmetauscherblocks oder eines Abschnitts eines Wärmetauscherblocks. Der Vorwärmetauscher und der Hauptwärmetauscher müssen aber nicht unbedingt zwei verschiedene Bauteile sein, sondern können sowohl als separate Wärmetauscherblöcke ausgeführt sein als auch in einem gemeinsamen Wärmetauscherblock integriert werden. Wesentlich ist, daß im Vorwärmetauscher eine solche Erwärmung der unter erhöhtem Druck stehenden Flüssigkeit erreicht wird, daß eine Verflüssigung der Zerlegungsluft, die gasförmig in die Drucksäule geleitet werden soll, am kalten Ende des Hauptwärmetauschers vermieden wird.The term preheater refers to the function of a Heat exchanger block or a section of a heat exchanger block. Of the Pre-heat exchanger and the main heat exchanger do not necessarily have to be two be different components, but can be both as separate Heat exchanger blocks can be run as well as in a common Heat exchanger block can be integrated. It is essential that in the preheater such heating of the liquid under increased pressure is achieved, that liquefaction of the decomposition air, which is passed in gaseous form into the pressure column should be avoided at the cold end of the main heat exchanger.

Sollte eine Betriebsstörung der Tieftemperaturluftzerlegungsanlage auftreten, so wird die in dem Tank gespeicherte Flüssigkeit mit Hilfe der Vorrichtung zur Druckerhöhung nicht in den Vorwärmetauscher, sondern in einen Notverdampfer gepumpt und dort verdampft. Das in dem Notverdampfer gewonnene gasförmige Produkt kann dann an die entsprechenden Einsatzorte weitergeleitet werden, um die Notversorgung sicherzustellen.Should there be a malfunction in the cryogenic air separation plant, the liquid stored in the tank by means of the device for increasing the pressure not pumped into the preheater, but into an emergency evaporator and there evaporates. The gaseous product obtained in the emergency evaporator can then on the appropriate locations are forwarded to the emergency care ensure.

Unter einer Betriebsstörung sollen alle Betriebszustände verstanden werden, bei denen die Menge oder Qualität der erzeugten Zerlegungsprodukte nicht dem Bedarf an diesen Produkten entspricht. Dies kann beispielsweise durch Ausfälle oder Fehlfunktionen von Anlagenkomponenten verursacht sein. Aber auch vorübergehend erhöhter Bedarf an einem oder mehreren Rektifikationsprodukten wird in diesem Zusammenhang als eine Störung des üblichen Betriebs der Anlage bezeichnet. Die Notversorgung gewährleistet also in Zeiten, in denen die momentan gewonnene Produktmenge nicht den Anforderungen entspricht, eine ausreichende Versorgung mit gasförmigem Produkt.An operating fault should be understood to mean all operating states at to whom the quantity or quality of the decomposition products produced does not meet the needs on these products. This can be caused by failures or Malfunction of system components. But also temporarily increased demand for one or more rectification products is in this Context referred to as a disruption to the normal operation of the plant. The Emergency care is guaranteed in times when the currently gained Amount of product does not meet requirements, adequate supply with gaseous product.

Als Tank kann jede Vorrichtung zur Flüssigkeitsspeicherung dienen. Diese kann sowohl innerhalb als auch außerhalb der Tieftemperaturluftzerlegungsanlage angeordnet sein. Die Druckerhöhung der flüssigen Fraktion kann beispielsweise mit einer stromabwärts des Tanks angeordneten Pumpe oder durch Änderung der statischen Höhe der Flüssigkeit erzielt werden.Any liquid storage device can serve as a tank. This can both inside and outside the cryogenic air separation plant be arranged. The pressure increase of the liquid fraction can, for example, with a pump located downstream of the tank or by changing the static height of the liquid can be achieved.

Die Erfindung kombiniert ein Verfahren zur Erzeugung von gasförmigem Druckprodukt durch Innenverdichtung mit einem Verfahren zur Notversorgung. Bei den bisherigen Verfahren, bei denen die Innenverdichtung und die Notversorgung unabhängig voneinander sind, werden für die Innenverdichtung des Flüssigproduktes und die Notversorgung jeweils eine eigene Pumpe und entsprechende Leitungen und Ventile benötigt. Durch die erfindungsgemäße Zusammenlegung wird der apparative Aufwand deutlich verringert.The invention combines a method for generating gaseous Printed product by internal compression using a procedure for emergency supply. At the previous procedures, in which the internal compression and emergency care are independent of each other, are used for the internal compression of the liquid product and the emergency supply each has its own pump and corresponding lines and Valves needed. By combining the invention, the apparatus Effort significantly reduced.

Die auf erhöhten Druck gebrachte flüssige Fraktion wird vorzugsweise in indirektem Wärmeaustausch mit einer in dem Rektifiziersystem gewonnenen Fraktion erwärmt. Besonders bevorzugt wird die Temperatur der auf erhöhten Druck gebrachten, flüssigen Fraktion mit einer stickstoffreichen oder sauerstoffreichen Fraktion, z.B. der Sumpfflüssigkeit der Drucksäule, erhöht. Dabei ist jedoch darauf zu achten, daß die Mengen-, Druck- und Enthalpieverhältnisse des Wärmeträgers und der flüssigen Fraktion aneinander angepaßt sind.The liquid fraction brought to increased pressure is preferably indirect Heat exchange is heated with a fraction obtained in the rectification system. The temperature of the pressures brought to increased pressure is particularly preferred. liquid fraction with a nitrogen-rich or oxygen-rich fraction, e.g. of the Bottom fluid of the pressure column, increased. However, it must be ensured that the Quantity, pressure and enthalpy ratios of the heat transfer medium and the liquid Group are adapted to each other.

Es hat sich herausgestellt, daß die Kältemenge, die von der aus dem Tank abgezogenen und auf erhöhten Druck gebrachten Flüssigkeit angeboten wird, sehr gut von dem Flüssigkeitsstrom, der aus dem Rektifiziersystem in den Tank geleitet wird, aufgenommen werden kann. Werden mehrere Flüssigprodukte, die zumindest teilweise anschließend innenverdichtet werden, aus dem Rektifiziersystem abgezogen, kann es aus apparativen Gründen auch vorteilhaft sein, eines der innenverdichteten Flüssigprodukte mit einem Flüssigprodukt anderer Zusammensetzung zu erwärmen. In der Regel ist jedoch die Erwärmung mit demselben Flüssigprodukt vor der Innenverdichtung, d.h. einem Wärmeträger, der sich von dem innenverdichteten Strom im wesentlichen nur durch seine Temperatur und seinen Druck unterscheidet, zu bevorzugen.It has been found that the amount of cold that comes from the tank withdrawn and pressurized liquid is offered, very well from the flow of liquid that flows from the rectification system into the tank will be included. Be several liquid products, at least partially then internally compressed from the rectification system deducted, it can also be advantageous for apparatus reasons, one of the internally compressed liquid products with a liquid product of another Warm composition. As a rule, however, the warming is with the same liquid product before internal compression, i.e. a heat transfer medium that differs from the internally compressed stream essentially only by its temperature and distinguishes its print, prefer.

Neben der Erwärmung der auf erhöhten Druck gebrachten, flüssigen Fraktion mit gasförmigen oder flüssigen Produkten aus dem Rektifiziersystem hat sich auch die Erwärmung dieser Fraktion mit der aus dem Hauptwärmetauscher austretenden, verdichteten Einsatzluft als günstig erwiesen.In addition to heating the liquid fraction brought to increased pressure with The gaseous or liquid products from the rectification system also have Heating of this fraction with that emerging from the main heat exchanger, compressed feed air proved to be cheap.

Häufig werden durch den Hauptwärmetauscher zum einen ein Drosselstrom und zum anderen gasförmige Zerlegungsluft geleitet. Zweckmäßigerweise wird die auf erhöhten Druck gebrachte, flüssige Fraktion durch den aus dem Hauptwärmetauscher austretenden Drosselstrom erwärmt. Bei kleineren Mengen zu erwärmender, auf erhöhten Druck gebrachter Flüssigkeit kann aber auch der gasförmige Zerlegungsluftstrom stromabwärts des Hauptwärmetauschers als Wärmeträger dienen.The main heat exchanger often turns into a choke flow and other gaseous separation air passed. Conveniently, the on increased liquid pressure brought about by the from the main heat exchanger emerging choke current heated. For smaller quantities to be heated up However, the gaseous liquid can also be subjected to increased pressure Separation air flow downstream of the main heat exchanger as a heat carrier to serve.

Die Entscheidung, welcher der oben genannten Wärmeträger im Einzelfall der geeignete ist, ist unter anderem von den apparativen Gegebenheiten, d.h. von der Anordnung der Verrohrungen, und von den Temperaturverhältnissen der beteiligten Gas- bzw. Flüssigkeitsströme abhängig.The decision as to which of the above-mentioned heat transfer fluids in the individual case is suitable, among other things, from the equipment, i.e. of the Arrangement of the piping, and the temperature conditions of the participants Depending on gas or liquid flows.

Werden unterschiedliche flüssige Fraktionen durch Rektifikation gewonnen und anschließend innenverdichtet, so ist es aus apparativen Gründen häufig günstiger, die Innenverdichtungsströme in indirektem Wärmeaustausch mit der komprimierten Einsatzluft zu erwärmen. Durch die im Vergleich zu den Produkten naturgemäß deutlich größere Menge an Einsatzluft können mehrere Innenverdichtungsströme in einem Vorwärmetauscher gegen die verdichtete Einsatzluft erwärmt werden. Dies erlaubt eine einfachere Ausführung der Anlage und eine Einsparung an Vorwärmetauschern.Are different liquid fractions obtained by rectification and then internally compressed, it is often cheaper for apparatus reasons Internal compression flows in indirect heat exchange with the compressed To heat the feed air. Due to the natural in comparison to the products A significantly larger amount of feed air can be used in several internal compression flows a preheater against the compressed feed air. This allows a simpler design of the system and savings Preheater.

Die Verwendung von Einsatzluft als Wärmeträger zur Erwärmung der innenverdichteten Flüssigkeitsströme hat gegenüber der Verwendung der Produktströme aus der Rektifikation neben der oben erwähnten Einsparung an Vorwärmetauschern insbesondere dann Vorteile, wenn die Temperatur der Einsatzluft stromabwärts des Hauptwärmetauschers höher ist als die der Produktströme. Sind umgekehrt die Produktströme aus dem Rektifikationssystem wärmer als der Einsatzluftstrom, so werden die innenverdichteten Flüssigkeitsprodukte vorteilhaft in indirektem Wärmeaustausch mit diesen Produktströmen erwärmt.The use of feed air as a heat carrier for heating the internally compressed liquid flows compared to the use of the Product flows from rectification in addition to the savings mentioned above Pre-heat exchangers are particularly advantageous when the temperature of the feed air downstream of the main heat exchanger is higher than that of the product flows. are conversely, the product flows from the rectification system warmer than that Feed air flow, the internally compressed liquid products are advantageous in indirect heat exchange heated with these product streams.

Die flüssigen Produktströme werden aus dem Rektifikationssystem unter überatmosphärischen Druck gewonnen und anschließend in die unter Normaldruck stehenden Tanks eingeleitet. Bei der dabei auftretenden Entspannung verdampft ein Teil der flüssigen Produkte und geht somit als Flüssigkeit verloren. Bei der Erwärmung der innenverdichteten Flüssigkeiten im Wärmeaustausch mit den Produktströmen aus dem Rektifikationssystem werden letztere vor der Einleitung in die Tanks gekühlt, wodurch die beschriebenen Verluste bei der Entspannung der Flüssigkeiten, die sogenannten Flashverluste, geringer ausfallen.The liquid product flows are removed from the rectification system obtained above atmospheric pressure and then in the under normal pressure standing tanks initiated. With the relaxation that occurs, evaporates Part of the liquid products and is therefore lost as a liquid. In the Heating of the internally compressed liquids in the heat exchange with the Product flows from the rectification system are the latter before being introduced in the tanks cooled, causing the losses described in the relaxation of the Liquids, the so-called flash losses, are lower.

Von Vorzug werden Sauerstoff und/oder Stickstoff als flüssige Produkte aus dem Rektifikationssystem abgezogen, in einen Tank geleitet, zumindest teilweise wieder aus dem Tank entnommen, in flüssigem Aggregatszustand verdichtet und anschließend erwärmt und verdampft.Oxygen and / or nitrogen are preferred as liquid products from the Rectification system withdrawn, fed into a tank, at least partially again removed from the tank, compressed in the liquid state and then heated and evaporated.

Es hat sich gezeigt, daß bei einer Erwärmung der auf erhöhten Druck gebrachten flüssigen Fraktion in indirektem Wärmeaustausch mit einer in dem Rektifiziersystem gewonnenen Fraktion eine Temperaturerhöhung der auf erhöhten Druck gebrachten, flüssigen Fraktion in dem Vorwärmetauscher auf bis zu 1 bis 1,5 K unterhalb der Siedetemperatur der in dem Rektifiziersystem gewonnenen Fraktion günstig ist. Auf diese Weise wird eine Verflüssigung der Zerlegungsluft bei der sich anschließenden Verdampfung der auf erhöhten Druck gebrachten, flüssigen Fraktion im Hauptwärmetauscher vermieden und die technische Ausführung des Vor- und des Hauptwärmetauschers kann relativ einfach gehalten werden. It has been shown that when heated, the pressure is increased liquid fraction in indirect heat exchange with one in the rectification system obtained fraction an increase in temperature of the brought to increased pressure, liquid fraction in the preheater up to 1 to 1.5 K below the Boiling temperature of the fraction obtained in the rectification system is favorable. On in this way a liquefaction of the separation air in the subsequent Evaporation of the liquid fraction brought to increased pressure in the Main heat exchanger avoided and the technical execution of the pre and the Main heat exchanger can be kept relatively simple.

Wird die auf erhöhten Druck gebrachten flüssigen Fraktion in indirektem Wärmeaustausch mit der aus dem Hauptwärmetauscher austretenden Einsatzluft, insbesondere mit dem Drosselstrom, erwärmt, so sind stärkere Temperaturerhöhungen möglich. Vorzugsweise wird in diesem Fall die auf erhöhten Druck gebrachten flüssigen Fraktion auf die gleiche Temperatur gebracht wie die anderen vom kalten Ende her in den Hauptwärmetauscher geführten Ströme. Dadurch wird die Gestaltung des Hauptwärmetauschers einfacher.The liquid fraction brought to increased pressure becomes indirect Heat exchange with the feed air emerging from the main heat exchanger, heated especially with the inductor current, so are stronger Temperature increases possible. In this case, it is preferred to increase the Pressurized liquid fraction brought to the same temperature as that other flows from the cold end into the main heat exchanger. This makes the design of the main heat exchanger easier.

Bei einer Betriebsstörung wird erfindungsgemäß ein Teil der flüssigen Fraktion aus dem Tank entnommen und einem Notverdampfer zugeführt. Der Flüssigkeitsstrom zu dem Vorwärmetauscher, der im Normalbetrieb die innenverdichtete Flüssigkeit erwärmt, wird dabei vorzugsweise unterbrochen. In dem Notverdampfer wird die flüssige Fraktion von Vorteil mit Umgebungsluft oder Wasser als Wärmeträger verdampft.In the event of a malfunction, part of the liquid fraction is removed according to the invention removed from the tank and fed to an emergency evaporator. The liquid flow too the preheater, which is the internally compressed liquid in normal operation heated, is preferably interrupted. In the emergency evaporator liquid fraction advantageous with ambient air or water as a heat transfer medium evaporates.

Neben dem Verfahren zur Tieftemperaturluftzerlegung bezieht sich die Erfindung auch auf eine entsprechende Vorrichtung, welche ein Rektifiziersystem mit einer Einsatzluftleitung umfaßt, die in einen Hauptwärmetauscher und von diesem in das Rektifiziersystem führt, mit einer Leitung zur Entnahme einer flüssigen Fraktion aus dem Rektifiziersystem und zu deren Einleitung in einen Tank, mit einer Flüssigproduktleitung für die flüssige Fraktion von dem Tank zu einem Vorwärmetauscher, einer Verbindung zwischen dem Vorwärmetauscher und dem Hauptwärmetauscher, einer Produktleitung zur Entnahme der verdampften flüssigen Fraktion als gasförmiges Druckprodukt, einer in der Flüssigproduktleitung angeordneten Vorrichtung zur Druckerhöhung der flüssigen Fraktion, und einer stromabwärts der Vorrichtung zur Druckerhöhung der flüssigen Fraktion abzweigenden Leitung zu einer Verdampfungsvorrichtung zur Notversorgung.In addition to the method for low-temperature air separation, the invention relates also on a corresponding device, which a rectification system with a Feed air line includes that in a main heat exchanger and from this into the Rectification system with a line for the removal of a liquid fraction the rectification system and for its introduction into a tank, with a Liquid product line for the liquid fraction from the tank to one Preheater, a connection between the preheater and the Main heat exchanger, a product line to extract the vaporized liquid Fraction as a gaseous pressure product, one in the liquid product line arranged device for increasing the pressure of the liquid fraction, and one downstream of the device for increasing the pressure of the liquid fraction branching line to an evaporation device for emergency supply.

Vorteilhaft ist der Vorwärmetauscher in der Leitung zur Entnahme des Flüssigproduktes aus dem Rektifiziersystem angeordnet, so daß das mittels der Vorrichtung zur Druckerhöhung auf erhöhten Druck gebrachte Flüssigprodukt durch das von dem Rektifiziersystem in den Tank geleitete Produkt erwärmt wird. Ebenfalls günstig ist es, den Vorwärmetauscher in der Einsatzluftleitung stromabwärts des Hauptwärmetauschers vorzusehen, so daß die aus dem Hauptwärmetauscher austretende Einsatzluft zur Vorerwärmung genutzt werden kann. In diesem Fall ist es besonders günstig, den Vorwärmetauscher und den Hauptwärmetauscher zu einem einzigen Bauteil zusammenzufassen, d.h. einen Wärmetauscherblock vorzusehen, in dem unterschiedliche Abschnitte die Funktionen des Vorwärmetauschers und die des Hauptwärmetauschers wahrnehmen.The preheater in the line for removing the is advantageous Liquid product arranged from the rectification system, so that by means of Device for increasing the pressure brought to increased pressure liquid product the product fed into the tank by the rectification system is heated. Likewise It is favorable to have the preheater in the feed air line downstream of the Main heat exchanger to be provided, so that from the main heat exchanger escaping feed air can be used for preheating. In this case it is particularly favorable, the preheater and the main heat exchanger into one to summarize a single component, i.e. to provide a heat exchanger block in the different sections the functions of the preheater and that of Perceive main heat exchanger.

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

Figur 1
eine erfindungsgemäße Luftzerlegungsanlage zur Gewinnung von Sauerstoff und Stickstoff unter erhöhtem Druck in Kombination mit einer Notversorgung und
Figur 2
eine Variante einer derartigen Anlage.
The invention and further advantageous details of the invention are explained in more detail below on the basis of exemplary embodiments schematically illustrated in the drawings. Here show:
Figure 1
an air separation plant according to the invention for the production of oxygen and nitrogen under increased pressure in combination with an emergency supply and
Figure 2
a variant of such a system.

Die gereinigte Einsatzluft wird in einen Drosselstrom 1 mit einem Druck von 5 bis 70 bar und einen auf Drucksäulendruck verdichteten Zerlegungsluftstrom 31 aufgeteilt und in das Hauptwärmertauschersystem 2 eingeleitet. Der maximale Druck, auf den die Einsatzluft komprimiert werden kann, wird durch die Ausführung des Hauptwärmetauschers 2 bestimmt. In dem Hauptwärmetauscher 2 wird die gasförmige Zerlegungsluft 31 etwa auf ihren Taupunkt abgekühlt und über Leitung 3 der Drucksäule 4 des Rektifiziersystems zugeführt. Der Drosselluftstrom 1 wird, soweit es der Q-T-Verlauf zuläßt, ebenfalls abgekühlt. Das Rektifiziersystem umfaßt unter anderem noch eine Niederdrucksäule 5, die bei einem Druck zwischen 1,1 und 3 bar, vorzugsweise zwischen 1,3 und 1,7 bar, betrieben wird. Die Drucksäule 4 und die Niederdrucksäule 5 stehen über den Hauptkondensator 6 in thermischem Kontakt.The cleaned feed air is in a throttle flow 1 with a pressure of 5 to 70 bar and a separation air stream 31 compressed to pressure column pressure and introduced into the main heat exchanger system 2. The maximum pressure on the the operational air can be compressed, is carried out by the execution of the Main heat exchanger 2 determined. In the main heat exchanger 2 gaseous decomposition air 31 cooled to about its dew point and via line 3 fed to the pressure column 4 of the rectification system. The throttle air flow 1 is, as far if the Q-T curve allows, also cooled. The rectification system includes: another a low-pressure column 5, which at a pressure between 1.1 and 3 bar, preferably between 1.3 and 1.7 bar, is operated. The pressure column 4 and the Low pressure column 5 are in thermal contact via the main condenser 6.

Gasförmiger Stickstoff 7 aus dem Kopf der Drucksäule 4 wird im Hauptkondensator 6 im Wärmeaustausch mit flüssigem Sauerstoff, der über Leitung 8 dem Sumpf der Niederdrucksäule 5 entnommen wird, verflüssigt. Der dabei verdampfende Sauerstoff wird über Leitung 15 wieder in die Niederdrucksäule 5 eingeleitet. Der flüssige Stickstoff wird zum einen als Rücklaufflüssigkeit 9 auf die Drucksäule 4 aufgegeben, zum anderen über den Vorwärmetauscher 10 einem Flüssigkeitsabscheider 11 zugeführt. Ein Teil der in dem Abscheider 11 anfallenden Flüssigkeit wird als Rücklaufflüssigkeit 14 für die Niederdrucksäule 5 verwendet, der restliche, flüssige Stickstoff, der unter dem Kopfdruck der Niederdrucksäule 5 steht, wird über Leitung 12 in einen Flüssigstickstofftank 13 entspannt. Der Flüssigstickstoff steht im Tank 13 vorzugsweise unter Atmosphärendruck. In dem Vorwärmetauscher 10 wird die Temperatur des Stickstoffs erniedrigt, so daß die aufgrund der Druckerniedrigung beim Einleiten des Flüssigstickstoffs in den Tank 13 entstehenden Verdampfungsverluste nur sehr gering sind.Gaseous nitrogen 7 from the top of the pressure column 4 is in the main condenser 6 in heat exchange with liquid oxygen, the bottom of line 8 Low pressure column 5 is removed, liquefied. The evaporating oxygen is introduced back into the low pressure column 5 via line 15. The liquid On the one hand, nitrogen is applied to the pressure column 4 as reflux liquid 9, on the other hand, via the preheater 10, a liquid separator 11 fed. A part of the liquid accumulating in the separator 11 is called Return liquid 14 used for the low pressure column 5, the remaining liquid Nitrogen, which is under the top pressure of the low pressure column 5, is via line 12 relaxed in a liquid nitrogen tank 13. The liquid nitrogen is in tank 13 preferably under atmospheric pressure. In the preheater 10 Temperature of the nitrogen lowered, so that due to the pressure drop arising when the liquid nitrogen is introduced into the tank 13 Evaporation losses are very low.

Aus dem Sumpf der Niederdrucksäule 5 wird flüssiger Sauerstoff 8 entnommen und zu einem Teil dem Hauptkondensator 6 zugeführt, zum anderen Teil in einem Vorwärmetauscher 16 unterkühlt. Der unterkühlte flüssige Sauerstoff wird in einen Flüssigsauerstofftank 17 eingeleitet, in dem der Sauerstoff unter Atmosphärendruck gelagert wird.Liquid oxygen 8 is taken from the bottom of the low-pressure column 5 and partly fed to the main capacitor 6, partly in one Preheat exchanger 16 subcooled. The supercooled liquid oxygen is converted into one Liquid oxygen tank 17 introduced, in which the oxygen is under atmospheric pressure is stored.

Der Flüssigstickstoff aus dem Tank 13 wird mittels der Pumpe 18 auf einen Druck von bis zu 200 bar gebracht und anschließend zum Vorwärmetauscher 10 geleitet (Leitung 19). Im Vorwärmetauscher 10 wird der Druckstickstoff, der eine Temperatur von beispielsweise 80 K besitzt, im Gegenstrom mit dem aus dem Hauptkondensator 6 abgezogenen Stickstoff auf etwa 95 K erwärmt. Der so erwärmte Druckstickstoff wird über Leitung 20 zum Hauptwärmetauscher 2 geleitet. Vor dem Hauptwärmetauscher 2 verzweigt sich die Leitung 20 in die in den Wärmetauscher 2 führenden Leitungen 21a und 21b. Über die Leitung 21a wird der unter hohem Druck stehende Stickstoff direkt in den Wärmetauscher 2 geleitet, dort verdampft und kann anschließend über Leitung 22a als Hochdruckprodukt mit einem Druck von vorzugsweise bis zu 60 bar entnommen werden. Der Druck des in den Hauptwärmetauscher 2 geleiteten Stickstoffs kann auch höher als 60 bar liegen, der Maximaldruck wird jedoch durch die Druckbeständigkeit des Wärmetauschers 2 bestimmt. In Leitung 21b kann ein Teil des Druckstickstoffs 20 entspannt, dann verdampft und über Leitung 22b als gasförmiges Produkt mittleren Druckes entnommen werden.The liquid nitrogen from the tank 13 is pumped to a pressure of brought up to 200 bar and then passed to the preheater 10 (Line 19). In the preheater 10, the pressure nitrogen, the temperature of 80 K, for example, in countercurrent to that from the main capacitor 6 stripped nitrogen heated to about 95 K. The pressure nitrogen heated in this way is passed via line 20 to the main heat exchanger 2. Before the Main heat exchanger 2, line 20 branches into that in heat exchanger 2 leading lines 21a and 21b. The line 21a is under high pressure standing nitrogen is passed directly into the heat exchanger 2, where it evaporates and can then via line 22a as a high pressure product with a pressure of preferably up to 60 bar. The pressure of the in the Main heat exchanger 2 directed nitrogen can also be higher than 60 bar However, maximum pressure is due to the pressure resistance of the heat exchanger 2 certainly. A portion of the pressure nitrogen 20 can then be relaxed in line 21b evaporated and via line 22b as a gaseous product of medium pressure be removed.

Zumindest ein Teil des in dem Tank 17 gelagerten Sauerstoffs wird in analoger Weise durch die beiden Pumpen 23a und 23b innenverdichtet. In dem Vorwärmetauscher 16 werden die beiden auf erhöhten Druck gebrachten Sauerstoffströme durch Wärmetausch mit dem aus dem Sumpf der Niederdrucksäule 5 gewonnenen Sauerstoffstrom erwärmt. Nach der Verdampfung des innenverdichteten Sauerstoffs im Hauptwärmetauscher 2 wird über die Leitungen 24a und 24b gasförmiger Sauerstoff erhöhten Druckes abgezogen.At least part of the oxygen stored in the tank 17 is produced in an analogous manner internally compressed by the two pumps 23a and 23b. In the preheater 16 the two oxygen flows brought to increased pressure through Heat exchange with that obtained from the bottom of the low pressure column 5 Oxygen flow warmed. After the evaporation of the internally compressed oxygen in the main heat exchanger 2 becomes more gaseous via the lines 24a and 24b Deducted oxygen of increased pressure.

Für den Fall, daß der ordnungsgemäße Betrieb der Anlage nicht mehr aufrechterhalten werden kann, beispielsweise bei Ausfall einer Komponente der Luftzerlegungsanlage, wird die weitere Versorgung mit Sauerstoff und Stickstoff über eine Notversorgung sichergestellt. Die Notversorgung wird auch dann eingesetzt, wenn der Bedarf an gasförmigem Produkt kurzfristig die Produktion übersteigt. Hierzu wird aus dem Tank 13 flüssiger Stickstoff mit Hilfe der Pumpe 18 zu einem Wasserbadverdampfer 25 gepumpt und dort verdampft. Analog kann mittels der Pumpen 23a und 23b flüssiger Sauerstoff den Verdampfern 26a bzw. 26b zugeführt werden, in denen der Sauerstoff gegen Umgebungsluft oder Wasser verdampft wird.In the event that the proper operation of the system is no longer can be maintained, for example in the event of a component failure Air separation plant, the further supply of oxygen and nitrogen is over emergency care ensured. Emergency care is also used when the need for gaseous product temporarily exceeds production. For this becomes liquid nitrogen from the tank 13 with the help of the pump 18 Water bath evaporator 25 pumped and evaporated there. Analogously, the Pumps 23a and 23b supply liquid oxygen to the evaporators 26a and 26b, respectively in which the oxygen is vaporized against ambient air or water.

Figur 2 zeigt eine Variante der erfindungsgemäßen Luftzerlegungsanlage, wobei in den Figuren 1 und 2 gleiche Anlagenteile mit gleichen Bezugsziffern bezeichnet sind. Die Anlage gemäß Figur 2 unterscheidet sich von der in Figur 1 dargestellten Anlage im wesentlichen darin, daß nunmehr die mit den Pumpen 18 und 23 innenverdichteten Produktströme im Vorwärmetauscher 30 gegen den am kalten Ende des Hauptwärmetauschers 2 austretenden Drosselluftstrom 1 erwärmt werden. Die Vorwärmetauscher 10 und 16 zur Erwärmung des innenverdichteten Stickstoffs bzw. Sauerstoffs gegen die entsprechenden aus der Niederdrucksäule 5 abgezogenen Produktströme entfallen.Figure 2 shows a variant of the air separation plant according to the invention, wherein in Figures 1 and 2, the same parts of the system are designated by the same reference numerals. The system according to FIG. 2 differs from the system shown in FIG. 1 essentially in that now with the pumps 18 and 23rd internally compressed product flows in the preheater 30 against the cold Leaving the main heat exchanger 2 emerging throttle air flow 1 are heated. The preheater 10 and 16 for heating the internally compressed nitrogen or oxygen against the corresponding ones from the low pressure column 5 withdrawn product flows are eliminated.

Die anhand von Figur 2 beschriebene Variante ist insbesondere dann vorteilhaft, wenn die aus dem Hauptwärmetauscher 2 austretende, komprimierte Drosselluft wärmer als die Rektifikationsprodukte ist. So wird eine bessere Vorerwärmung der unter erhöhtem Druck stehenden Flüssigprodukte erzielt und der apparative Aufwand wird geringer, da anstatt zwei Vorwärmetauschern nur ein Vorwärmetauscher notwendig istThe variant described with reference to FIG. 2 is particularly advantageous if when the compressed throttle air emerging from the main heat exchanger 2 is warmer than the rectification products. This will improve the preheating of the achieved liquid products under increased pressure and the equipment effort becomes lower, since instead of two preheater exchangers, only one preheater exchanger necessary is

Claims (10)

Verfahren zur Tieftemperaturluftzerlegung von Luft durch Rektifikation, wobei verdichtete Einsatzluft in einem Hauptwärmetauscher abgekühlt und einem Rektifiziersystem zugeführt wird, eine flüssige Fraktion in dem Rektifiziersystem gewonnen und in einem Tank gespeichert wird, zumindest ein Teil der flüssigen Fraktion aus dem Tank entnommen und auf einen erhöhten Druck gebracht wird,
und im normalen Betrieb die auf erhöhten Druck gebrachte flüssige Fraktion in einem Vorwärmetauscher erwärmt und in dem Hauptwärmetauscher verdampft wird, wobei Produktgas unter erhöhtem Druck gewonnen wird,
während bei einer Betriebsstörung zumindest ein Teil des Flüssigproduktes aus dem Tank entnommen, verdampft und zur Notversorgung verwendet wird. Process for the low-temperature air separation of air by rectification, whereby compressed compressed air is cooled in a main heat exchanger and fed to a rectification system, a liquid fraction is obtained in the rectification system and stored in a tank, at least part of the liquid fraction is removed from the tank and brought to an increased pressure,
and in normal operation the liquid fraction brought to increased pressure is heated in a preheater and evaporates in the main heat exchanger, whereby product gas is obtained under increased pressure,
while in the event of a malfunction at least part of the liquid product is removed from the tank, evaporated and used for emergency supply. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die auf erhöhten Druck gebrachte flüssige Fraktion in indirektem Wärmeaustausch mit einer in dem Rektifiziersystem gewonnenen Fraktion erwärmt wird.A method according to claim 1, characterized in that the increased Pressurized liquid fraction in indirect heat exchange with an in the fraction obtained in the rectification system is heated. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß die auf erhöhten Druck gebrachte flüssige Fraktion in indirektem Wärmeaustausch mit der in den Tank geführten Fraktion erwärmt wird.A method according to claim 2, characterized in that the increased Pressurized liquid fraction in indirect heat exchange with that in the Tank guided fraction is heated. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die auf erhöhten Druck gebrachte flüssige Fraktion in indirektem Wärmeaustausch mit der aus dem Hauptwärmetauscher austretenden, verdichteten Einsatzluft erwärmt wird.A method according to claim 1, characterized in that the increased Pressurized liquid fraction in indirect heat exchange with the the compressed heat exiting the main heat exchanger is heated. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß Sauerstoff als flüssige Fraktion gewonnen wird.Method according to one of claims 1 to 4, characterized in that Oxygen is obtained as a liquid fraction. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß Stickstoff als flüssige Fraktion gewonnen wird. Method according to one of claims 1 to 5, characterized in that Nitrogen is obtained as a liquid fraction. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß bei einer Betriebsstörung die flüssige Fraktion in indirektem Wärmeaustausch mit Luft oder Wasser verdampft wird.Method according to one of claims 1 to 6, characterized in that at the liquid fraction in indirect heat exchange with a malfunction Air or water is evaporated. Vorrichtung zur Tieftemperaturzerlegung von Luft mit einem Rektifiziersystem, einer Einsatzluftleitung, die in einen Hauptwärmetauscher und von diesem in das Rektifiziersystem führt mit einer Leitung zur Entnahme einer flüssigen Fraktion aus dem Rektifiziersystem und zu deren Einleitung in einen Tank, einer Flüssigproduktleitung für die flüssige Fraktion von dem Tank zu einem Vorwärmetauscher, einer Verbindung zwischen dem Vorwärmetauscher und dem Hauptwärmetauscher, einer Produktleitung zur Entnahme der verdampften flüssigen Fraktion als gasförmiges Druckprodukt aus dem Hauptwärmetauscher, einer in der Flüssigproduktleitung angeordneten Vorrichtung zur Druckerhöhung der flüssigen Fraktion, und einer stromabwärts der Vorrichtung zur Druckerhöhung der flüssigen Fraktion von der Flüssigproduktleitung abzweigenden Leitung zu einer Verdampfungsvorrichtung zur Notversorgung. Device for the low-temperature separation of air with a rectification system, a feed air line that leads into a main heat exchanger and from there into the rectification system with a line for removing a liquid fraction from the rectification system and for introducing it into a tank, a liquid product line for the liquid fraction from the tank to a preheater, a connection between the pre-heat exchanger and the main heat exchanger, a product line for removing the vaporized liquid fraction as a gaseous pressure product from the main heat exchanger, a device arranged in the liquid product line for increasing the pressure of the liquid fraction, and a line downstream of the device for increasing the pressure of the liquid fraction from the liquid product line to an evaporation device for emergency supply. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß der Vorwärmetauscher in der Leitung zur Entnahme der flüssigen Fraktion aus dem Rektifiziersystem angeordnet ist.Apparatus according to claim 8, characterized in that the Pre-heat exchanger in the line for removing the liquid fraction from the Rectification system is arranged. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß der Vorwärmetauscher in der Einsatzluftleitung stromabwärts des Hauptwärmetauschers angeordnet ist.Apparatus according to claim 8, characterized in that the Pre-heat exchanger in the feed air line downstream of the Main heat exchanger is arranged.
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Families Citing this family (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6295840B1 (en) 2000-11-15 2001-10-02 Air Products And Chemicals, Inc. Pressurized liquid cryogen process
GB0219415D0 (en) * 2002-08-20 2002-09-25 Air Prod & Chem Process and apparatus for cryogenic separation process
FR2849172A1 (en) * 2002-12-19 2004-06-25 Air Liquide Improved air distillation process, for oxygen production, uses vaporized gas from storage for at least partial pressurization of adsorber ending regeneration phase
FR2853407B1 (en) * 2003-04-02 2012-12-14 Air Liquide METHOD AND INSTALLATION FOR SUPPLYING GAS UNDER PRESSURE
FR2855598B1 (en) * 2003-05-28 2005-10-07 Air Liquide METHOD AND INSTALLATION FOR SUPPLYING PRESSURE GAS RELIEF BY CRYOGENIC LIQUID VAPORIZATION
FR2872262B1 (en) * 2004-06-29 2010-11-26 Air Liquide METHOD AND INSTALLATION FOR PROVIDING SUPPORT OF A PRESSURIZED GAS
DE102005029274A1 (en) * 2004-08-17 2006-02-23 Linde Ag Obtaining gaseous pressure product, by cryogenic separation of air implementing normal operation, emergency operation, and bypass operation
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
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
DE102011015233A1 (en) * 2011-03-25 2012-09-27 Linde Ag Apparatus for the 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
DE102011112909A1 (en) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Process and apparatus for recovering steel
EP2600090B1 (en) 2011-12-01 2014-07-16 Linde Aktiengesellschaft Method and device for generating pressurised oxygen by cryogenic decomposition of air
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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
WO2014154339A2 (en) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Method for air separation and air separation plant
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5408831A (en) * 1992-12-30 1995-04-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure
EP0681153A1 (en) * 1994-05-04 1995-11-08 Linde Aktiengesellschaft Process and apparatus for the low temperature separation of air
US5526647A (en) * 1994-07-29 1996-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure at a variable flow rate
US5566556A (en) * 1993-06-07 1996-10-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
EP0848220A1 (en) * 1996-12-12 1998-06-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and plant for supplying an air gas at variable quantities

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1166565A (en) * 1956-01-04 1958-11-13 Union Carbide & Carbon Corp Process and installation for separation by rectification of gas mixtures
GB929798A (en) * 1960-04-11 1963-06-26 British Oxygen Co Ltd Low temperature separation of air
FR2670278B1 (en) * 1990-12-06 1993-01-22 Air Liquide METHOD AND INSTALLATION FOR AIR DISTILLATION IN A VARIABLE REGIME FOR THE PRODUCTION OF GASEOUS OXYGEN.
JP2909678B2 (en) * 1991-03-11 1999-06-23 レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Method and apparatus for producing gaseous oxygen under pressure
CN1071444C (en) * 1992-02-21 2001-09-19 普拉塞尔技术有限公司 Cryogenic air separation system for producing gaseous oxygen
GB9521996D0 (en) * 1995-10-27 1996-01-03 Boc Group Plc Air separation

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5408831A (en) * 1992-12-30 1995-04-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure
US5566556A (en) * 1993-06-07 1996-10-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
EP0681153A1 (en) * 1994-05-04 1995-11-08 Linde Aktiengesellschaft Process and apparatus for the low temperature separation of air
US5526647A (en) * 1994-07-29 1996-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure at a variable flow rate
EP0848220A1 (en) * 1996-12-12 1998-06-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and plant for supplying an air gas at variable quantities

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HUP9801620A1 (en) 1999-03-29
DK0895045T3 (en) 2003-03-03
DE19732887A1 (en) 1999-02-04
HU9801620D0 (en) 1998-09-28
DE59806410D1 (en) 2003-01-09
PL186823B1 (en) 2004-03-31
US6038885A (en) 2000-03-21
EP0895045B1 (en) 2002-11-27
EP0895045A3 (en) 1999-06-16
PL327374A1 (en) 1999-02-01
ES2187861T3 (en) 2003-06-16
BR9802805A (en) 1999-10-05

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