EP0842385A1 - Method and device for the production of variable amounts of a pressurized gaseous product - Google Patents

Method and device for the production of variable amounts of a pressurized gaseous product

Info

Publication number
EP0842385A1
EP0842385A1 EP96927545A EP96927545A EP0842385A1 EP 0842385 A1 EP0842385 A1 EP 0842385A1 EP 96927545 A EP96927545 A EP 96927545A EP 96927545 A EP96927545 A EP 96927545A EP 0842385 A1 EP0842385 A1 EP 0842385A1
Authority
EP
European Patent Office
Prior art keywords
liquid fraction
heat exchanger
pressure
heat
product
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
EP96927545A
Other languages
German (de)
French (fr)
Other versions
EP0842385B1 (en
EP0842385B2 (en
Inventor
Horst Corduan
Horst Altmeyer
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
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Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP0842385A1 publication Critical patent/EP0842385A1/en
Publication of EP0842385B1 publication Critical patent/EP0842385B1/en
Application granted granted Critical
Publication of EP0842385B2 publication Critical patent/EP0842385B2/en
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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
    • 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
    • F25J3/04006—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
    • F25J3/04218—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
    • F25J3/04309—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 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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the invention relates to a method and a device for the variable production of a gaseous pressure product by low-temperature separation of air by means of pressure increase in the liquid state and subsequent evaporation.
  • the invention is therefore based on the object of specifying a method and a device which can be operated as flexibly as possible and which in particular avoid the disadvantages described above. This object is achieved by the method according to claim 1.
  • the gaseous print product is withdrawn in liquid form from the or one of the rectification columns and buffered in a first storage tank.
  • the liquid level in the tank rises or falls depending on whether a below-average or an above-average amount of product is currently being produced.
  • the amount of liquid fraction generated in the rectification that cannot be vaporized or otherwise used (for example as a liquid product) at the moment can be introduced into the tank; Accordingly, liquid is evacuated from the tank when there is a high product requirement.
  • “Storage tank” here means any device for storing liquid. This can be, for example, an external tank with its own insulation, but also a different type of vessel, which is arranged within the low-temperature separation plant and is suitable for buffering liquid.
  • any known method can be used to increase the pressure in the liquid state, for example pressure build-up evaporation on the storage tank, utilization of a static height, pumps upstream or downstream of the storage tank, or combinations of these methods.
  • the liquid fraction is pressurized by a pump located downstream of the tank. The throughput of this pump can be controlled to vary the amount of product.
  • the method according to the invention also has a refrigeration cycle with a cycle compressor and an expansion machine.
  • a heat transfer medium in particular a process gas for air separation, is compressed therein, expanded to perform work, and returned to the circuit compressor.
  • cold is generated to compensate for insulation and exchange losses and, if necessary, for product liquefaction.
  • the circuit compressor also serves to compress the heat transfer medium, which condenses against the product to be evaporated and is buffered in a second storage tank (first partial flow of the heat transfer medium). It compresses the heat transfer medium to a pressure that corresponds to a condensation temperature that is at least approximately is equal to the vaporization temperature of the liquid pressurized fraction. At least a part of the heat transfer medium compressed in the circuit compressor is returned to the circuit compressor, in particular the second partial flow after its relaxation, or part of it. The second partial flow of the heat carrier compressed in the circuit compressor therefore does not need to be discarded or not completely, but is at least partially circulated. Refrigeration cycle and variable product evaporation are integrated in the invention; the same machine is used both for cooling and for generating the pressure required for the evaporation of the liquid fraction.
  • the first partial flow is also varied in accordance with the variable product quantity in the invention.
  • this variation can be implemented in different ways and can thus be flexibly adapted to the current needs.
  • the amount of heat carrier compressed in the circuit compressor is kept constant when there is an increased need for gaseous pressure product.
  • the variation of the first partial flow is absorbed by a corresponding variation of the second partial flow of the heat transfer medium.
  • the amount of the second partial flow is decreased / increased by the same amount by which the amount of the first partial flow is increased / decreased.
  • An increased amount of heat transfer medium liquefied in the second partial flow is temporarily stored in the second tank; an increased amount of gas in the second partial flow can be compensated for by a corresponding removal of gas (for example as a product) from the circuit; Conversely, if production is below average, a correspondingly smaller amount of gas is withdrawn from the cycle.
  • the system can be operated in a second operating mode.
  • the throughput of the second partial flow remains the same, while the variation of the first partial flow is followed up by the circuit compressor. If there is an increased need for gaseous pressure product, the amount of the second partial flow is kept constant and the amount of the heat carrier compressed in the circuit compressor is increased by the same amount as the amount of the first partial flow. Nevertheless, the The method according to the invention, even in this mode of operation, the relative fluctuations in the compressor throughput are comparatively small, since the circulation quantity can remain constant.
  • the constant proportion of the gas compressed in the circuit compressor dampens the relative fluctuations in the compressor throughput.
  • the two modes of operation can also be combined by compensating for part of the fluctuations in the first partial flow by varying the second partial flow and for another part by changing the throughput on the circuit compressor. If there is an increased need for gaseous pressure product, both the amount of the heat carrier compressed in the circuit compressor is increased and the amount of the second partial stream is reduced.
  • the rectification system has a double column consisting of a pressure column and a low pressure column, for example liquid oxygen from the bottom of the low pressure column or liquefied nitrogen from the pressure column can be used as the liquid fraction.
  • further flow of the heat transfer medium is relaxed while performing work.
  • additional cooling can be generated in the circuit
  • the amount of further electricity that is supplied to the work-relieving relaxation can be reduced when there is an increased need for gaseous pressure product and an excess of cold can thus be at least partially compensated for.
  • the work-relieving expansion of the further stream leads approximately from the inlet pressure of the circuit compressor (lower level of the refrigeration circuit) to about atmospheric pressure, and the further work relieved of pressure is withdrawn as a pressureless gas product.
  • any process stream available in the process can be used as a heat carrier for the refrigeration cycle and the evaporation of the liquid fraction, for example air or another oxygen-nitrogen mixture.
  • nitrogen from the rectification system is preferably used as the heat carrier, in the case of a double column, for example, gaseous nitrogen which is obtained at the top of the pressure column.
  • the entire cycle nitrogen is produced in the plant itself.
  • a subset of the heat transfer medium can come from an external source, for example by feeding liquid nitrogen from another system or from a tanker truck into the second storage tank.
  • the second storage tank can thus be used in addition to its buffering effect for variable print product extraction as a safety reserve (backup) for a temporary failure of the system and / or as a buffer for liquid product.
  • the use of nitrogen as a heat transfer medium has the advantage that the refrigeration cycle and the evaporation of printed products have no negative effects on the rectification, as would be the case with the supply of air liquefied against the pressurized product and with the feeding of gaseous air from an expansion machine into a low-pressure column. Rectification can thus be optimal in the process according to the invention using nitrogen as the heat transfer medium be driven.
  • the process is therefore also suitable for high product purities and yields, as well as for the extraction of argon following air separation in the narrower sense (eg crude argon column connected to the low pressure column of a double column).
  • the main heat exchanger system has a heat exchanger block in which both the cooling of the feed air and the evaporation of the liquid fraction are carried out under increased pressure.
  • the main heat exchanger system has a plurality of heat exchanger blocks, in particular a first and a second heat exchanger block, the cooling of the feed air being carried out in the first heat exchanger block and the evaporation of the liquid fraction under increased pressure in the second heat exchanger block.
  • the two heat exchanger blocks are coupled by a compensating current which is taken from one of the two heat exchanger blocks between the warm and cold ends and fed to the other of the two heat exchanger blocks between the warm and cold ends.
  • the invention also relates to a device according to claim 8.
  • Compressed and cleaned feed air 10 is cooled under a pressure of 5 to 10 bar, preferably 5.5 to 6.5 bar in the heat exchanger 11, which forms the main heat exchanger system with the heat exchanger 12. Via line 13, it is introduced into a pressure column 14 at approximately dew point temperature.
  • the pressure column belongs to the rectification system, which also has a low pressure column 15, which is operated at a pressure of 1.3 to 2 bar, preferably 1.5 to 1.7 bar.
  • Pressure column 14 and Niederbuchklaie 15 are thermally coupled via a main capacitor 16.
  • Bottom liquid 17 from the pressure column 14 is subcooled in a counterflow 18 against product flows of the low pressure column and fed into the low pressure column 15 (line 19).
  • Gaseous nitrogen 20 from the top of the pressure column 14 is liquefied in the main condenser 16 against evaporating liquid in the bottom of the low pressure column 15.
  • Some of the condensate 21 is fed as a return to the pressure column 14 (line 22) and another part 23 is introduced into a separator 25 after supercooling 18 (FIG. 24).
  • the low-pressure column 15 is supplied with return liquid from the separator 25 (line 26).
  • Low pressure nitrogen 27 and impure nitrogen 28 are heated to approximately ambient temperature after removal from the low pressure column 15 in the heat exchangers 18 and 11.
  • the impure nitrogen 30 can be used to regenerate a molecular sieve (not shown) for air purification; the low-pressure nitrogen 29 is either discharged as a product or used in an evaporative cooler to cool cooling water.
  • Oxygen is withdrawn as a liquid fraction via line 31 from the bottom of the low-pressure column 15, supercooled (18) and introduced into a liquid oxygen tank (first storage tank) 33 (32).
  • the liquid oxygen tank 33 is preferably at about atmospheric pressure.
  • Liquid oxygen 34 from the first storage tank 33 is brought to an increased pressure of, for example, 5 to 80 bar by means of a pump 35, depending on the product pressure required. (Of course, other methods for increasing the pressure in the liquid phase can also be used, for example by utilizing a hydrostatic potential or by pressure build-up evaporation in a storage tank.)
  • the liquid high-pressure oxygen 36 is evaporated in the heat exchanger 12 and removed as an internally compressed gaseous product 37.
  • the part of the gaseous nitrogen from the pressure column 14, which is not fed to the main condenser 16, is drawn off via the lines 38, 39 and 40 through the heat exchanger 11 and fed as a heat transfer medium to a cold circuit, which includes a two-stage cycle compressor 41, 42 and one Expansion turbine 43 includes.
  • the nitrogen from for example, compression stage pressure is compressed to a pressure that corresponds to a nitrogen condensation temperature that is at least approximately equal to the evaporation temperature of the liquid pressurized oxygen 36.
  • this pressure is, for example, 15 to 60 bar.
  • a first partial stream 45 of the highly compressed nitrogen 44 is liquefied at least partially, preferably completely or essentially completely, against the evaporating oxygen 36 and fed into a separator 46.
  • the second partial flow 59 of the nitrogen compressed in the circuit compressor is fed to the expansion turbine 43 at the high pressure and at a temperature which lies between the temperatures at the warm and at the cold end of the heat exchanger 12, and is expanded there to perform work at approximately pressure column pressure.
  • the relaxed second partial flow 60 is partly fed back through heat exchanger 12 (via 61, 62) and partly through heat exchanger 11 (via 63, 64, 39, 40) to the inlet of the circuit compressor 41, 42.
  • Liquid nitrogen from the separator 46 can be fed as a return line to the pressure column 14 via line 47 and / or introduced via line 48 into a second storage tank (liquid nitrogen tank 49) which is under a pressure of, for example, 1 to 5 bar, preferably below about atmospheric pressure .
  • the tank can also optionally be fed with excess liquid 50 from the separator 25, which is not required as a return for the low pressure column 15. If necessary, liquid nitrogen can be pressed into the separator 46 by means of a pump 51 (line 52).
  • Part of the nitrogen 53 from line 39 can be removed from the heat exchanger 11 at an intermediate temperature.
  • This part serves partly as a compensating flow 54, with the aid of which the efficiency of the main heat exchanger system 11, 12 can be improved, and partly as a further flow 55 of the heat transfer medium, which is expanded in a second expansion turbine 56 to slightly above atmospheric pressure while performing work.
  • the further stream 57 which is relaxed in terms of work, is heated in the heat exchanger 12 to approximately ambient temperature and leaves the system as a gaseous product 58.
  • Liquid oxygen and / or liquid nitrogen can be withdrawn as products from the storage tanks 33, 49 (the corresponding lines are not shown in the drawing).
  • the alternating storage has no disruptive effects on the rectification, in particular neither liquid air is fed to the rectification nor is low-pressure air fed directly into the low-pressure column.
  • a conventional argon rectification can be connected to an intermediate point 66 of the low-pressure column 15, as is indicated in the drawing by the lines shown there.
  • one of the methods and devices described in EP-B-377117 or in one of the European patent applications 95101844.9 or 95101845.6 with older seniority is preferably used.
  • the first stage 41 of the circuit compressor is also used as a product compressor in that a product stream 65 is drawn off under a pressure of preferably 8 to 35 bar, for example 20 bar, between the first and the second stage.
  • the two basic modes of operation of a method and a device according to the invention are now explained below.
  • the system is designed for a certain average amount of pressurized oxygen product. Production can fluctuate around this average value, between a minimum and a maximum value. To explain how this fluctuation is achieved, the two extreme operating cases ("Max.”, “Min.”) And the operating case of the average pressure oxygen production (“Average”) of a system that processes 190,000 NrrvVh feed air are presented in the following numerical examples .
  • the pressures are
  • Liquid oxygen tank 33 1.1 bar
  • Table 1 relates to the mode of operation in which the expansion turbine 43 for the second partial flow 59 is operated at a constant speed; in the table 2 the operating mode shown, the throughput is kept constant by the circuit compressor 41, 42. Of course, any transition between these two modes of operation is also possible in the exemplary embodiment.
  • the amounts of the respective flows for the three operating cases mentioned are given in 1000 Nm 3 / h.
  • the reference symbols in the first column of the table refer to the drawing.
  • the scheme in the drawing is divided in half by a dashed line.
  • the left half essentially contains the cold circuit and the storage tanks; the entire rectification is in the right half.
  • all flows in the right half of the drawing remain completely or essentially unchanged, the fluctuations in the production of pressurized oxygen only affect the circuit and the storage tanks. This is reflected in the first six lines of the two tables, in which all streams are mentioned that cross the dashed line; these have the same throughput in all operating cases, while the amount of evaporation changes (reference symbols 36, 37).
  • the second partial flow 59, 60 is kept constant.
  • the variation of the first partial stream 45 necessary for the evaporation is brought about by the corresponding change in the throughput through the circuit compressor (stream 44): if, for example, the production increases from the average to the maximum value, the throughput through the circuit compressor increases by approximately the same amount like the amount of product too.
  • the additional gas is made available by a corresponding reduction in the amount of gas which is withdrawn from the circuit as a further stream 55, 57, 58 through the turbine 56.
  • the fluctuating amounts of liquefied heat transfer medium (first partial flow 45) are buffered in that excess liquid is fed to the second storage tank 49 via line 48 when production is above average; Conversely, the missing liquid is fed from the liquid nitrogen tank via line 52 in the case of a small amount of product, in order to keep the return flow for the pressure column 14 constant.
  • Table 1 The numerical example of Table 1 is designed so that an average excess of liquid of 1500 NrrvVh of oxygen and nitrogen is generated. This can be continuous, intermittent or in variable form be carried away from liquid products. In addition, it is also possible with the method to change the average cooling capacity of the circuit and thus the average amount of liquid products during operation by adapting the average speeds of the turbines accordingly. The system can thus be operated particularly flexibly not only with regard to the internally compressed printed product, but also with regard to liquid production.

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Abstract

In the method proposed, charge air is fed to a cryogenic rectifying system (15, 16) where it is split up into its constituent gases, and a liquid fraction (31, 32) is taken off and passed into a first storage tank (33). The pressure of any suitable amount of the liquid fraction (34) is increased (35). The liquid fraction (36) is then evaporated under the increased pressure by indirect heat exchange (12) and converted into a pressurized gaseous product (37). A heat-transfer fluid circulates in a refrigeration circuit fitted with a compressor (41, 42). Part (45) of the flow of heat-transfer fluid (44) compressed in the compressor (41, 42) is fed to the indirect heat-exchange unit (12) where the liquid fraction (36) is evaporated and the heat-transfer fluid (44) at least partly liquefied. Another part (59) of the flow of heat-transfer fluid (44) compressed in the compressor (41, 42) is allowed to expand (43), doing useful work. Liquefied heat-transfer fluid (45, 48) is stored in a buffer storage tank (49).

Description

Verfahren und Vorrichtung zur variablen Erzeugung eines gasförmigen DruckproduktsMethod and device for the variable production of a gaseous printed product
Beschreibungdescription
Die Erfindung betrifft ein Verfahren und eine Vorrichtung zur variablen Erzeugung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft mittels Druckerhöhung im flüssigen Zustand und anschließender Verdampfung.The invention relates to a method and a device for the variable production of a gaseous pressure product by low-temperature separation of air by means of pressure increase in the liquid state and subsequent evaporation.
Die Methode, ein Flüssigprodukt eines Luftzerlegers auf Druck zu bringen und anschließend zu verdampfen, wird häufig auch als "Innenverdichtung" bezeichnet. Derartige Prozesse sind für die Gewinnung einer konstanten Menge eines unter Druck stehenden Gases altbekannt (beispielsweise DE-C-752439) und bieten gegenüber der gasförmigen Produktverdichtung den Vorteil geringerer Apparatekosten.The method of pressurizing a liquid product of an air separator and then evaporating it is often referred to as "internal compression". Such processes are well known for obtaining a constant amount of a gas under pressure (for example DE-C-752439) and offer the advantage of lower apparatus costs compared to the gaseous product compression.
Ebenfalls bekannt sind "Wechselspeicherverfahren" mit mindestens zwei Speichertanks, bei denen variable Mengen eines Luftgases unter Atmosphärendruck gewonnen werden können und trotzdem ein stationärer Betrieb der Rektifikation möglich ist (siehe beispielsweise W. Rohde, Linde-Berichte aus Technik und Wissenschaft, 54/1984, Seiten 18 bis 20).Also known are "removable storage methods" with at least two storage tanks, in which variable quantities of an air gas can be obtained under atmospheric pressure and nevertheless a stationary operation of the rectification is possible (see, for example, W. Rohde, Linde Reports from Technology and Science, 54/1984, Pages 18 to 20).
Die Druckschriften DE-B-1056633, EP-A-422974, EP-A-524785 und EP-A-556861 zeigen Prozesse, die Innenverdichtung und Wechselspeicherung kombinieren, indem sowohl das zu verdampfende Flüssigprodukt als auch bei der Verdampfung verflüssigter Wärmeträger (Luft oder Stickstoff) in Speichertanks gepuffert werden. Das Problem des variierenden Bedarfs an Wärmeträger für die Verdampfung des Flüssigprodukts wird in DE-B-1056633 dadurch gelöst, daß der jeweils nicht für die Verdampfung benötigte Anteil des Wärmeträgers arbeitsleistend entspannt und verworfen wird. Davon ist man später abgekommen und verdichtet statt dessen variable Mengen an Wärmeträger (EP-A-422974, EP-A-524785 und EP-A-556861). Während im ersten Fall ein gereinigtes Gas ungenutzt verlorengeht, treten im zweiten Fall große relative Schwankungen des Verdichterdurchsatzes auf. Beide Arten von Anlagen können nur in der jeweiligen Betriebsweise gefahren werden.The documents DE-B-1056633, EP-A-422974, EP-A-524785 and EP-A-556861 show processes that combine internal compression and alternating storage, by both the liquid product to be evaporated and the evaporation of liquefied heat transfer media (air or Nitrogen) are buffered in storage tanks. The problem of the varying need for heat transfer medium for the evaporation of the liquid product is solved in DE-B-1056633 in that the portion of the heat transfer medium that is not required for the evaporation is relaxed and discarded while performing work. This was later abandoned and instead variable amounts of heat transfer medium (EP-A-422974, EP-A-524785 and EP-A-556861) were compressed. While in the first case a cleaned gas is lost unused, in the second case there are large relative fluctuations in the compressor throughput. Both types of systems can only be operated in the respective operating mode.
Der Erfindung liegt daher die Aufgabe zugrunde, ein Verfahren und eine Vorrichtung anzugeben, die möglichst flexibel betrieben werden können und die insbesondere die oben beschriebenen Nachteile vermeiden. Diese Aufgabe wird durch das Verfahren gemäß Anspruch 1 gelöst.The invention is therefore based on the object of specifying a method and a device which can be operated as flexibly as possible and which in particular avoid the disadvantages described above. This object is achieved by the method according to claim 1.
Das gasförmig zu gewinnende Druckprodukt wird in flüssiger Form aus der oder einer der Rektifiziersäulen abgezogen und in einem ersten Speichertank gepuffert. Je nachdem, ob momentan eine unterdurchschnittliche oder eine überdurchschnittliche Produktmenge erzeugt wird, steigt oder sinkt der Flüssigkeitsstand im Tank. Beispielsweise kann diejenige Menge an in der Rektifikation erzeugter flüssiger Fraktion, die momentan nicht verdampft oder anderweitig (beispielsweise als Flüssigprodukt) verwendet werden kann, in den Tank eingeführt werden; entsprechend wird bei hohem Produktbedarf Flüssigkeit aus dem Tank zur Verdampfung geführt. Es ist aber auch möglich, die gesamte flüssige Fraktion in den Speichertank einzuleiten und jeweils die aktuell benötigte Menge zu entnehmen und der Verdampfung zuzuführen. Unter "Speichertank" ist hier jede Vorrichtung zur Flüssigkeitsspeicherung zu verstehen. Dabei kann es sich beispielsweise um einen externen Tank mit eigener Isolierung handeln, aber auch um eine andere Art von Gefäß, das innerhalb der Tieftemperaturzerlegungsanlage angeordnet und zur Pufferung von Flüssigkeit geeignet ist.The gaseous print product is withdrawn in liquid form from the or one of the rectification columns and buffered in a first storage tank. The liquid level in the tank rises or falls depending on whether a below-average or an above-average amount of product is currently being produced. For example, the amount of liquid fraction generated in the rectification that cannot be vaporized or otherwise used (for example as a liquid product) at the moment can be introduced into the tank; Accordingly, liquid is evacuated from the tank when there is a high product requirement. However, it is also possible to introduce the entire liquid fraction into the storage tank and to take out the currently required amount and feed it to the evaporation. “Storage tank” here means any device for storing liquid. This can be, for example, an external tank with its own insulation, but also a different type of vessel, which is arranged within the low-temperature separation plant and is suitable for buffering liquid.
Zur Druckerhöhung im flüssigen Zustand kann jede bekannte Methode angewandt werden, beispielsweise Druckaufbauverdampfung am Speichertank, Ausnutzung einer statischen Höhe, Pumpen stromaufwärts oder stromabwärts des Speichertanks, oder auch Kombinationen dieser Methoden. Vorzugsweise wird die flüssige Fraktion durch eine stromabwärts des Tanks angeordnete Pumpe auf Druck gebracht. Der Durchsatz dieser Pumpe kann gesteuert werden, um die Variation der Produktmenge zu bewirken.Any known method can be used to increase the pressure in the liquid state, for example pressure build-up evaporation on the storage tank, utilization of a static height, pumps upstream or downstream of the storage tank, or combinations of these methods. Preferably the liquid fraction is pressurized by a pump located downstream of the tank. The throughput of this pump can be controlled to vary the amount of product.
Das erfindungsgemäße Verfahren weist außerdem einen Kältekreislauf mit einem Kreislaufverdichter und einer Entspannungsmaschine auf. Darin wird ein Wärmeträger, insbesondere ein Prozeßgas der Luftzerlegung, verdichtet, arbeitsleistend entspannt und wieder zum Kreislaufverdichter zurückgeführt. Mit Hilfe dieses Kreislaufs wird Kälte zum Ausgleich von Isolations- und Austauschverlusten und gegebenenfalls zur Produktverflüssigung erzeugt.The method according to the invention also has a refrigeration cycle with a cycle compressor and an expansion machine. A heat transfer medium, in particular a process gas for air separation, is compressed therein, expanded to perform work, and returned to the circuit compressor. With the help of this cycle, cold is generated to compensate for insulation and exchange losses and, if necessary, for product liquefaction.
Der Kreislaufverdichter dient gleichzeitig zur Verdichtung des Wärmeträgers, der gegen das zu verdampfende Produkt kondensiert und in einem zweiten Speichertank gepuffert wird (erster Teilstrom des Wärmeträgers). Er verdichtet den Wärmeträger auf einen Druck, der einer Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatur der flüssig auf Druck gebrachten Fraktion ist. Mindestens ein Teil des im Kreislaufverdichter verdichteten Wärmeträgers wird zum Kreislaufverdichter zurückgeleitet, insbesondere der zweite Teilstrom nach seiner arbeitsleistenden Entspannung oder ein Teil davon. Der zweite Teilstrom des im Kreislaufverdichter komprimierten Wärmeträgers braucht also nicht oder nicht vollständig verworfen zu werden, sondern wird mindestens teilweise im Kreis geführt. Kältekreislauf und variable Produktverdampfung sind bei der Erfindung integriert; dieselbe Maschine dient sowohl zur Kälteerzeugung als auch zur Erzeugung des für die Verdampfung der flüssigen Fraktion benötigten Drucks.The circuit compressor also serves to compress the heat transfer medium, which condenses against the product to be evaporated and is buffered in a second storage tank (first partial flow of the heat transfer medium). It compresses the heat transfer medium to a pressure that corresponds to a condensation temperature that is at least approximately is equal to the vaporization temperature of the liquid pressurized fraction. At least a part of the heat transfer medium compressed in the circuit compressor is returned to the circuit compressor, in particular the second partial flow after its relaxation, or part of it. The second partial flow of the heat carrier compressed in the circuit compressor therefore does not need to be discarded or not completely, but is at least partially circulated. Refrigeration cycle and variable product evaporation are integrated in the invention; the same machine is used both for cooling and for generating the pressure required for the evaporation of the liquid fraction.
Selbstverständlich wird auch bei der Erfindung der erste Teilstrom entsprechend der variablen Produktmenge variiert. Diese Variation kann jedoch hier auf unterschiedliche Weise realisiert und damit flexibel an die jeweils aktuellen Bedürfnisse angepaßt werden.Of course, the first partial flow is also varied in accordance with the variable product quantity in the invention. However, this variation can be implemented in different ways and can thus be flexibly adapted to the current needs.
In einer ersten Betriebsweise wird bei erhöhtem Bedarf an gasförmigem Druckprodukt die Menge des im Kreislaufverdichter verdichteten Wärmeträgers konstant gehalten. Die Variation des ersten Teilstroms wird durch eine entsprechende Variation des zweiten Teilstroms des Wärmeträgers aufgefangen. Bei Erhöhung/Verringerung der Produktion wird die Menge des zweiten Teilstroms um denselben Betrag verringert/erhöht, um den die Menge des ersten Teilstroms erhöht/verringert wird. (Mit "Menge" werden hier molare Mengen pro Zeiteineinheit bezeichnet, die z.B. in NnrWh angegeben werden können.) Damit kann der Kreislaufverdichter konstant gefahren werden, beispielsweise mit seiner Ausiegungskapazität, eine Steuerung in Abhängigkeit von der Produktmenge ist nicht nötig. Eine erhöhte Menge an im zweiten Teilstrom verflüssigtem Wärmeträger wird im zweiten Tank zwischengespeichert; eine erhöhte Gasmenge im zweiten Teilstrom kann durch eine entsprechende Entnahme von Gas (beispielsweise als Produkt) aus dem Kreislauf kompensiert werden; umgekehrt wird bei unterdurchschnittlicher Produktion eine entsprechend geringere Menge an Gas aus dem Kreislauf entnommen.In a first mode of operation, the amount of heat carrier compressed in the circuit compressor is kept constant when there is an increased need for gaseous pressure product. The variation of the first partial flow is absorbed by a corresponding variation of the second partial flow of the heat transfer medium. When the production is increased / decreased, the amount of the second partial flow is decreased / increased by the same amount by which the amount of the first partial flow is increased / decreased. ("Quantity" here refers to molar quantities per unit of time, which can be specified, for example, in NnrWh.) This means that the circulation compressor can be operated constantly, for example with its expansion capacity, and control depending on the product quantity is not necessary. An increased amount of heat transfer medium liquefied in the second partial flow is temporarily stored in the second tank; an increased amount of gas in the second partial flow can be compensated for by a corresponding removal of gas (for example as a product) from the circuit; Conversely, if production is below average, a correspondingly smaller amount of gas is withdrawn from the cycle.
Alternativ dazu kann die Anlage in einer zweiten Betriebsweise gefahren werden. Dabei bleibt der Durchsatz des zweiten Teilstroms gleich, während die Variation des ersten Teilstroms vom Kreislaufverdichter nachgefahren wird. Bei erhöhtem Bedarf an gasförmigem Druckprodukt wird also die Menge des zweiten Teilstroms konstant gehalten und die Menge des im Kreislaufverdichter verdichteten Wärmeträgers um denselben Betrag wie die Menge des ersten Teilstroms erhöht. Dennoch sind beim erfindungsgemäßen Verfahren auch bei dieser Betriebsweise die relativen Schwankungen des Verdichterdurchsatzes vergleichweise gering, da die Kreislaufmenge konstant bleiben kann. Der gleichbleibende Anteil des im Kreislaufverdichter komprimierten Gases dämpft die relativen Ausschläge des Verdichterdurchsatzes.Alternatively, the system can be operated in a second operating mode. The throughput of the second partial flow remains the same, while the variation of the first partial flow is followed up by the circuit compressor. If there is an increased need for gaseous pressure product, the amount of the second partial flow is kept constant and the amount of the heat carrier compressed in the circuit compressor is increased by the same amount as the amount of the first partial flow. Nevertheless, the The method according to the invention, even in this mode of operation, the relative fluctuations in the compressor throughput are comparatively small, since the circulation quantity can remain constant. The constant proportion of the gas compressed in the circuit compressor dampens the relative fluctuations in the compressor throughput.
Die beiden Betriebsweisen können aber auch kombiniert werden, indem die Schwankungen des ersten Teilstroms zu einem Teil durch Variation des zweiten Teilstroms und zu einem anderen Teil durch Veränderung des Durchsatzes am Kreislaufverdichter kompensiert werden. Bei erhöhtem Bedarf an gasförmigem Druckprodukt werden dann sowohl die Menge des im Kreislaufverdichter verdichteten Wärmeträgers erhöht als auch die Menge des zweiten Teilstroms verringert.However, the two modes of operation can also be combined by compensating for part of the fluctuations in the first partial flow by varying the second partial flow and for another part by changing the throughput on the circuit compressor. If there is an increased need for gaseous pressure product, both the amount of the heat carrier compressed in the circuit compressor is increased and the amount of the second partial stream is reduced.
Je nach Bedarf kann zwischen diesen Betriebsweisen gewechselt werden, beispielsweise um Flüssigproduktentnahmen aus dem Tank zu kompensieren oder für bestimmte Zeit eine erhöhte Menge an Flüssigprodukt(en) zu liefern. Je nach Menge des zweiten Teilstroms wird bei dessen arbeitsleistender Entspannung unterschiedlich viel Kälte erzeugt.Depending on requirements, you can switch between these modes of operation, for example to compensate for liquid product withdrawals from the tank or to supply an increased amount of liquid product (s) for a certain period of time. Depending on the amount of the second partial flow, different amounts of cold are generated during its work-relieving relaxation.
In jedem Fall können bei dem erfindungsgemäßen Verfahren sämtliche Ströme, die in die Rektifiziersäule(n) eingespeist oder daraus entnommen werden, konstant bleiben. Schwankungen in der Produktmenge haben damit keinerlei Auswirkungen auf die Rektifikation. Insbesondere können in jedem betriebsfall gleichbleibend hohe Reinheiten und Ausbeuten erzielt werden.In any case, in the method according to the invention, all the currents which are fed into or removed from the rectification column (s) can remain constant. Fluctuations in the product quantity therefore have no effect on the rectification. In particular, consistently high purities and yields can be achieved in every operating case.
Falls das Rektifiziersystem eine aus Drucksäule und Niederdrucksäule bestehende Doppelsäule aufweist, kann beispielsweise flüssiger Sauerstoff vom Sumpf der Niederdrucksäule oder verflüssigter Stickstoff aus der Drucksäule als flüssige Fraktion verwendet werden.If the rectification system has a double column consisting of a pressure column and a low pressure column, for example liquid oxygen from the bottom of the low pressure column or liquefied nitrogen from the pressure column can be used as the liquid fraction.
In einer günstigen Ausführungsform wird weiterer Strom des Wärmeträgers arbeitsleistend entspannt. Dadurch kann einerseits zusätzlich Kälte in dem Kreislauf erzeugt werden, andererseits ist eine weitere Möglichkeit zur genaueren Anpassung der Kälteleistung an den momentanen Bedarf gegeben, die unabhängig von der Regelung des Kreislaufverdichters und des zweiten Teilstroms ist. Insbesondere kann die Menge des weiteren Stroms, die der arbeitsleistenden Entspannung zugeführt wird, bei erhöhtem Bedarf an gasförmigem Druckprodukt erniedrigt werden und damit ein Überschuß an Kälte mindestens teilweise kompensiert werden. Vorzugsweise führt die arbeitsleistende Entspannung des weiteren Stroms etwa von dem Eintrittsdruck des Kreislaufverdichters (unteres Niveau des Kältekreislaufs) auf etwa Atmosphärendruck und der arbeitsleistend entspannte weitere Strom wird als druckloses Gasprodukt abgezogen. Damit lassen sich auch Schwankungen der im Kreislauf zirkulierenden Gasmenge auffangen. Insbesondere kann beispielsweise bei der ersten Betriebsweise (konstanter Durchsatz am Kreislaufverdichter) eine Verringerung der Menge des zweiten Teilstroms durch eine entsprechende Erniedrigung der Menge des arbeitsleistend entspannten weiteren Stroms ausgeglichen werden. Bei der zweiten Betriebsweise (konstanter Durchsatz bei der arbeitsleistenden Entspannung des zweiten Teilstroms) kann zum Beispiel eine Erhöhung des Kreislaufverdichterdurchsatzes durch eine Veringerung der Gasmenge kompensiert werden, die als weiterer Strom den Kreislauf verläßt.In a favorable embodiment, further flow of the heat transfer medium is relaxed while performing work. As a result, on the one hand, additional cooling can be generated in the circuit, on the other hand, there is another possibility for more precise adaptation of the cooling capacity to the current demand, which is independent of the regulation of the circuit compressor and the second partial flow. In particular, the amount of further electricity that is supplied to the work-relieving relaxation can be reduced when there is an increased need for gaseous pressure product and an excess of cold can thus be at least partially compensated for. Preferably, the work-relieving expansion of the further stream leads approximately from the inlet pressure of the circuit compressor (lower level of the refrigeration circuit) to about atmospheric pressure, and the further work relieved of pressure is withdrawn as a pressureless gas product. This also allows fluctuations in the amount of gas circulating in the circuit to be absorbed. In particular, in the first mode of operation (constant throughput at the circuit compressor), a reduction in the amount of the second partial stream can be compensated for by a corresponding reduction in the amount of the further stream which is relaxed during work. In the second mode of operation (constant throughput in the work relieving pressure of the second partial flow), for example, an increase in the circulation compressor throughput can be compensated for by a reduction in the amount of gas which leaves the circuit as a further flow.
Grundsätzlich kann jeder in dem Verfahren verfügbare Prozeßstrom als Wärmeträger für den Kältekreislauf und die Verdampfung der flüssigen Fraktion verwendet werden, beispielsweise Luft oder auch ein anderes Sauerstoff-Stickstoff-Gemisch. Bevorzugt wird jedoch Stickstoff aus dem Rektifiziersystem als Wärmeträger eingesetzt, im Falle einer Doppelsäule beispielsweise gasförmiger Stickstoff, der am Kopf der Drucksäule anfällt. In der Regel wird der gesamte Kreislaufstickstoff in der Anlage selbst produziert. Zusätzlich kann jedoch eine Teilmenge des Wärmeträgers aus einer äußeren Quelle stammen, beispielsweise durch Einspeisung von Flüssigstickstoff aus einer anderen Anlage oder aus einem Tankwagen in den zweiten Speichertank.In principle, any process stream available in the process can be used as a heat carrier for the refrigeration cycle and the evaporation of the liquid fraction, for example air or another oxygen-nitrogen mixture. However, nitrogen from the rectification system is preferably used as the heat carrier, in the case of a double column, for example, gaseous nitrogen which is obtained at the top of the pressure column. As a rule, the entire cycle nitrogen is produced in the plant itself. In addition, however, a subset of the heat transfer medium can come from an external source, for example by feeding liquid nitrogen from another system or from a tanker truck into the second storage tank.
Wenn Stickstoff als Produkt gewonnen wird, kann somit der zweite Speichertank neben seiner Pufferwirkung für die variable Druckproduktgewinnung auch als Sicherheitsreserve (Backup) für einen zeitweisen Ausfall der Anlage und/oder als Puffer für Flüssigprodukt eingesetzt werden.If nitrogen is obtained as a product, the second storage tank can thus be used in addition to its buffering effect for variable print product extraction as a safety reserve (backup) for a temporary failure of the system and / or as a buffer for liquid product.
Außerdem hat die Verwendung von Stickstoff als Wärmeträger den Vorteil, daß Kältekreislauf und Druckproduktverdampfung keinerlei negative Auswirkungen auf die Rektifikation hat, wie es bei der Zuspeisung von gegen Druckprodukt verflüssigter Luft und bei der Einspeisung von gasförmiger Luft aus einer Entspannungsmaschine in eine Niederdrucksäule der Fall wäre. Die Rektifikation kann also bei dem erfindungsgemäßen Verfahren mit Einsatz von Stickstoff als Wärmeträger optimal gefahren werden. Das Verfahren ist damit auch für hohe Produktreinheiten und - ausbeuten geeignet, ebenso wie für die Gewinnung von Argon im Anschluß an die Luftzerlegung im engeren Sinne (z.B. an die Niederdrucksäule einer Doppelsäule angeschlossene Rohargonsäule).In addition, the use of nitrogen as a heat transfer medium has the advantage that the refrigeration cycle and the evaporation of printed products have no negative effects on the rectification, as would be the case with the supply of air liquefied against the pressurized product and with the feeding of gaseous air from an expansion machine into a low-pressure column. Rectification can thus be optimal in the process according to the invention using nitrogen as the heat transfer medium be driven. The process is therefore also suitable for high product purities and yields, as well as for the extraction of argon following air separation in the narrower sense (eg crude argon column connected to the low pressure column of a double column).
Es ist günstig, wenn die Einsatzluft für das Rektifiziersystem in einem Hauptwärmetauschersystem abgekühlt wird, in dem auch die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt wird. Durch diese Integraton der Wärmeaustauschvorgänge können die Austauschverluste gering gehalten werden.It is advantageous if the feed air for the rectification system is cooled in a main heat exchanger system, in which the liquid fraction is also evaporated under increased pressure. By integrating the heat exchange processes, the exchange losses can be kept low.
Dies kann zum einen dadurch realisiert werden, daß das Hauptwärmetauschersystem einen Wärmetauscherblock aufweist, in dem sowohl die Abkühlung der Einsatzluft als auch die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt werden.On the one hand, this can be achieved in that the main heat exchanger system has a heat exchanger block in which both the cooling of the feed air and the evaporation of the liquid fraction are carried out under increased pressure.
Apparativ weniger aufwendig ist es jedoch, wenn das Hauptwärmetauschersystem mehrere Waärmetauscherblöcke aufweist, insbesondere einen ersten und einen zweiten Wärmetauscherblock, wobei in dem ersten Wärmetauscherblock die Abkühlung der Einsatzluft und in dem zweiten Wärmetauscherblock die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt wird. In diesem Fall ist es günstig, wenn die beiden Wärmetauscherblöcke durch einen Ausgleichsstrom gekoppelt sind, der einem der beiden Wärmetauscherblöcke zwischen dem warmen und kalten Ende entnommen und dem anderen der beiden Wärmetauscherblöcke zwischen dem warmen und kalten Ende zugeführt wird.However, it is less expensive in terms of equipment if the main heat exchanger system has a plurality of heat exchanger blocks, in particular a first and a second heat exchanger block, the cooling of the feed air being carried out in the first heat exchanger block and the evaporation of the liquid fraction under increased pressure in the second heat exchanger block. In this case, it is advantageous if the two heat exchanger blocks are coupled by a compensating current which is taken from one of the two heat exchanger blocks between the warm and cold ends and fed to the other of the two heat exchanger blocks between the warm and cold ends.
Die Erfindung betrifft außerdem eine Vorrichtung gemäß Anspruch 8.The invention also relates to a device according to claim 8.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand des Ausführungsbeispiels des Linde-VARIPOX®-Verfahrens (VARiable Internal Pressurization of OXygen) und der entsprechenden Anlage näher erläutert, die in den Zeichnungen schematisch dargestellt sind.The invention and further details of the invention are explained in more detail below with reference to the exemplary embodiment of the Linde VARIPOX® method (VARiable Internal Pressurization of OXygen) and the corresponding system, which are shown schematically in the drawings.
Verdichtete und gereinigte Einsatzluft 10 wird unter einem Druck von 5 bis 10 bar, vorzugsweise 5,5 bis 6,5 bar im Wärmetauscher 11 abgekühlt, der mit dem Wärmetauscher 12 das Hauptwärmetauschersystem bildet. Über Leitung 13 wird sie bei etwa Taupunktstemperatur in eine Drucksäule 14 eingeleitet. Die Drucksäule gehört zu dem Rektifiziersystem, das außerdem eine Niederdrucksäule 15 aufweist, die bei einem Druck von 1 ,3 bis 2 bar, vorzugsweise 1 ,5 bis 1 ,7 bar betrieben wird. Drucksäule 14 und Niederdrucksäuie 15 sind über einen Hauptkondensator 16 thermisch gekoppelt.Compressed and cleaned feed air 10 is cooled under a pressure of 5 to 10 bar, preferably 5.5 to 6.5 bar in the heat exchanger 11, which forms the main heat exchanger system with the heat exchanger 12. Via line 13, it is introduced into a pressure column 14 at approximately dew point temperature. The pressure column belongs to the rectification system, which also has a low pressure column 15, which is operated at a pressure of 1.3 to 2 bar, preferably 1.5 to 1.7 bar. Pressure column 14 and Niederdrucksäuie 15 are thermally coupled via a main capacitor 16.
Sumpfflüssigkeit 17 aus der Drucksäule 14 wird in einem Gegenströmer 18 gegen Produktströme der Niederdrucksäule unterkühlt und in die Niederdrucksäule 15 eingespeist (Leitung 19). Gasförmiger Stickstoff 20 vom Kopf der Drucksäule 14 wird im Hauptkondensator 16 gegen verdampfende Flüssigkeit im Sumpf der Niederdrucksäule 15 verflüssigt. Das Kondensat 21 wird zu einem Teil als Rücklauf auf die Drucksäule 14 aufgegeben (Leitung 22) und zu einem anderen Teil 23 nach Unterkühlung 18 in einen Abscheider 25 eingeführt (24). Die Niederdrucksäule 15 wird aus dem Abscheider 25 mit Rücklaufflüssigkeit versorgt (Leitung 26).Bottom liquid 17 from the pressure column 14 is subcooled in a counterflow 18 against product flows of the low pressure column and fed into the low pressure column 15 (line 19). Gaseous nitrogen 20 from the top of the pressure column 14 is liquefied in the main condenser 16 against evaporating liquid in the bottom of the low pressure column 15. Some of the condensate 21 is fed as a return to the pressure column 14 (line 22) and another part 23 is introduced into a separator 25 after supercooling 18 (FIG. 24). The low-pressure column 15 is supplied with return liquid from the separator 25 (line 26).
Niederdruckstickstoff 27 und unreiner Stickstoff 28 werden nach Entnahme aus der Niederdrucksäule 15 in den Wärmetauschern 18 und 11 auf etwa Umgebungstemperatur angewärmt. Der unreine Stickstoff 30 kann zur Regenerierung eines nicht dargestellten Molekularsiebs für die Luftreinigung eingesetzt werden; der Niederdruckstickstoff 29 wird entweder als Produkt abgeführt oder in einem Verdunstungskühler zur Abkühlung von Kühlwasser verwendet.Low pressure nitrogen 27 and impure nitrogen 28 are heated to approximately ambient temperature after removal from the low pressure column 15 in the heat exchangers 18 and 11. The impure nitrogen 30 can be used to regenerate a molecular sieve (not shown) for air purification; the low-pressure nitrogen 29 is either discharged as a product or used in an evaporative cooler to cool cooling water.
Sauerstoff wird als flüssige Fraktion über Leitung 31 aus dem Sumpf der Niederdrucksäule 15 abgezogen, unterkühlt (18) und in einen Flüssigsauerstofftank (ersten Speichertank) 33 eingeführt (32). Der Flüssigsauerstofftank 33 steht vorzugsweise unter etwa Atmosphärendruck . Flüssiger Sauerstoff 34 aus dem ersten Speichertank 33 wird mittels einer Pumpe 35 auf einen erhöhten Druck von beispielsweise 5 bis 80 bar gebracht, je nach benötigtem Produktdruck . (Selbstverständlich sind auch andere Methoden zur Druckerhöhung in der flüssigen Phase anwendbar, beispielsweise durch Ausnutzung eines hydrostatischen Potentials oder durch Druckaufbauverdampfung an einem Speichertank.) Der flüssige Hochdrucksauerstoff 36 wird im Wärmetauscher 12 verdampft und als innenverdichtetes gasförmiges Produkt 37 abgezogen.Oxygen is withdrawn as a liquid fraction via line 31 from the bottom of the low-pressure column 15, supercooled (18) and introduced into a liquid oxygen tank (first storage tank) 33 (32). The liquid oxygen tank 33 is preferably at about atmospheric pressure. Liquid oxygen 34 from the first storage tank 33 is brought to an increased pressure of, for example, 5 to 80 bar by means of a pump 35, depending on the product pressure required. (Of course, other methods for increasing the pressure in the liquid phase can also be used, for example by utilizing a hydrostatic potential or by pressure build-up evaporation in a storage tank.) The liquid high-pressure oxygen 36 is evaporated in the heat exchanger 12 and removed as an internally compressed gaseous product 37.
Der Teil des gasförmigen Stickstoffs aus der Drucksäule 14, der nicht dem Hauptkondensator 16 zugeführt wird, wird über die Leitungen 38, 39 und 40 durch den Wärmetauscher 11 abgezogen und als Wärmeträger einem Kaltekreislauf zugeführt, der unter anderem einen zweistufigen Kreislaufverdichter 41 , 42 und eine Entspannungsturbine 43 umfaßt. Im Kreislaufverdichter 41 , 42 wird der Stickstoff von etwa Druckstufendruck auf einen Druck komprimiert, der einer Stickstoff- Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatur des flüssigen Drucksauerstoffs 36 ist. Dieser Druck beträgt - je nach vorgegebenem Abgabedruck des Sauerstoffs - beispielsweise 15 bis 60 bar. Ein erster Teilstrom 45 des hochverdichteten Stickstoffs 44 wird gegen den verdampfenden Sauerstoff 36 mindestens teilweise, vorzugsweise vollständig oder im wesentlichen vollständig verflüssigt und in einen Abscheider 46 eingespeist.The part of the gaseous nitrogen from the pressure column 14, which is not fed to the main condenser 16, is drawn off via the lines 38, 39 and 40 through the heat exchanger 11 and fed as a heat transfer medium to a cold circuit, which includes a two-stage cycle compressor 41, 42 and one Expansion turbine 43 includes. In the cycle compressor 41, 42 the nitrogen from for example, compression stage pressure is compressed to a pressure that corresponds to a nitrogen condensation temperature that is at least approximately equal to the evaporation temperature of the liquid pressurized oxygen 36. Depending on the specified delivery pressure of the oxygen, this pressure is, for example, 15 to 60 bar. A first partial stream 45 of the highly compressed nitrogen 44 is liquefied at least partially, preferably completely or essentially completely, against the evaporating oxygen 36 and fed into a separator 46.
Der zweite Teilstrom 59 des im Kreislaufverdichter komprimierten Stickstoffs wird bei dem hohen Druck und bei einer Temperatur, die zwischen den Temperaturen am warmen und am kalten Ende des Wärmetauschers 12 liegt, der Entspannungsturbine 43 zugeleitet und dort auf etwa Drucksäulendruck arbeitsleistend entspannt. Der entspannte zweite Teilstrom 60 wird zum einen Teil durch Wärmetauscher 12 (über 61, 62), zum anderen Teil durch Wärmetauscher 11 (über 63, 64, 39, 40) zum Eintritt des Kreislaufverdichters 41 , 42 zurückgeführt.The second partial flow 59 of the nitrogen compressed in the circuit compressor is fed to the expansion turbine 43 at the high pressure and at a temperature which lies between the temperatures at the warm and at the cold end of the heat exchanger 12, and is expanded there to perform work at approximately pressure column pressure. The relaxed second partial flow 60 is partly fed back through heat exchanger 12 (via 61, 62) and partly through heat exchanger 11 (via 63, 64, 39, 40) to the inlet of the circuit compressor 41, 42.
Flüssiger Stickstoff aus dem Abscheider 46 kann über Leitung 47 als Rücklauf auf die Drucksäule 14 aufgegeben und/oder über Leitung 48 in einen zweiten Speichertank (Flüssigstickstofftank 49) eingeführt werden, der unter einem Druck von beispielsweise 1 bis 5 bar, vorzugsweise unter etwa Atmosphärendruck steht. Der Tank kann außerdem gegebenenfalls von überschüssiger Flüssigkeit 50 aus dem Abscheider 25 gespeist werden, die nicht als Rücklauf für die Niederdrucksäule 15 benötigt wird. Bei Bedarf kann flüssiger Stickstoff mittels einer Pumpe 51 in den Abscheider 46 gedrückt werden (Leitung 52).Liquid nitrogen from the separator 46 can be fed as a return line to the pressure column 14 via line 47 and / or introduced via line 48 into a second storage tank (liquid nitrogen tank 49) which is under a pressure of, for example, 1 to 5 bar, preferably below about atmospheric pressure . The tank can also optionally be fed with excess liquid 50 from the separator 25, which is not required as a return for the low pressure column 15. If necessary, liquid nitrogen can be pressed into the separator 46 by means of a pump 51 (line 52).
Ein Teil des Stickstoffs 53 aus Leitung 39 kann bei einer Zwischentemperatur aus dem Wärmetauscher 11 entnommen werden. Dieser Teil dient teilweise als Ausgleichsstrom 54, mit dessen Hilfe die Effizienz des Hauptwärmetauschersystems 11, 12 verbessert werden kann, und teilweise als weiterer Strom 55 des Wärmeträgers, der in einer zweiten Entspannungsturbine 56 arbeitsleistend auf etwas über Atmosphärendruck entspannt wird. Der arbeitsleistend entspannte weitere Strom 57 wird im Wärmetauscher 12 auf etwa Umgebungstemperatur angewärmt und verläßt die Anlage als gasförmiges Produkt 58.Part of the nitrogen 53 from line 39 can be removed from the heat exchanger 11 at an intermediate temperature. This part serves partly as a compensating flow 54, with the aid of which the efficiency of the main heat exchanger system 11, 12 can be improved, and partly as a further flow 55 of the heat transfer medium, which is expanded in a second expansion turbine 56 to slightly above atmospheric pressure while performing work. The further stream 57, which is relaxed in terms of work, is heated in the heat exchanger 12 to approximately ambient temperature and leaves the system as a gaseous product 58.
Aus den Speichertanks 33, 49 können flüssiger Sauerstoff und/oder flüssiger Stickstoff als Produkte abgezogen werden (die entsprechenden Leitungen sind in der Zeichnung nicht dargestellt). Die Wechselspeicherung hat bei dem erfindungsgemäßen Verfahren keinerlei störende Einflüsse auf die Rektifikation, insbesondere wird weder Flüssigluft der Rektifikation zugeführt, noch wird Niederdruckluft direkt in die Niederdrucksäule eingespeist. Dadurch eignet sich der Prozeß hervorragend für besonders anspruchsvolle Trennaufgaben wie die Gewinnung von Argon. Dazu kann an einer Zwischenstelle 66 der Niederdrucksäule 15 eine konventionelle Argonrektifikation angeschlossen sein, wie es in der Zeichnung durch die dort gezeigten Leitungen angedeutet ist. Bevorzugt wird dazu einer der in EP-B-377117 oder in einer der europäischen Patentanmeldungen 95101844.9 oder 95101845.6 mit älterem Zeitrang beschriebenen Verfahren und Vorrichtungen eingesetzt.Liquid oxygen and / or liquid nitrogen can be withdrawn as products from the storage tanks 33, 49 (the corresponding lines are not shown in the drawing). In the method according to the invention, the alternating storage has no disruptive effects on the rectification, in particular neither liquid air is fed to the rectification nor is low-pressure air fed directly into the low-pressure column. This makes the process ideal for particularly demanding separation tasks such as the extraction of argon. For this purpose, a conventional argon rectification can be connected to an intermediate point 66 of the low-pressure column 15, as is indicated in the drawing by the lines shown there. For this purpose, one of the methods and devices described in EP-B-377117 or in one of the European patent applications 95101844.9 or 95101845.6 with older seniority is preferably used.
In dem Beispiel wird die erste Stufe 41 des Kreislaufverdichters auch als Produktverdichter verwendet, indem zwischen der ersten und der zweiten Stufe ein Produktstrom 65 unter einem Druck von vorzugsweise 8 bis 35 bar, beispielsweise 20 bar abgezogen wird.In the example, the first stage 41 of the circuit compressor is also used as a product compressor in that a product stream 65 is drawn off under a pressure of preferably 8 to 35 bar, for example 20 bar, between the first and the second stage.
Im folgenden werden nun die beiden grundsätzlichen Betriebsweisen eines Verfahrens und einer Vorrichtung gemäß der Erfindung erläutert. Die Anlage ist für eine bestimmte mittlere Menge an Drucksauerstoffprodukt ausgelegt. Die Produktion kann um diesen mittleren Wert schwanken, und zwar zwischen einem minimalen und einem maximalen Wert. Zur Erläuterung, wie diese Schwankung bewerkstelligt wird, werden in den folgenden Zahlenbeispielen die beiden extremen Betriebsfälle ("Max.", "Min.") und der Betriebsfall der durchschnittlichen Drucksauerstoffproduktion ("Mittl.") einer Anlage vorgestellt, die 190.000 NrrvVh Einsatzluft verarbeitet. Die Drücke betragen dabeiThe two basic modes of operation of a method and a device according to the invention are now explained below. The system is designed for a certain average amount of pressurized oxygen product. Production can fluctuate around this average value, between a minimum and a maximum value. To explain how this fluctuation is achieved, the two extreme operating cases ("Max.", "Min.") And the operating case of the average pressure oxygen production ("Average") of a system that processes 190,000 NrrvVh feed air are presented in the following numerical examples . The pressures are
Drucksäule 14 5,1 barPressure column 14 5.1 bar
Niederdrucksäule 15 1 ,3 barLow pressure column 15 1, 3 bar
Drucksauerstoff 37 26 barPressurized oxygen 37 26 bar
Eintritt des Kreislaufverdichters 4,8 barEntry of the circuit compressor 4.8 bar
Austritt des Kreislaufverdichters 42 barOutlet of the circuit compressor 42 bar
Flüssigsauerstofftank 33 1,1 barLiquid oxygen tank 33 1.1 bar
Flüssigstickstofftank 1 ,1 barLiquid nitrogen tank 1, 1 bar
Tabelle 1 betrifft diejenige Betriebsweise, in der die Entspannungsturbine 43 für den zweiten Teilstrom 59 mit konstanter Drehzahl gefahren wird; bei der in Tabelle 2 dargestellten Betriebsweise wird der Durchsatz durch den Kreislaufverdichter 41, 42 konstant gehalten. Selbstverständlich ist auch bei dem Ausführungsbeispiel jeder beliebige Übergang zwischen diesen beiden Betriebsweisen möglich. In beiden Tabellen werden die Mengen der jeweiligen Ströme für die drei genannten Betriebsfälle in 1000 Nm3/h angegeben. Die Bezugszeichen in der ersten Tabellenspalte beziehen sich auf die Zeichnung. Table 1 relates to the mode of operation in which the expansion turbine 43 for the second partial flow 59 is operated at a constant speed; in the table 2 the operating mode shown, the throughput is kept constant by the circuit compressor 41, 42. Of course, any transition between these two modes of operation is also possible in the exemplary embodiment. In both tables, the amounts of the respective flows for the three operating cases mentioned are given in 1000 Nm 3 / h. The reference symbols in the first column of the table refer to the drawing.
Das Schema ist in der Zeichnung ist durch ein gestrichelte Linie in zwei Hälften geteilt. Die linke Hälfte enthält im wesentlichen den Kaltekreislauf und die Speichertanks; die gesamte Rektifikation befindet sich in der rechten Hälfte. Im Wechselbetrieb des Verfahrens und der Anlage bleiben alle Ströme in der rechten Hälfte der Zeichnung vollständig oder im wesentlichen unverändert, die Schwankungen in der Drucksauerstoffproduktion wirken sich nur auf den Kreislauf und die Speichertanks aus. Dies spiegelt sich in den ersten sechs Zeilen der beiden Tabellen wieder, in denen sämtliche Ströme genannt sind, die die gestrichelte Linie überschreiten; diese weisen in allen Betriebsfällen den gleichen Durchsatz auf, während sich die Verdampfungsmenge ändert (Bezugszeichen 36, 37). Insbesondere wird über Leitung 38 eine konstante Menge von 105.000 NrrvVh Stickstoff aus der Drucksäule 14 in den variablen Teil der Anlage geführt, der in den Strömen 40 und 53 von einem - ebenfalls gleichbleibenden - Teil (15.000 NrrvVh) des in der Turbine 43 entspannten zweiten Teilstroms überlagert wird. Ebenso bleibt die Entnahme von flüssigem Sauerstoffprodukt 31 , 32 aus der Niederdrucksäule 15 in allen Betriebsfällen konstant. The scheme in the drawing is divided in half by a dashed line. The left half essentially contains the cold circuit and the storage tanks; the entire rectification is in the right half. In alternating operation of the process and the system, all flows in the right half of the drawing remain completely or essentially unchanged, the fluctuations in the production of pressurized oxygen only affect the circuit and the storage tanks. This is reflected in the first six lines of the two tables, in which all streams are mentioned that cross the dashed line; these have the same throughput in all operating cases, while the amount of evaporation changes (reference symbols 36, 37). In particular, a constant amount of 105,000 NrrvVh nitrogen is fed via line 38 from the pressure column 14 into the variable part of the system, which flows 40 and 53 from a - also constant - part (15,000 NrrvVh) of the second partial flow expanded in the turbine 43 is superimposed. Likewise, the removal of liquid oxygen product 31, 32 from the low pressure column 15 remains constant in all operating cases.
In dem Zahlenbeispiel von Tabelle 1 wird der zweite Teilstrom 59, 60 konstant gehalten. Die für die Verdampfung notwendige Variation des ersten Teilstroms 45 wird durch die entsprechende Veränderung des Durchsatzes durch den Kreislaufverdichter (Strom 44) bewirkt: Erhöht sich beispielsweise die Produktion von dem durchschnittlichen auf den maximalen Wert, so nimmt der Durchsatz durch den Kreislaufverdichter etwa um denselben Betrag wie die Produktmenge zu. Das zusätzliche Gas wird durch eine entsprechende Verringerung der Gasmenge zur Verfügung gestellt, die als weiterer Strom 55, 57, 58 durch die Turbine 56 aus dem Kreislauf entnommen wird.In the numerical example in Table 1, the second partial flow 59, 60 is kept constant. The variation of the first partial stream 45 necessary for the evaporation is brought about by the corresponding change in the throughput through the circuit compressor (stream 44): if, for example, the production increases from the average to the maximum value, the throughput through the circuit compressor increases by approximately the same amount like the amount of product too. The additional gas is made available by a corresponding reduction in the amount of gas which is withdrawn from the circuit as a further stream 55, 57, 58 through the turbine 56.
Die schwankenden Mengen an verflüssigtem Wärmeträger (erster Teilstrom 45) werden dadurch gepuffert, daß bei überdurchschnittlicher Produktion über Leitung 48 überschüssige Flüssigkeit dem zweiten Speichertank 49 zugeführt wird; umgekehrt wird die fehlende Flüssigkeit bei geringer Produktmenge über Leitung 52 aus dem Flüssigstickstofftank nachgeführt, um die Rücklaufmenge für die Drucksäule 14 konstant zu halten.The fluctuating amounts of liquefied heat transfer medium (first partial flow 45) are buffered in that excess liquid is fed to the second storage tank 49 via line 48 when production is above average; Conversely, the missing liquid is fed from the liquid nitrogen tank via line 52 in the case of a small amount of product, in order to keep the return flow for the pressure column 14 constant.
Das Zahlenbeispiel von Tabelle 1 ist so ausgelegt, daß ein durchschnittlicher Überschuß an Flüssigkeit von jeweils 1500 NrrvVh Sauerstoff und Stickstoff erzeugt wird. Dieser kann kontinuierlich, intermittierend oder auch in variabler Menge in Form von Flüssigprodukten abgeführt werden. Im übrigen ist es bei dem Verfahren auch möglich, die durchschnittliche Kälteleistung des Kreislaufs und damit die mittlere Menge der Flüssigprodukte während des Betriebs zu verändern, indem die durchschnittlichen Drehzahlen der Turbinen entsprechend angepaßt werden. Die Anlage kann damit nicht nur bezüglich des innenverdichteten Druckprodukts, sondern auch hinsichtlich der Flüssigkeitsproduktion besonders flexibel betrieben werden.The numerical example of Table 1 is designed so that an average excess of liquid of 1500 NrrvVh of oxygen and nitrogen is generated. This can be continuous, intermittent or in variable form be carried away from liquid products. In addition, it is also possible with the method to change the average cooling capacity of the circuit and thus the average amount of liquid products during operation by adapting the average speeds of the turbines accordingly. The system can thus be operated particularly flexibly not only with regard to the internally compressed printed product, but also with regard to liquid production.
Im Beispiel von Tabelle 2 wird statt des zweiten Teilstroms der Durchsatz des Kreislaufverdichters 41 , 42 konstant gehalten. In the example in Table 2, the throughput of the circulation compressor 41, 42 is kept constant instead of the second partial flow.

Claims

Patentansprüche claims
1. Verfahren zur variablen Erzeugung eines gasförmigen Druckprodukts (37) durch Tieftemperaturzerlegung von Luft, bei dem Einsatzluft (10, 13) einem Rektifiziersystem (14, 15) zugeführt wird, wobei eine flüssige Fraktion (31 , 32, 34) aus dem Rektifiziersystem (14, 15) in einem ersten Speichertank (33) gepuffert, der Druck der flüssigen Fraktion (34) erhöht (35) und eine variable Menge der flüssigen Fraktion (36) unter dem erhöhten Druck durch indirekten Wärmeaustausch (12) verdampft und als gasförmiges1. A method for the variable production of a gaseous pressure product (37) by low-temperature separation of air, in which feed air (10, 13) is fed to a rectification system (14, 15), a liquid fraction (31, 32, 34) from the rectification system ( 14, 15) buffered in a first storage tank (33), the pressure of the liquid fraction (34) increased (35) and a variable amount of the liquid fraction (36) evaporated under the increased pressure by indirect heat exchange (12) and as a gas
Druckprodukt (37) gewonnen wird, wobei ferner ein Wärmeträger in einem Kältekreislauf geführt wird, der einenPrinted product (37) is obtained, wherein a heat transfer medium is also guided in a refrigeration cycle, the one
Kreislaufverdichter (41 , 42) aufweist, ein erster Teilstrom (44, 45) von im Kreislaufverdichter (41 , 42) verdichtetemCircuit compressor (41, 42) has a first partial flow (44, 45) of that compressed in the circuit compressor (41, 42)
Wärmeträger dem indirekten Wärmeaustausch (12) zur Verdampfung der flüssigen Fraktion (36) zugeführt und dabei mindestens teilweise verflüssigt wird, ein zweiter Teilstrom (44, 59) von im Kreislaufverdichter (41 , 42) verdichtetemHeat transfer medium to the indirect heat exchange (12) for evaporation of the liquid fraction (36) and at least partially liquefied, a second partial flow (44, 59) of that compressed in the circuit compressor (41, 42)
Wärmeträger (44) arbeitsleistend entspannt (43) wird und verflüssigter Wärmeträger (45, 48, 52) in einem zweiten Speichertank (49) gepuffert wird.Heat carrier (44) is relaxed (43) while performing work, and liquefied heat carrier (45, 48, 52) is buffered in a second storage tank (49).
2. Verfahren nach Anspruch 1 , dadurch gekennzeichnet, daß ein weiterer Strom (55) des Wärmeträgers arbeitsleistend entspannt (56) wird.2. The method according to claim 1, characterized in that a further stream (55) of the heat transfer medium is relaxed to perform work (56).
3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß die Menge des weiteren Stroms (55), die der arbeitsleistenden Entspannung (56) zugeführt wird, bei erhöhtem Bedarf an gasförmigem Druckprodukt (37) erniedrigt wird.3. The method according to claim 2, characterized in that the amount of further current (55), which is the work-relieving relaxation (56), is reduced when there is an increased need for gaseous pressure product (37).
4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß Stickstoff (31) aus dem Rektifiziersystem (14, 15) als Wärmeträger eingesetzt wird.4. The method according to any one of claims 1 to 3, characterized in that nitrogen (31) from the rectification system (14, 15) is used as a heat transfer medium.
5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß die Einsatzluft (10) für das Rektifiziersystem (14, 15) in einem Hauptwärmetauschersystem (11 , 12) abgekühlt wird, in dem auch die Verdampfung (12) der flüssigen Fraktion (36) unter erhöhtem Druck durchgeführt wird.5. The method according to any one of claims 1 to 4, characterized in that the feed air (10) for the rectification system (14, 15) in a main heat exchanger system (11, 12) is cooled, in which the Evaporation (12) of the liquid fraction (36) is carried out under increased pressure.
6. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß das Hauptwärmetauschersystem einen Wärmetauscherblock aufweist, in dem sowohl die Abkühlung der Einsatzluft als auch die Verdampfung der flüssigen Fraktion unter erhöhtem Druck durchgeführt werden.6. The method according to claim 5, characterized in that the main heat exchanger system has a heat exchanger block in which both the cooling of the feed air and the evaporation of the liquid fraction are carried out under increased pressure.
7. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß das Hauptwärmetauschersystem einen ersten und einen zweiten Wärmetauscherblock aufweist, wobei in dem ersten Wärmetauscherblock (11) die Abkühlung der Einsatzluft (10) und in dem zweiten Wärmetauscherbiock (12) die Verdampfung der flüssigen Fraktion (36) unter erhöhtem Druck durchgeführt wird, und wobei die beiden Wärmetauscherblöcke (11, 12) durch einen Ausgleichsstrom (54) gekoppelt sind, der einem (11) der beiden Wärmetauscherblöcke zwischen dem warmen und kalten Ende entnommen und dem anderen (12) der beiden Wärmetauscherblöcke zwischen dem warmen und kalten Ende zugeführt wird.7. The method according to claim 5, characterized in that the main heat exchanger system has a first and a second heat exchanger block, wherein in the first heat exchanger block (11) the cooling of the feed air (10) and in the second heat exchanger block (12) the evaporation of the liquid fraction ( 36) is carried out under increased pressure, and the two heat exchanger blocks (11, 12) are coupled by an equalizing current (54) which is removed from one (11) of the two heat exchanger blocks between the hot and cold ends and the other (12) of the two Heat exchanger blocks are fed between the warm and cold ends.
8. Vorrichtung zur variablen Erzeugung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft, mit einem Rektifiziersystem (14, 15), in das eine Einsatzluftleitung (10, 13) führt, mit einer Flüssigkeitsleitung (31 , 32) zur Entnahme einer flüssigen Fraktion aus dem Rektifiziersystem (14, 15) und zu deren Einleitung in einen ersten8. Device for the variable production of a gaseous pressure product by low-temperature separation of air, with a rectification system (14, 15) into which a feed air line (10, 13) leads, with a liquid line (31, 32) for removing a liquid fraction from the rectification system (14, 15) and their introduction to a first
Speichertank (33), mit Mitteln (35) zur Erhöhung des Drucks der flüssigen Fraktion (34), mit einem Wärmetauscher (12) zur Verdampfung der flüssigen Fraktion (36) unter erhöhtem Druck, mit einer Produktleitung (37) zur Entnahme der verdampften flüssigenStorage tank (33), with means (35) for increasing the pressure of the liquid fraction (34), with a heat exchanger (12) for evaporating the liquid fraction (36) under increased pressure, with a product line (37) for removing the evaporated liquid
Fraktion als gasförmiges Druckprodukt, mit einem Kältekreislauf, der einen Kreislaufverdichter (41 , 42) aufweist, mit einer ersten Teilstromleitung (44, 45), die von dem KreislaufverdichterFraction as a gaseous pressure product, with a refrigeration cycle, which has a circuit compressor (41, 42), with a first partial flow line (44, 45), which from the circuit compressor
(41 , 42) zu dem Wärmetauscher (12) zur Verdampfung der flüssigen Fraktion(41, 42) to the heat exchanger (12) to evaporate the liquid fraction
(36) verbunden ist, mit einer zweiten Teilstromleitung (44, 59), die von dem Kreislaufverdichter(36) is connected to a second partial flow line (44, 59) which is connected to the circuit compressor
(41. 42) zu einer Entspannungsmaschine (43) führt und mit einem zweiten Speichertank (49) zur Pufferung von verflüssigtem Wärmeträger (45, 48). (41, 42) leads to a relaxation machine (43) and with a second storage tank (49) for buffering liquefied heat transfer medium (45, 48).
EP96927545A 1995-07-21 1996-07-18 Method and device for the production of variable amounts of a pressurized gaseous product Expired - Lifetime EP0842385B2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19526785 1995-07-21
DE19526785A DE19526785C1 (en) 1995-07-21 1995-07-21 Method and device for the variable production of a gaseous printed product
PCT/EP1996/003175 WO1997004279A1 (en) 1995-07-21 1996-07-18 Method and device for the production of variable amounts of a pressurized gaseous product

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EP0842385A1 true EP0842385A1 (en) 1998-05-20
EP0842385B1 EP0842385B1 (en) 2001-04-18
EP0842385B2 EP0842385B2 (en) 2003-12-03

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JP (1) JP3947565B2 (en)
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CN (1) CN1134638C (en)
AU (1) AU719608B2 (en)
BR (1) BR9609781A (en)
CA (1) CA2227050A1 (en)
DE (2) DE19526785C1 (en)
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US5953937A (en) 1999-09-21
JPH11509615A (en) 1999-08-24
TW318882B (en) 1997-11-01
EP0842385B1 (en) 2001-04-18
CN1134638C (en) 2004-01-14
WO1997004279A1 (en) 1997-02-06
AU719608B2 (en) 2000-05-11
DK0842385T3 (en) 2001-08-06
ES2158336T5 (en) 2004-07-01
JP3947565B2 (en) 2007-07-25
DE19526785C1 (en) 1997-02-20
KR100421071B1 (en) 2004-04-17
CA2227050A1 (en) 1997-02-06
EP0842385B2 (en) 2003-12-03
AU6734496A (en) 1997-02-18
MX9800557A (en) 1998-04-30
KR19990035798A (en) 1999-05-25
ZA966146B (en) 1997-02-04
BR9609781A (en) 1999-12-21
DK0842385T4 (en) 2004-03-22
ES2158336T3 (en) 2001-09-01
DE59606808D1 (en) 2001-05-23
CN1191600A (en) 1998-08-26

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