EP0949471A1 - Cryogenic air separation plant with two different operation modes - Google Patents

Cryogenic air separation plant with two different operation modes Download PDF

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Publication number
EP0949471A1
EP0949471A1 EP19990106715 EP99106715A EP0949471A1 EP 0949471 A1 EP0949471 A1 EP 0949471A1 EP 19990106715 EP19990106715 EP 19990106715 EP 99106715 A EP99106715 A EP 99106715A EP 0949471 A1 EP0949471 A1 EP 0949471A1
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EP
European Patent Office
Prior art keywords
air
liquid
pressure
compressor
turbine
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
EP19990106715
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German (de)
French (fr)
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EP0949471B1 (en
Inventor
Jürgen Dipl.-Phys. Voit
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Linde GmbH
Original Assignee
Linde GmbH
Linde Technische Gase GmbH
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Application filed by Linde GmbH, Linde Technische Gase GmbH filed Critical Linde GmbH
Priority to EP19990106715 priority Critical patent/EP0949471B1/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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
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    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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    • 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
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    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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    • 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
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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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    • 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
    • F25J3/04339—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 air
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    • 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
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    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
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    • 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
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank
    • 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
    • Y10S62/90—Triple column

Definitions

  • EP 0 044 679 A1 is a process for the production of gaseous Compressed oxygen (DGOX) and small amounts of liquid oxygen (LOX) known: cold supplies for air separation and the production of liquid product Air cooling circuit. It contains a compression with two compressor stages in series Compression of an air flow in the first stage to a medium pressure for one work-relieving relaxation of a partial flow of this air to a lower pressure and a second compressor stage to compress the remaining air flow to one higher pressure for throttle relaxation to the same low pressure. After Merging the partial streams and branching off a liquid phase formed the gas phase recycles for compression and the liquid phase after splitting into two Choke currents fed to a rectification. The refrigeration cycle in such a The process cannot be switched off and the cooling capacity is reduced an energetically unfavorable operation.
  • DGOX Gaseous Compressed oxygen
  • LOX liquid oxygen
  • the object of the invention is a method and a device of the aforementioned Kind with an energetically favorable production of the gaseous printed product and of the liquid product in variable quantities and with high availability of the Generation of the printed product.
  • the gas operation of the Air flow in the refrigeration circuit is reduced to zero and a compensation of Cold losses that are no longer covered by the refrigeration cycle are extremely cold stored liquid is used.
  • This enables the generation of gaseous printed product even with a full liquid product tank, for example stored liquid product in a heat exchanger in counterflow to used air is guided, this air is cooled, partially liquefied and the Rectification is supplied or by stored liquid directly to the rectification is fed.
  • Cryogenic liquid of at least one liquid fraction from the rectification for example liquid nitrogen (LIN), liquid oxygen (LOX) or liquid air Compensation for cold losses in gas operation can be in a tank be cached, being used as a tank to store these fractions Buffer tanks and / or product tanks can be used. Most is the use of Product tanks are the cheapest solution, while liquid air is more like a buffer tank Required, since liquid air usually doesn't matter as a product.
  • LIN liquid nitrogen
  • LOX liquid oxygen
  • Temporary storage can be used temporarily using at least two tanks be made, on the one hand with increased pressure oxygen (DGOX) demand in addition to the LOX from rectification from one tank LOX removed, compressed, evaporated in countercurrent and warmed and then as DGOX product is released and thereby recovered in countercurrent cold and is used to create and cache LIN product, where on the other hand, with low DGOX requirements, correspondingly little LOX from the Rectification system given as DGOX and more LOX temporarily stored becomes.
  • DGOX pressure oxygen
  • a two-column process can be used for rectification, one Head cooling of the pressure column with an intermediate liquid from a low pressure column accomplished and a sump heating of the low pressure column by indirect Heat exchange with air is made.
  • the two-column process is from DE 196 09 490 A1 and is particularly suitable if only a small one Oxygen purity is required.
  • a three-column process can also be used as the rectification system, being a double column with a high pressure part and a low pressure part and a Additional column is used under intermediate pressure.
  • the three-column process is from DE 195 37 913 A1 known. Even with oxygen purities> 99.5 mol% are with this Process energy savings possible.
  • the work-relieving relaxation can take place in at least one cooling turbine, the power on the shaft of such a turbine for driving either one electricity generating generator or a booster is used, the booster is used, for example, to recompress the air in the refrigeration cycle. In In both cases, the energy of the cooling turbine is used cheaply.
  • Characteristic of the device according to the invention is that the compressor station is designed with at least two compressors arranged in parallel, which are designed in this way are that only one of the compressors is in operation in gas operation, this compressor Throttle air supplies and the refrigeration circuit is not pressurized while in Operation with production of printed product and liquid product at least two in parallel arranged compressors are in operation and in addition to the supply of throttle air the cooling circuit is pressurized with air.
  • a compressor station has several advantages.
  • a compressor is energetically connected to its gas operation cheapest operating point, with additional production of liquid product several, for example two compressors close to their optimal operating point used. With several compressors, one becomes simultaneously Machine redundancy created that ensures security of supply in gas operation increased accordingly.
  • Another advantage of the invention is that with a Compressor, operated as a cycle compressor, also an energy-efficient liquid product can be generated and that this liquid operation through machine redundancy is also made possible with high security of supply.
  • the refrigeration turbine in the refrigeration circuit wiring harness can function as a turbine / generator unit be trained.
  • the energy gained in the cooling turbine is transferred to the local power grid fed.
  • the cooling turbine in the wiring harness of the cooling circuit can act as a turbine / booster unit be formed, the booster in the wiring harness of the refrigeration circuit as Post-compressor of air from the compressor station is switched.
  • the one in the cold turbine gained energy, for example via a common wave with a Booster used to drive this booster.
  • a secondary compressor for air from the Compressor station can be arranged.
  • the changing demand can be energy-efficient with a high security of supply of the steelworks on gaseous printed products.
  • the Invention and further refinements of the invention are described below of exemplary embodiments illustrated in the drawings.
  • air to be broken down is drawn in at 1 and in an air compressor 30 a first pressure, essentially medium pressure column pressure (plus line losses) compressed, pre-cooled in a cooling device 31 in direct contact with water and in a cleaning device (molecular sieve system) 32 in particular of water and Free of carbon dioxide.
  • a first pressure essentially medium pressure column pressure (plus line losses) compressed, pre-cooled in a cooling device 31 in direct contact with water and in a cleaning device (molecular sieve system) 32 in particular of water and Free of carbon dioxide.
  • the cleaned air is divided into three sub-streams, the first of which without further measures to increase pressure via line 103, through a main heat exchanger 2 and is introduced via line 104 into a medium pressure column 6.
  • the medium pressure column 6 is - according to the respective product specification and pressure losses - under operated at a pressure of 2 to 4 bar, preferably about 2.5 to 3.5 bar.
  • the second partial flow of the cleaned air is in a post-compressor 202 essential pressure column pressure (plus line losses) compressed, in Main heat exchanger 2 in indirect heat exchange with cold process streams cooled to dew point temperature and introduced into the bottom of a pressure column 7 (see positions 201,202,203,2,204 and 7).
  • the pressure column 7 is at one Working pressure of 5 to 10 bar, preferably operated 5.5 to 6.5 bar and is over a main capacitor 3 thermally coupled to a low pressure column 5.
  • Latter works at a pressure of 1.1 to 2.0 bar, preferably 1.3 to 1.7 bar.
  • Air post-compressor 202 can be driven by the same motor shaft as that Air compressor 30.
  • the third partial flow is fed via a line 301 to a compressor station 305 for Turbine air (306, 307, 308) into a turbine 309 and / or for rectification air (313, 314, 315), the intake pressure 303 using a throttle device 302 can be reduced especially in underload operation.
  • the air of the third partial flow is about in the compression station 305
  • Medium pressure column pressure compressed to a pressure equal to an air condensation temperature corresponds, which is at least approximately equal to Evaporation temperature of the liquid pressurized oxygen 17 is.
  • the third partial flow of the cleaned air also on the pressure side of the air post-compressor 202 are branched off when air (312) from the expansion turbine 309 is fed into the pressure column 7.
  • the suction pressure of the compressor station 305 then corresponds to the pressure column pressure.
  • a first portion 307 of the highly compressed air 306 is at a temperature 308 which between the temperatures at the warm and cold ends of the Main heat exchanger 2 is fed to the expansion turbine 309 and there for example, medium pressure column pressure relaxed while working.
  • the embodiment is the turbine output by a brake generator to the The relaxed turbine outlet flow is partly through the Main heat exchanger 2 via lines 310, 311 and 304 to the suction side of the Compressor station 305 returned, partly via line 312 in the bottom of the Medium pressure column 6 fed.
  • a second part 313 of the highly compressed air 306 is against the evaporating Pressurized oxygen 17 at least partially, preferably completely or in essentially completely liquefied, to a part 314 above the sump in the Low pressure column 5 and another part 315 in the bottom of the pressure column 7 relaxed.
  • Bottom liquid 70 and washing nitrogen 74 from the top of the pressure column 7 are in a supercooling counterflow 4 against a residual gas flow 50
  • Low pressure column 5 supercooled and in each case in the low pressure column 5 and / or in the Medium pressure column relaxed (lines 71, 72, 73, 75, 76 and 77).
  • Bottom liquid 60 and washing nitrogen 61 from the medium pressure column are also in the Subcooling countercurrent 4 subcooled against the residual gas stream 50 (not in Figure 1 shown) or the bottom liquid 60 directly into the top condenser 10 of the Medium pressure column and the washing nitrogen 61 on the head of the low pressure column 5 given up.
  • a residual gas stream 51 and products from the rectification section, in Example GOX and DGOX are approximately in the main heat exchanger 2 Ambient temperature warmed up (lines 51, 52, 54, 55, 17 and 18).
  • the Residual gas stream 52 can be completely or partially as stream 53 for the regeneration of the Molecular sieve station 32 can be used.
  • Liquid oxygen 15 is taken from the bottom of the low pressure column, depending on Product specification with the help of an oxygen pump 16 to the required Delivery pressure compressed or completely or partially into a removable storage tank 80 filled.
  • Liquid nitrogen 78 is drawn off from the top of the low pressure column 5 or branched off from one of the washing nitrogen lines 75 or 61 and likewise internally compressed (not shown in FIG. 1) or in a removable storage tank 79 fed.
  • the compressor station 305 consists of at least two in parallel switched compressors. This makes it possible to also use the removable storage system to operate as a pure gas apparatus, i.e. without liquid production the to generate internally compressed oxygen (DGOX).
  • DGOX internally compressed oxygen
  • one of the two compressors of the compression station 305 is taken out of operation and the second compressor takes over the task of compressing the inside Evaporate pressurized oxygen 17.
  • the compressor station 305 thus exists according to the invention from two compressors, each with a different function, from one for the generation of cold for liquid production and the other for Evaporation of the internally compressed oxygen is used.
  • the removable storage tanks 79 and 80 are used in the example of a time-limited Overproduction of DGOX, the removal of LOX and LIN as sales products, as Emergency supply tanks, as removable storage of the LOX and LIN cold contents and as Cooling supply with the cooling circuit switched off.
  • the compressor station shown in FIG. 1 can be single-stage or multi-stage machines with intercooling and / or aftercooling included.
  • the work output of the Expansion turbine 309 in the present embodiment to a booster transfer.
  • the air throttle flow 313 is cooled in the Main heat exchanger 2 and subsequent isenthalpic relaxation in the Double column 5,7 compressed to a pressure which is at least as large as that Final pressure of the compressor station 305 of the exemplary embodiment in FIG. 1.
  • air to be broken down is drawn in at 1 and in an air compressor 30 a first pressure, essentially medium pressure column pressure (plus line losses) compressed, pre-cooled in a cooling device 31 in direct contact with water and in a cleaning device (molecular sieve system) 32 in particular of water and Free of carbon dioxide.
  • a first pressure essentially medium pressure column pressure (plus line losses) compressed, pre-cooled in a cooling device 31 in direct contact with water and in a cleaning device (molecular sieve system) 32 in particular of water and Free of carbon dioxide.
  • the cleaned air is divided into three sub-streams, the first of which without further measures to increase pressure via line 103, through main heat exchanger 2 and can be introduced via line 104 into a medium pressure column 6.
  • the Medium pressure column 6 is - according to the respective product specification and Pressure losses - under a pressure of 2 to 4 bar, preferably about 2.5 to 3.5 bar operated.
  • the second partial flow of the cleaned air is applied to one in a post-compressor 202 Compresses pressure that corresponds to an air condensation temperature that at least approximately the same as the evaporation temperature of a liquid low-pressure oxygen 15 is, in the main heat exchanger 2 in indirect heat exchange with cold Process streams cooled and in a bottom condenser 3 of the low pressure column 5 introduced (see positions 201, 202, 203, 2, 204 and 3).
  • Air post-compressor 202 can be driven by the same motor shaft as that Air compressor 30.
  • the two-column apparatus shown works with high oxygen purities (greater than 99.5%) in the limit case over into the normal double column apparatus (see e.g. patent DE 195 26 785 C1).
  • the second partial flow then goes to zero and that Low pressure column taps of streams 62 and 63 shift towards the swamp the low pressure column 5, so that the top capacitor 10 to the main capacitor of the Double column is and the pressure of the medium pressure column corresponding to the thermal coupling increased.
  • the third partial flow is fed via a line 301 to a compressor station 305 for Turbine air (306, 307, 308) into a turbine 309 and / or for rectification air (313, 314, 315) supplied, the suction pressure 303 thereof with the aid of a throttle device 302 can be reduced in particular in underload operation.
  • the air of the third Partial flow is in the compressor station 305 from about medium pressure column pressure compresses a pressure that corresponds to an air condensation temperature that at least approximately equal to the vaporization temperature of the liquid pressurized oxygen 17 is.
  • a first partial stream 307 of the highly compressed air 306 is fed via line 308 to a Temperature that is between the temperatures at the warm and cold ends of the Main heat exchanger 2 is fed to the expansion turbine 309 and there for example, medium pressure column pressure relaxed while working.
  • the embodiment is the turbine output by a brake generator to the The relaxed turbine outlet flow is partly through the Main heat exchanger 2 via lines 310,311 and 304 to the suction side of the Compressor station 305 returned, partly via line 312 in the bottom of the Medium pressure column 6 fed.
  • a second partial flow 313 of the highly compressed air 306 is against the evaporating pressurized oxygen 17 at least partially, preferably completely or essentially completely liquefied, to a part 314 above the sump in the low pressure column 5 and another part 315 in the swamp of the Medium pressure column 6 relaxed.
  • Liquid oxygen 15 is taken from the bottom of the low pressure column, depending on Product specification with the help of an oxygen pump 16 to the required Delivery pressure compressed or completely or partially into a removable storage tank 80 filled.
  • Liquid nitrogen 78 is drawn off from the top of the low pressure column 5 or branched off from the washing nitrogen line 61 and likewise internally compressed (in 1 not shown) or fed into the removable storage tank 79.
  • the compressor station 305 consists of at least two in parallel switched compressors. This makes it possible to also use the removable storage system to operate as a pure gas apparatus, i.e. without liquid production the to generate internally compressed oxygen (DGOX).
  • DGOX internally compressed oxygen
  • one of the two compressors of the compression station 305 is taken out of operation and the second compressor takes over the task of compressing the inside Evaporate pressurized oxygen 17.
  • the compressor station 305 thus exists according to the invention from two compressors, each with a different function, from one for the generation of cold for liquid production and the other for Evaporation of the internally compressed oxygen is used.
  • the removable storage tanks 79 and 80 are used in the example of a time-limited Overproduction of DGOX, the removal of LOX and LIN as sales products, as Emergency supply tanks, as removable storage of the LOX and LIN cold contents and as Cooling supply with the cooling circuit switched off.
  • the compressor station shown in FIG. 3 can be single-stage or multi-stage machines with intercooling and / or aftercooling included.
  • the work performance of the Expansion turbine 309 in the present embodiment to a booster transfer.
  • the air throttle flow 313 is cooled in the Main heat exchanger 2 and subsequent isenthalpic expansion into the columns 5 and 6 compressed to a pressure at least as large as the ultimate pressure of the Compressor station 305 of the exemplary embodiment in FIG. 3.
  • the table shows the product flows, the alternating storage flows, for the (circuit and throttle air) compressor station the number of compressors in operation, the air flows and the energy requirements of the system. All gas and liquid flows are given in m 3 / h, with m 3 / h in the normal state at 1 atm and 273 K respectively.
  • the operating cases A1, A2 and A3 are characterized in that both compressors of the compressor station are in operation and deliver a turbine flow and a throttle flow.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation Of Gases By Adsorption (AREA)

Abstract

Whilst the plant produces gas, the passage of air through a cooling circuit has to be stopped, causing a loss of cooling which is compensated by stored liquid in order to maintain operating efficiency. Hence liquid oxygen (nitrogen or air) is stored in buffer tanks (79,80), compressed and used, in addition to the liquid from the rectification, during periods of high demand. In periods of low demand excess liquid is sent to the buffer tanks. In a combined process the additional cooling is supplied conventionally by air expanded in a turbine (309) driving a load such as a generator.Rectification is carried out in a double, or triple, column system. Air initially supplied by a compressor (30) is compressed further at a station (305) consisting of two compressors in parallel to increase the flexibility of the system.

Description

Die Erfindung betrifft ein Verfahren zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft, das zeitweise in einem Gasbetrieb und zeitweise in einem kombinierten Betrieb betrieben wird,
wobei im Gasbetrieb und im kombinierten Betrieb

  • gereinigte Einsatzluft unter Überdruck abgekühlt, teilweise veflüssigt und zur Gewinnung gasförmiger und flüssiger Fraktionen einer Rektifikation unterzogen wird,
  • tiefkalte Flüssigkeit mindestens einer der flüssigen Fraktionen aus der Rektifikation unter erhöhtem Druck durch indirekten Wärmeaustausch mit Einsatzluft verdampft, angewärmt und als gasförmiges Druckprodukt gewonnen wird,
    wobei im kombinierten Betrieb
  • die hierzu benötigte Kälte in einem Luft-Kältekreislauf erzeugt wird, indem Luft in dem Kältekreislauf verdichtet und arbeitsleistend entspannt wird, der Luft hierbei Wärme entzogen wird und die arbeitsleistend entspannte Luft mindestens zum Teil im Gegenstrom mit der abzukühlenden Einsatzluft wieder angewärmt und dann rückverdichtet wird,
  • tiefkalte Flüssigkeit erzeugt und mindestens zum Teil gespeichert wird
The invention relates to a method for producing gaseous pressure product by low-temperature separation of air, which is operated at times in a gas operation and at times in a combined operation.
being in gas operation and in combined operation
  • cleaned feed air is cooled under excess pressure, partially liquefied and subjected to rectification to obtain gaseous and liquid fractions,
  • cryogenic liquid at least one of the liquid fractions from the rectification is vaporized under elevated pressure by indirect heat exchange with feed air, heated and obtained as a gaseous pressure product,
    being in combined operation
  • the cold required for this is generated in an air-cooling circuit by compressing air in the cooling circuit and relieving it to perform work, extracting heat from the air and at least partially reheating the relaxed work air in countercurrent with the feed air to be cooled and then recompressing it,
  • cryogenic liquid is generated and at least partially stored

Die Erfindung betrifft außerdem eine Vorrichtung zur Durchführung des Verfahrens mit

  • einem Hauptverdichter für Einsatzluft, wobei der Austrittsdruck des Hauptluftverdichters auch Arbeitsdruck einer folgenden Reinigungseinheit ist,
  • einer Reinluftleitung aus der Reinigungseinheit zu einer Verdichterstation für die Luft im Kältekreislauf und für die Luftzufuhr zur Rektifikation
  • und einer druckseitigen Leitung aus der Verdichterstation, die einerseits in einen Leitungsstrang des Kältekreislaufs mit mindestens einer Kälteturbine mündet und andererseits in eine Abzweigung für Drosselluft zu den Säulen.
The invention also relates to a device for carrying out the method
  • a main compressor for feed air, the outlet pressure of the main air compressor also being the working pressure of a subsequent cleaning unit,
  • a clean air line from the cleaning unit to a compressor station for the air in the refrigeration circuit and for the air supply for rectification
  • and a pressure-side line from the compressor station, which leads on the one hand into a line branch of the refrigeration circuit with at least one cooling turbine and on the other hand into a branch for throttle air to the columns.

Aus der Schrift EP 0 044 679 A1 ist ein Verfahren zur Erzeugung von gasförmigem Drucksauerstoff (DGOX) und geringer Mengen Flüssigsauerstoff (LOX) bekannt: Kälte für die Luftzerlegung und die Erzeugung von Flüssigprodukt liefert ein Luftkältekreislauf. Er enthält eine Verdichtung mit zwei Kompressorstufen in Serie zur Verdichtung eines Luftstromes in der ersten Stufe auf einen mittleren Druck für eine arbeitsleistende Entspannung eines Teilstromes dieser Luft auf einen unteren Druck und eine zweite Kompressorstufe zur Verdichtung des restlichen Luftstromes auf einen höheren Druck für eine Drosselentspannung auf den gleichen niedrigen Druck. Nach Zusammenführung der Teilströme und Abzweigen einer gebildeten Flüssigphase wird die Gasphase zur Verdichtung rezykliert und die Flüssigphase nach Aufteilung in zwei Drosselströme einer Rektifikation zugeführt. Der Kältekreislauf kann bei einem solchen Verfahren nicht abgeschaltet werden und ein Zurückfahren der Kälteleistung führt zu einem energetisch ungünstigen Betrieb.From the document EP 0 044 679 A1 is a process for the production of gaseous Compressed oxygen (DGOX) and small amounts of liquid oxygen (LOX) known: cold supplies for air separation and the production of liquid product Air cooling circuit. It contains a compression with two compressor stages in series Compression of an air flow in the first stage to a medium pressure for one work-relieving relaxation of a partial flow of this air to a lower pressure and a second compressor stage to compress the remaining air flow to one higher pressure for throttle relaxation to the same low pressure. After Merging the partial streams and branching off a liquid phase formed the gas phase recycles for compression and the liquid phase after splitting into two Choke currents fed to a rectification. The refrigeration cycle in such a The process cannot be switched off and the cooling capacity is reduced an energetically unfavorable operation.

Aufgabe der Erfindung ist ein Verfahren und eine Vorrichtung der eingangs genannten Art mit einer energetisch günstigen Erzeugung des gasförmigen Druckprodukts und des Flüssigprodukts jeweils in variablen Mengen und bei hoher Verfügbarkeit der Erzeugung des Druckprodukts.The object of the invention is a method and a device of the aforementioned Kind with an energetically favorable production of the gaseous printed product and of the liquid product in variable quantities and with high availability of the Generation of the printed product.

Diese Aufgabe wird erfindungsgemäß gelöst von einem Verfahren mit den Merkmalen des Anspruchs 1 und von einer Vorrichtung mit den Merkmalen des Anspruchs 8. Ausführungen der Erfindung sind Gegenstand von Unteransprüchen.According to the invention, this object is achieved by a method having the features of claim 1 and of a device with the features of claim 8. Embodiments of the invention are the subject of dependent claims.

Kennzeichnend an dem erfindungsgemäßen Verfahren ist, daß beim Gasbetrieb der Luftdurchsatz im Kältekreislauf auf Null reduziert wird und zu einer Kompensation von Kälteverlusten, die nicht mehr durch den Kältekreislauf gedeckt werden, tiefkalte gespeicherte Flüssigkeit verwendet wird. Dies ermöglicht die Erzeugung von gasförmigem Druckprodukt auch bei vollem Flüssigprodukttank, indem beispielsweise gespeichertes Flüssigprodukt in einem Wärmeaustauscher im Gegenstrom zur eingesetzten Luft geführt wird, diese Luft dabei abgekühlt, teilweise verflüssigt und der Rektifikation zugeführt wird oder indem gespeicherte Flüssigkeit direkt der Rektifikation zugeführt wird.It is characteristic of the method according to the invention that the gas operation of the Air flow in the refrigeration circuit is reduced to zero and a compensation of Cold losses that are no longer covered by the refrigeration cycle are extremely cold stored liquid is used. This enables the generation of gaseous printed product even with a full liquid product tank, for example stored liquid product in a heat exchanger in counterflow to used air is guided, this air is cooled, partially liquefied and the Rectification is supplied or by stored liquid directly to the rectification is fed.

Tiefkalte Flüssigkeit mindestens einer flüssigen Fraktion aus der Rektifikation, beispielsweise Flüssigstickstoff (LIN), Flüssigsauerstoff (LOX) oder flüssige Luft, zur Kompensation von Kälteverlusten im Gasbetrieb kann in einem Tank zwischengespeichert werden, wobei als Tank zum Speichern dieser Fraktionen Pufferbehälter und/oder Produkttanks verwendet werden. Meist ist die Nutzung von Produkttanks die günstigste Lösung, während flüssige Luft eher einen Pufferbehälter erfordert, da flüssige Luft als Produkt meist keine Rolle spielt.Cryogenic liquid of at least one liquid fraction from the rectification, for example liquid nitrogen (LIN), liquid oxygen (LOX) or liquid air Compensation for cold losses in gas operation can be in a tank be cached, being used as a tank to store these fractions Buffer tanks and / or product tanks can be used. Most is the use of Product tanks are the cheapest solution, while liquid air is more like a buffer tank Required, since liquid air usually doesn't matter as a product.

Zeitweise kann unter Verwendung mindestens zweier Tanks eine Wechselspeicherung vorgenommen werden, wobei einerseits bei erhöhtem Drucksauerstoff (DGOX)-Bedarf zusätzlich zum LOX aus der Rektifikation aus dem einen Tank zwischengespeichertes LOX entnommen, verdichtet, im Gegenstrom verdampft und angewärmt und dann als DGOX-Produkt abgeben wird und hierbei im Gegenstrom Kälte zurückgewonnen und zur Erzeugung und Zwischenspeicherung von LIN-Produkt verwendet wird, wobei andererseits bei niedrigem DGOX-Bedarf entsprechend wenig LOX aus dem Rektifiziersystem als DGOX abgegeben und dafür mehr LOX zwischengespeichert wird. Der Vorteil besteht darin, daß zeitweise mehr DGOX geliefert wird als nach Auslegung der Luftzerlegung möglich wäre, indem gespeichertes LOX entnommen und dem Kälteinhalt des LOX entsprechend LIN gespeichert wird.Temporary storage can be used temporarily using at least two tanks be made, on the one hand with increased pressure oxygen (DGOX) demand in addition to the LOX from rectification from one tank LOX removed, compressed, evaporated in countercurrent and warmed and then as DGOX product is released and thereby recovered in countercurrent cold and is used to create and cache LIN product, where on the other hand, with low DGOX requirements, correspondingly little LOX from the Rectification system given as DGOX and more LOX temporarily stored becomes. The advantage is that sometimes more DGOX is delivered than to Interpretation of air separation would be possible by removing stored LOX and the cold content of the LOX is saved according to LIN.

Zur Rektifikation kann ein Zweisäulenverfahren eingesetzt werden, wobei eine Kopfkühlung der Drucksäule mit einer Zwischenflüssigkeit aus einer Niederdrucksäule bewerkstelligt und eine Sumpfheizung der Niederdrucksäule durch indirekten Wärmeaustausch mit Luft vorgenommen wird. Das Zweisäulenverfahren ist aus DE 196 09 490 A1 bekannt und eignet sich besonders, wenn nur eine geringe Sauerstoffreinheit erforderlich ist.A two-column process can be used for rectification, one Head cooling of the pressure column with an intermediate liquid from a low pressure column accomplished and a sump heating of the low pressure column by indirect Heat exchange with air is made. The two-column process is from DE 196 09 490 A1 and is particularly suitable if only a small one Oxygen purity is required.

Als Rektifiziersystem kann alternativ auch ein Dreisäulenverfahren eingesetzt werden, wobei eine Doppelsäule mit einem Hochdruckteil und einem Niederdruckteil und eine Zusatzsäule unter Zwischendruck eingesetzt wird. Das Dreisäulenverfahren ist aus DE 195 37 913 A1 bekannt. Auch bei Sauerstoffreinheiten > 99,5 mol % sind mit diesem Verfahren Energieeinsparungen möglich. Alternatively, a three-column process can also be used as the rectification system, being a double column with a high pressure part and a low pressure part and a Additional column is used under intermediate pressure. The three-column process is from DE 195 37 913 A1 known. Even with oxygen purities> 99.5 mol% are with this Process energy savings possible.

Bei der Gewinnung von gasförmigem Druckprodukt durch Verdampfen und Anwärmen von Flüssigkeit unter Druck, auch Innenverdichtung genannt, im Gegenstrom mit warmer Luft, kann Luft auf dem oberen Druckniveau der Verdichtung im Kältekreislauf verwendet werden oder solche, die von diesem Druckniveau ausgehend nachverdichtet wird.In the production of gaseous printed products by evaporation and heating of liquid under pressure, also called internal compression, in counterflow warm air, air can reach the upper pressure level of compression in the refrigeration cycle used or those based on this pressure level is densified.

Die arbeitsleistende Entspannung kann in mindestens einer Kälteturbine erfolgen, wobei die Leistung an der Welle einer solchen Turbine zum Antrieb entweder eines stromerzeugenden Generators oder eines Boosters verwendet wird, wobei der Booster beispielsweise zum Nachverdichten der Luft im Kältekreislauf eingesetzt wird. In beiden Fällen wird die Energie der Kälteturbine günstig genutzt.The work-relieving relaxation can take place in at least one cooling turbine, the power on the shaft of such a turbine for driving either one electricity generating generator or a booster is used, the booster is used, for example, to recompress the air in the refrigeration cycle. In In both cases, the energy of the cooling turbine is used cheaply.

Kennzeichnend an der erfindungsgemäßen Vorrichtung ist, daß die Verdichterstation mit mindestens zwei parallel angeordneten Verdichtem ausgeführt ist, die so ausgelegt sind, daß im Gasbetrieb nur einer der Verdichter in Betrieb ist, wobei dieser Verdichter Drosselluft liefert und der Kältekreislauf nicht mit Luft beaufschlagt ist, während im Betrieb mit Erzeugung von Druckprodukt und Flüssigprodukt mindestens zwei parallel angeordnete Verdichter in Betrieb sind und zusätzlich zum Liefem von Drosselluft auch der Kältekreislauf mit Luft beaufschlagt ist. Eine solche Verdichterstation besitzt mehrere Vorteile. Für den Gasbetrieb wird ein Verdichter an seinem energetisch günstigsten Betriebspunkt, bei zusätzlicher Erzeugung von Flüssigprodukt werden mehrere, beispielsweise zwei Verdichter nahe ihrem optimalen Betriebspunkt eingesetzt. Mit mehreren Verdichtem wird außerdem gleichzeitig eine Maschinenredundanz geschaffen, die die Versorgungssicherheit im Gasbetrieb entsprechend erhöht. Ein weiterer Vorteil der Erfindung besteht darin, daß mit einem Verdichter, als Kreislaufverdichter betrieben, auch energetisch günstig Flüssigprodukt erzeugt werden kann und daß dieser Flüssigbetrieb durch die Maschinenredundanz ebenfalls mit hoher Versorgungssicherheit ermöglicht wird.Characteristic of the device according to the invention is that the compressor station is designed with at least two compressors arranged in parallel, which are designed in this way are that only one of the compressors is in operation in gas operation, this compressor Throttle air supplies and the refrigeration circuit is not pressurized while in Operation with production of printed product and liquid product at least two in parallel arranged compressors are in operation and in addition to the supply of throttle air the cooling circuit is pressurized with air. Such a compressor station has several advantages. A compressor is energetically connected to its gas operation cheapest operating point, with additional production of liquid product several, for example two compressors close to their optimal operating point used. With several compressors, one becomes simultaneously Machine redundancy created that ensures security of supply in gas operation increased accordingly. Another advantage of the invention is that with a Compressor, operated as a cycle compressor, also an energy-efficient liquid product can be generated and that this liquid operation through machine redundancy is also made possible with high security of supply.

Die Kälteturbine im Leitungsstrang des Kältekreislaufs kann als Turbinen/Generator-Einheit ausgebildet sein. Die in der Kälteturbine gewonnene Energie wird in das örtliche Stromnetz eingespeist. The refrigeration turbine in the refrigeration circuit wiring harness can function as a turbine / generator unit be trained. The energy gained in the cooling turbine is transferred to the local power grid fed.

Die Kälteturbine im Leitungstrang des Kältekreislaufs kann als Turbinen/Booster-Einheit ausgebildet sein, wobei der Booster im Leitungsstrang des Kältekreislaufs als Nachverdichter von Luft aus der Verdichterstation geschaltet ist. Die in der Kälteturbine gewonnene Energie wird, beispielsweise über eine gemeinsame Welle mit einem Booster zum Antrieb dieses Boosters verwendet.The cooling turbine in the wiring harness of the cooling circuit can act as a turbine / booster unit be formed, the booster in the wiring harness of the refrigeration circuit as Post-compressor of air from the compressor station is switched. The one in the cold turbine gained energy, for example via a common wave with a Booster used to drive this booster.

Im Leitungsstrang für die Drosselluft kann ein Nachverdichter für Luft aus der Verdichterstation angeordnet sein.A secondary compressor for air from the Compressor station can be arranged.

Eine vorteilhafte Anwendung erfährt das Verfahren und die Vorrichtung gemäß Erfindung in einer Luftzerlegungsanlage zur Belieferung eines Stahlwerks mit Stickstoff und Sauerstoff.The method and the device according to FIG Invention in an air separation plant for supplying a steel plant with nitrogen and oxygen.

Energetisch günstig kann mit hoher Versorgungssicherheit dem wechselnden Bedarf des Stahlwerks an gasförmigem Druckprodukt Rechnung getragen werden. Die Erfindung sowie weitere Ausgestaltungen der Erfindung werden im folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert.The changing demand can be energy-efficient with a high security of supply of the steelworks on gaseous printed products. The Invention and further refinements of the invention are described below of exemplary embodiments illustrated in the drawings.

Hierbei zeigen:

  • Figur 1 ein Ausführungsbeispiel der Erfindung mit Dreisäulen-Rektifikation und Turbinen/Generator-Einheit,
  • Figur 2 eine Ausführung mit Dreisäulen-Rektifikation, Turbinen/Booster-Einheit und Drosselluft-Nachverdichtung,
  • Figur 3 ein Ausführungsbeispiel der Erfindung mit Zweisäulen-Rektifikation und Turbinen/Generator-Einheit und
  • Figur 4 eine Ausführung mit Zweisäulen-Rektifikation, Turbinen/Booster-Einheit und Drosselluft-Nachverdichtung.
    • Here show:
  • 1 shows an embodiment of the invention with three-column rectification and turbine / generator unit,
  • FIG. 2 shows an embodiment with three-column rectification, turbine / booster unit and throttle air post-compression,
  • Figure 3 shows an embodiment of the invention with two-column rectification and turbine / generator unit and
  • Figure 4 shows an embodiment with two-column rectification, turbine / booster unit and throttle air post-compression.

    • Figur 1Figure 1

    In Figur 1 wird zu zerlegende Luft bei 1 angesaugt und in einem Luftverdichter 30 auf einen ersten Druck im wesentlichen Mitteldrucksäulendruck (plus Leitungsverluste) verdichtet, in einer Kühleinrichtung 31 in direktem Kontakt mit Wasser vorgekühlt und in einer Reinigungseinrichtung (Molsiebanlage) 32 insbesondere von Wasser und Kohlendioxid befreit.In FIG. 1, air to be broken down is drawn in at 1 and in an air compressor 30 a first pressure, essentially medium pressure column pressure (plus line losses) compressed, pre-cooled in a cooling device 31 in direct contact with water and in a cleaning device (molecular sieve system) 32 in particular of water and Free of carbon dioxide.

    Die gereinigte Luft wird in drei Teilströme aufgeteilt, von denen der erste ohne weitere druckerhöhende Maßnahmen über Leitung 103, durch einen Hauptwärmetauscher 2 und über Leitung 104 in eine Mitteldrucksäule 6 eingeführt wird. Die Mitteldrucksäule 6 wird - entsprechend der jeweiligen Produktspezifikation und den Druckverlusten - unter einem Druck von 2 bis 4 bar, vorzugsweise etwa 2,5 bis 3,5 bar betrieben.The cleaned air is divided into three sub-streams, the first of which without further measures to increase pressure via line 103, through a main heat exchanger 2 and is introduced via line 104 into a medium pressure column 6. The medium pressure column 6 is - according to the respective product specification and pressure losses - under operated at a pressure of 2 to 4 bar, preferably about 2.5 to 3.5 bar.

    Der zweite Teilstrom der gereinigten Luft wird in einem Nachverdichter 202 auf im wesentlichen Drucksäulendruck (plus Leitungsverluste) verdichtet, im Hauptwärmetauscher 2 in indirektem Wärmeaustausch mit kalten Verfahrensströmen auf Taupunktstemperatur abgekühlt und in den Sumpf einer Drucksäule 7 eingeführt (siehe Positionen 201,202,203,2,204 und 7). Die Drucksäule 7 wird bei einem Arbeitsdruck von 5 bis 10 bar, vorzugsweise 5,5 bis 6,5 bar betrieben und ist über einen Hauptkondensator 3 mit einer Niederdrucksäule 5 thermisch gekoppelt. Letztere arbeitet bei einem Druck von 1,1 bis 2,0 bar vorzugsweise 1,3 bis 1,7 bar. Der Luftnachverdichter 202 kann von derselben Motorwelle angetrieben werden wie der Luftverdichter 30.The second partial flow of the cleaned air is in a post-compressor 202 essential pressure column pressure (plus line losses) compressed, in Main heat exchanger 2 in indirect heat exchange with cold process streams cooled to dew point temperature and introduced into the bottom of a pressure column 7 (see positions 201,202,203,2,204 and 7). The pressure column 7 is at one Working pressure of 5 to 10 bar, preferably operated 5.5 to 6.5 bar and is over a main capacitor 3 thermally coupled to a low pressure column 5. Latter works at a pressure of 1.1 to 2.0 bar, preferably 1.3 to 1.7 bar. Of the Air post-compressor 202 can be driven by the same motor shaft as that Air compressor 30.

    Der dritte Teilstrom wird über eine Leitung 301 einer Verdichterstation 305 für Turbinenluft (306, 307, 308) in eine Turbine 309 und/oder für Rektifikationsluft (313, 314, 315) zugeführt, wobei der Ansaugdruck 303 mit Hilfe einer Drosselvorrichtung 302 vermindert werden kann insbesondere bei Unterlastbetrieb.The third partial flow is fed via a line 301 to a compressor station 305 for Turbine air (306, 307, 308) into a turbine 309 and / or for rectification air (313, 314, 315), the intake pressure 303 using a throttle device 302 can be reduced especially in underload operation.

    Die Luft des dritten Teilstroms wird in der Verdichterstation 305 von etwa Mitteldrucksäulendruck auf einen Druck komprimiert, der einer Luft-Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatur des flüssigen Drucksauerstoffs 17 ist. Alternativ kann der dritte Teilstrom der gereinigten Luft auch an der Druckseite des Luftnachverdichters 202 abgezweigt werden, wenn gleichzeitig Luft (312) aus der Entspannungsturbine 309 in die Drucksäule 7 eingespeist wird. Der Ansaugdruck der Verdichterstation 305 entspricht dann dem Drucksäulendruck. The air of the third partial flow is about in the compression station 305 Medium pressure column pressure compressed to a pressure equal to an air condensation temperature corresponds, which is at least approximately equal to Evaporation temperature of the liquid pressurized oxygen 17 is. Alternatively, the third partial flow of the cleaned air also on the pressure side of the air post-compressor 202 are branched off when air (312) from the expansion turbine 309 is fed into the pressure column 7. The suction pressure of the compressor station 305 then corresponds to the pressure column pressure.

    Ein erster Teil 307 der hochverdichteten Luft 306 wird bei einer Temperatur 308, die zwischen den Temperaturen am warmen und am kalten Ende des Hauptwärmetauschers 2 liegt, der Entspannungsturbine 309 zugeleitet und dort auf etwa Mitteldrucksäulendruck arbeitsleistend entspannt. Im vorliegenden Ausführungsbeispiel wird die Turbinenleistung durch einen Bremsgenerator an das Werksnetz übertragen.Der entspannte Turbinenaustrittsstrom wird teils durch den Hauptwärmetauscher 2 über die Leitungen 310, 311 und 304 auf die Saugseite der Verdichterstation 305 zurückgeführt, teils über Leitung 312 in den Sumpf der Mitteldrucksäule 6 eingespeist.A first portion 307 of the highly compressed air 306 is at a temperature 308 which between the temperatures at the warm and cold ends of the Main heat exchanger 2 is fed to the expansion turbine 309 and there for example, medium pressure column pressure relaxed while working. In the present The embodiment is the turbine output by a brake generator to the The relaxed turbine outlet flow is partly through the Main heat exchanger 2 via lines 310, 311 and 304 to the suction side of the Compressor station 305 returned, partly via line 312 in the bottom of the Medium pressure column 6 fed.

    Ein zweiter Teil 313 der hochverdichteten Luft 306 wird gegen den verdampfenden Drucksauerstoff 17 mindestens teilweise, vorzugsweise vollständig oder im wesentlichen vollständig verflüssigt, zu einem Teil 314 oberhalb vom Sumpf in die Niederdrucksäule 5 und zu einem anderen Teil 315 in den Sumpf der Drucksäule 7 entspannt.A second part 313 of the highly compressed air 306 is against the evaporating Pressurized oxygen 17 at least partially, preferably completely or in essentially completely liquefied, to a part 314 above the sump in the Low pressure column 5 and another part 315 in the bottom of the pressure column 7 relaxed.

    Sumpfflüssigkeit 70 und Waschstickstoff 74 vom Kopf der Drucksäule 7 werden in einem Unterkühlungsgegenströmer 4 gegen einen Restgasstrom 50 der Niederdrucksäule 5 unterkühlt und jeweils in die Niederdrucksäule 5 und / oder in die Mitteldrucksäule entspannt (Leitungen 71,72,73,75,76 und 77). Sumpfflüssigkeit 60 und Waschstickstoff 61 aus der Mitteldrucksäule werden ebenfalls im Unterkühlungsgegenströmer 4 gegen den Restgasstrom 50 unterkühlt (in Figur 1 nicht dargestellt) oder die Sumpfflüssigkeit 60 direkt in den Kopfkondensator 10 der Mitteldrucksäule und der Waschstickstoff 61 auf den Kopf der Niederdrucksäule 5 aufgegeben. Ein Restgasstrom 51 und Produkte aus dem Rektifikationsabschnitt, im Beispiel GOX und DGOX werden im Hauptwärmetauscher 2 etwa auf Umgebungstemperatur angewärmt (Leitungen 51, 52, 54, 55, 17 und 18). Der Restgasstrom 52 kann vollständig oder teilweise als Strom 53 zur Regenerierung der Molekularsiebstation 32 eingesetzt werden.Bottom liquid 70 and washing nitrogen 74 from the top of the pressure column 7 are in a supercooling counterflow 4 against a residual gas flow 50 Low pressure column 5 supercooled and in each case in the low pressure column 5 and / or in the Medium pressure column relaxed (lines 71, 72, 73, 75, 76 and 77). Bottom liquid 60 and washing nitrogen 61 from the medium pressure column are also in the Subcooling countercurrent 4 subcooled against the residual gas stream 50 (not in Figure 1 shown) or the bottom liquid 60 directly into the top condenser 10 of the Medium pressure column and the washing nitrogen 61 on the head of the low pressure column 5 given up. A residual gas stream 51 and products from the rectification section, in Example GOX and DGOX are approximately in the main heat exchanger 2 Ambient temperature warmed up (lines 51, 52, 54, 55, 17 and 18). Of the Residual gas stream 52 can be completely or partially as stream 53 for the regeneration of the Molecular sieve station 32 can be used.

    Flüssiger Sauerstoff 15 wird dem Sumpf der Niederdrucksäule entnommen, je nach Produktspezifikation mit Hilfe einer Sauerstoffpumpe 16 auf den geforderten Abgabedruck komprimiert oder vollständig oder teilweise in einen Wechselpeichertank 80 eingefüllt. Flüssiger Stickstoff 78 wird vom Kopf der Niederdrucksäule 5 abgezogen oder von einer der Waschstickstoffleitungen 75 bzw.61 abgezweigt und ebenfalls innenverdichtet (in Figur 1 nicht dargestellt) oder in einen Wechselspeichertank 79 eingespeist.Liquid oxygen 15 is taken from the bottom of the low pressure column, depending on Product specification with the help of an oxygen pump 16 to the required Delivery pressure compressed or completely or partially into a removable storage tank 80 filled. Liquid nitrogen 78 is drawn off from the top of the low pressure column 5 or branched off from one of the washing nitrogen lines 75 or 61 and likewise internally compressed (not shown in FIG. 1) or in a removable storage tank 79 fed.

    Zur Erhöhung der Flexibilität der Fahrweise und der Verfügbarkeit der Druckprodukte, im Beispiel des DGOX besteht die Verdichterstation 305 aus mindestens zwei parallel geschalteten Verdichtern. Hierdurch wird es möglich, die Wechselspeicheranlage auch als reinen Gaseapparat zu betreiben,d.h. ohne Flüssigproduktion weiterhin den innenverdichteten Drucksauerstoff (DGOX) zu erzeugen. Im Fall von zwei Verdichtern wird einer der beiden Verdichter der Verdichterstation 305 außer Betrieb genommen und der zweite Verdichter übernimmt die Aufgabe, den innenverdichteten Drucksauerstoff 17 zu verdampfen. Somit besteht die Verdichterstation 305 erfindungsgemäß aus zwei Verdichtem mit jeweils unterschiedlicher Funktion, von denen der eine zur Erzeugung der Kälte für die Flüssigproduktion und der andere zur Verdampfung des innenverdichteten Drucksauerstoffs herangezogen wird.To increase the flexibility of the driving style and the availability of the print products, In the example of the DGOX, the compressor station 305 consists of at least two in parallel switched compressors. This makes it possible to also use the removable storage system to operate as a pure gas apparatus, i.e. without liquid production the to generate internally compressed oxygen (DGOX). In the case of two compressors one of the two compressors of the compression station 305 is taken out of operation and the second compressor takes over the task of compressing the inside Evaporate pressurized oxygen 17. The compressor station 305 thus exists according to the invention from two compressors, each with a different function, from one for the generation of cold for liquid production and the other for Evaporation of the internally compressed oxygen is used.

    Die Wechselspeichertanks 79 und 80 dienen im Beispiel einer zeitlich begrenzten Überproduktion von DGOX, der Entnahme von LOX und LIN als Verkaufsprodukte, als Notversorgungstanks,als Wechselspeicherung der LOX - und LIN -Kälteinhalte und als Kälteversorgung bei abgeschaltetem Kältekreislauf. Die in Figur 1 angegebene Verdichterstation kann ein- oder mehr- stufige Maschinen mit Zwischen- und / oder Nachkühlung enthalten.The removable storage tanks 79 and 80 are used in the example of a time-limited Overproduction of DGOX, the removal of LOX and LIN as sales products, as Emergency supply tanks, as removable storage of the LOX and LIN cold contents and as Cooling supply with the cooling circuit switched off. The compressor station shown in FIG. 1 can be single-stage or multi-stage machines with intercooling and / or aftercooling included.

    Figur 2Figure 2

    In Abweichung zum Ausführungsbeispiel in Figur 1 wird die Arbeitsleistung der Entspannungsturbine 309 in der vorliegenden Ausführung an einen Booster übertragen. Außerdem wird der Luftdrosselstrom 313 vor seiner Abkühlung im Hauptwärmetauscher 2 und anschließender isenthalper Entspannung in die Doppelsäule 5,7 auf einen Druck komprimiert, der mindestens so groß ist wie der Enddruck der Verdichterstation 305 des Ausführungsbeispiels in Figur 1.In deviation from the exemplary embodiment in FIG. 1, the work output of the Expansion turbine 309 in the present embodiment to a booster transfer. In addition, the air throttle flow 313 is cooled in the Main heat exchanger 2 and subsequent isenthalpic relaxation in the Double column 5,7 compressed to a pressure which is at least as large as that Final pressure of the compressor station 305 of the exemplary embodiment in FIG. 1.

    Figur 3Figure 3

    In Figur 3 wird zu zerlegende Luft bei 1 angesaugt und in einem Luftverdichter 30 auf einen ersten Druck im wesentlichen Mitteldrucksäulendruck (plus Leitungsverluste) verdichtet, in einer Kühleinrichtung 31 in direktem Kontakt mit Wasser vorgekühlt und in einer Reinigungseinrichtung (Molsiebanlage) 32 insbesondere von Wasser und Kohlendioxid befreit.In FIG. 3, air to be broken down is drawn in at 1 and in an air compressor 30 a first pressure, essentially medium pressure column pressure (plus line losses) compressed, pre-cooled in a cooling device 31 in direct contact with water and in a cleaning device (molecular sieve system) 32 in particular of water and Free of carbon dioxide.

    Die gereinigte Luft wird in drei Teilströme aufgeteilt, von denen der erste ohne weitere druckerhöhende Maßnahmen über Leitung 103, durch Hauptwärmetauscher 2 und über Leitung 104 in eine Mitteldrucksäule 6 eingeführt werden kann. Die Mitteldrucksäule 6 wird - entsprechend der jeweiligen Produktspezifikation und den Druckverlusten - unter einem Druck von 2 bis 4 bar, vorzugsweise etwa 2,5 bis 3,5 bar betrieben.The cleaned air is divided into three sub-streams, the first of which without further measures to increase pressure via line 103, through main heat exchanger 2 and can be introduced via line 104 into a medium pressure column 6. The Medium pressure column 6 is - according to the respective product specification and Pressure losses - under a pressure of 2 to 4 bar, preferably about 2.5 to 3.5 bar operated.

    Der zweite Teilstrom der gereinigten Luft wird in einem Nachverdichter 202 auf einen Druck verdichtet, der einer Luft-Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatur eines flüssigen Niederdrucksauerstoffs 15 ist, im Hauptwärmetauscher 2 in indirektem Wärmeaustausch mit kalten Verfahrensströmen abgekühlt und in einen Sumpfkondensator 3 der Niederdrucksäule 5 eingeführt (siehe Positionen 201, 202, 203, 2, 204 und 3).The second partial flow of the cleaned air is applied to one in a post-compressor 202 Compresses pressure that corresponds to an air condensation temperature that at least approximately the same as the evaporation temperature of a liquid low-pressure oxygen 15 is, in the main heat exchanger 2 in indirect heat exchange with cold Process streams cooled and in a bottom condenser 3 of the low pressure column 5 introduced (see positions 201, 202, 203, 2, 204 and 3).

    Letztere arbeitet bei einem Druck von 1,1 bis 2,0 bar vorzugsweise 1,3 bis 1,7 bar. Der Luftnachverdichter 202 kann von derselben Motorwelle angetrieben werden wie der Luftverdichter 30.The latter works at a pressure of 1.1 to 2.0 bar, preferably 1.3 to 1.7 bar. Of the Air post-compressor 202 can be driven by the same motor shaft as that Air compressor 30.

    Bei hohen Sauerstoffreinheiten (größer 99,5 % ) geht der gezeigte Zweisäulenapparat im Grenzfall über in den normalen Doppelsäulenapparat (siehe z.B. Patentschrift DE 195 26 785 C1). Der zweite Teilstrom geht dann gegen Null und die Niederdrucksäulenanstiche der Ströme 62 und 63 verschieben sich in Richtung Sumpf der Niederdrucksäule 5, so daß der Kopfkondensator 10 zum Hauptkondensator der Doppelsäule wird und sich der Druck der Mitteldrucksäule entsprechend der thermischen Kopplung erhöht.The two-column apparatus shown works with high oxygen purities (greater than 99.5%) in the limit case over into the normal double column apparatus (see e.g. patent DE 195 26 785 C1). The second partial flow then goes to zero and that Low pressure column taps of streams 62 and 63 shift towards the swamp the low pressure column 5, so that the top capacitor 10 to the main capacitor of the Double column is and the pressure of the medium pressure column corresponding to the thermal coupling increased.

    Der dritte Teilstrom wird über eine Leitung 301 einer Verdichterstation 305 für Turbinenluft (306, 307, 308) in eine Turbine 309 und/oder für Rektifikationsluft (313, 314, 315) zugeführt, wobei deren Ansaugdruck 303 mit Hilfe einer Drosselvorrichtung 302 vermindert werden kann insbesondere bei Unterlastbetrieb. Die Luft des dritten Teilstromes wird in der Verdichterstation 305 von etwa Mitteldrucksäulendruck auf einen Druck komprimiert, der einer Luft-Kondensationstemperatur entspricht, die mindestens etwa gleich der Verdampfungstemperatur des flüssigen Drucksauerstoffs 17 ist.The third partial flow is fed via a line 301 to a compressor station 305 for Turbine air (306, 307, 308) into a turbine 309 and / or for rectification air (313, 314, 315) supplied, the suction pressure 303 thereof with the aid of a throttle device 302 can be reduced in particular in underload operation. The air of the third Partial flow is in the compressor station 305 from about medium pressure column pressure compresses a pressure that corresponds to an air condensation temperature that at least approximately equal to the vaporization temperature of the liquid pressurized oxygen 17 is.

    Ein erster Teilstrom 307 der hochverdichteten Luft 306 wird über Leitung 308 bei einer Temperatur, die zwischen den Temperaturen am warmen und am kalten Ende des Hauptwärmetauschers 2 liegt, der Entspannungsturbine 309 zugeleitet und dort auf etwa Mitteldrucksäulendruck arbeitsleistend entspannt. Im vorliegenden Ausführungsbeispiel wird die Turbinenleistung durch einen Bremsgenerator an das Werksnetz übertragen.Der entspannte Turbinenaustrittsstrom wird teils durch den Hauptwärmetauscher 2 über die Leitungen 310,311 und 304 auf die Saugseite der Verdichterstation 305 zurückgeführt, teils über Leitung 312 in den Sumpf der Mitteldrucksäule 6 eingespeist.A first partial stream 307 of the highly compressed air 306 is fed via line 308 to a Temperature that is between the temperatures at the warm and cold ends of the Main heat exchanger 2 is fed to the expansion turbine 309 and there for example, medium pressure column pressure relaxed while working. In the present The embodiment is the turbine output by a brake generator to the The relaxed turbine outlet flow is partly through the Main heat exchanger 2 via lines 310,311 and 304 to the suction side of the Compressor station 305 returned, partly via line 312 in the bottom of the Medium pressure column 6 fed.

    Ein zweiter Teilstrom 313 der hochverdichteten Luft 306 wird gegen den verdampfenden Drucksauerstoff 17 mindestens teilweise, vorzugsweise vollständig oder im wesentlichen vollständig verflüssigt, zu einem Teil 314 oberhalb vom Sumpf in die Niederdrucksäule 5 und zu einem anderen Teil 315 in den Sumpf der Mitteldrucksäule 6 entspannt.A second partial flow 313 of the highly compressed air 306 is against the evaporating pressurized oxygen 17 at least partially, preferably completely or essentially completely liquefied, to a part 314 above the sump in the low pressure column 5 and another part 315 in the swamp of the Medium pressure column 6 relaxed.

    Sumpfflüssigkeit 60 und Waschstickstoff 61 vom Kopfkondensator 10 der Mitteldrucksäule 6 werden in einem Unterkühlungsgegenströmer 4 gegen einen Restgasstrom 50 der Niederdrucksäule 5 unterkühlt und jeweils in diese entspannt (Leitungen 71,75 und 76). Ein Restgasstrom 51 und Produkte aus dem Rektifikationsabschnitt, im Beispiel DGOX werden im Hauptwärmetauscher 2 etwa auf Umgebungstemperatur angewärmt (Leitungen 51,52,17 und 18). Der Restgasstrom 52 kann vollständig oder teilweise zur Regenerierung 53 der Molekularsiebstation 32 eingesetzt werden.Bottom liquid 60 and washing nitrogen 61 from the top condenser 10 Medium pressure column 6 are in a supercooling counterflow 4 against one Residual gas stream 50 of the low pressure column 5 is subcooled and relaxed in each of these (Lines 71, 75 and 76). A residual gas stream 51 and products from the Rectification section, in the example DGOX, are approximately in the main heat exchanger 2 Ambient temperature warmed up (lines 51, 52, 17 and 18). The residual gas stream 52 can be used in whole or in part for the regeneration 53 of the molecular sieve station 32 be used.

    Flüssiger Sauerstoff 15 wird dem Sumpf der Niederdrucksäule entnommen, je nach Produktspezifikation mit Hilfe einer Sauerstoffpumpe 16 auf den geforderten Abgabedruck komprimiert oder vollständig oder teilweise in einen Wechselpeichertank 80 eingefüllt. Flüssiger Stickstoff 78 wird vom Kopf der Niederdrucksäule 5 abgezogen oder von der Waschstickstoffleitung 61 abgezweigt und ebenfalls innenverdichtet (in Figur 1 nicht dargestellt) oder in den Wechselspeichertank 79 eingespeist. Liquid oxygen 15 is taken from the bottom of the low pressure column, depending on Product specification with the help of an oxygen pump 16 to the required Delivery pressure compressed or completely or partially into a removable storage tank 80 filled. Liquid nitrogen 78 is drawn off from the top of the low pressure column 5 or branched off from the washing nitrogen line 61 and likewise internally compressed (in 1 not shown) or fed into the removable storage tank 79.

    Zur Erhöhung der Flexibilität der Fahrweise und der Verfügbarkeit der Druckprodukte, im Beispiel des DGOX besteht die Verdichterstation 305 aus mindestens zwei parallel geschalteten Verdichtem. Hierdurch wird es möglich, die Wechselspeicheranlage auch als reinen Gaseapparat zu betreiben,d.h. ohne Flüssigproduktion weiterhin den innenverdichteten Drucksauerstoff (DGOX) zu erzeugen. Im Fall von zwei Verdichtern wird einer der beiden Verdichter der Verdichterstation 305 außer Betrieb genommen und der zweite Verdichter übernimmt die Aufgabe, den innenverdichteten Drucksauerstoff 17 zu verdampfen. Somit besteht die Verdichterstation 305 erfindungsgemäß aus zwei Verdichtem mit jeweils unterschiedlicher Funktion, von denen der eine zur Erzeugung der Kälte für die Flüssigproduktion und der andere zur Verdampfung des innenverdichteten Drucksauerstoffs herangezogen wird.To increase the flexibility of the driving style and the availability of the print products, In the example of the DGOX, the compressor station 305 consists of at least two in parallel switched compressors. This makes it possible to also use the removable storage system to operate as a pure gas apparatus, i.e. without liquid production the to generate internally compressed oxygen (DGOX). In the case of two compressors one of the two compressors of the compression station 305 is taken out of operation and the second compressor takes over the task of compressing the inside Evaporate pressurized oxygen 17. The compressor station 305 thus exists according to the invention from two compressors, each with a different function, from one for the generation of cold for liquid production and the other for Evaporation of the internally compressed oxygen is used.

    Die Wechselspeichertanks 79 und 80 dienen im Beispiel einer zeitlich begrenzten Überproduktion von DGOX, der Entnahme von LOX und LIN als Verkaufsprodukte, als Notversorgungstanks,als Wechselspeicherung der LOX - und LIN -Kälteinhalte und als Kälteversorgung bei abgeschaltetem Kältekreislauf. Die in Figur 3 angegebene Verdichterstation kann ein- oder mehr- stufige Maschinen mit Zwischen- und / oder Nachkühlung enthalten.The removable storage tanks 79 and 80 are used in the example of a time-limited Overproduction of DGOX, the removal of LOX and LIN as sales products, as Emergency supply tanks, as removable storage of the LOX and LIN cold contents and as Cooling supply with the cooling circuit switched off. The compressor station shown in FIG. 3 can be single-stage or multi-stage machines with intercooling and / or aftercooling included.

    Figur 4Figure 4

    In Abweichung zum Ausführungsbeispiel 3 wird die Arbeitsleistung der Entspannungsturbine 309 in der vorliegenden Ausführung an einen Booster übertragen. Außerdem wird der Luftdrosselstrom 313 vor seiner Abkühlung im Hauptwärmetauscher 2 und anschließender isenthalper Entspannung in die Säulen 5 und 6 auf einen Druck komprimiert, der mindestens so groß ist wie der Enddruck der Verdichterstation 305 des Ausführungsbeispiel in Figur 3.In deviation from exemplary embodiment 3, the work performance of the Expansion turbine 309 in the present embodiment to a booster transfer. In addition, the air throttle flow 313 is cooled in the Main heat exchanger 2 and subsequent isenthalpic expansion into the columns 5 and 6 compressed to a pressure at least as large as the ultimate pressure of the Compressor station 305 of the exemplary embodiment in FIG. 3.

    Beispiel:Example:

    Für die Belieferung eines Stahlwerks werden stark schwankende Mengen DGOX und Druckstickstoff (DRGAN) benötigt. Für die Belieferung des Gasmarktes sollen zusätzlich die Flüssigprodukte LOX, LIN und Flüssigargon (LAR) produziert werden, um die Wirtschaftlichkeit der Produktionsanlage zu erhöhen. Die Investitionsentscheidung wird zugunsten einer Anlage mit Turbinen/Booster-Einheit und Doppelsäulenrektifikation gefällt, weil keine Energie ins örtliche Stromnetz eingespeist werden darf und weil eine hohe Sauerstoffreinheit gefordert wird. Bis auf die nicht dargestellte Argongewinnung entspricht dies einer Anlage, wie sie in Figur 4 dargestellt ist. Die Tabelle zeigt für vier Hauptbetriebsarten A1, A2, A3 und A4 der Anlage die Produktströme, die Wechselspeicherströme, für die (Kreislauf-und Drosselluft-) Verdichterstation die Anzahl der im Betrieb befindlichen Kompressoren, die Luftströme und den Energiebedarf der Anlage. Alle Gas- und Flüssigkeitsströme sind in m3/h angegeben, wobei jeweils m3/h im Normalzustand bei 1atm und 273 K gemeint sind. Die Betriebsfälle A1, A2 und A3 zeichnen sich dadurch aus, daß beide Kompressoren der Verdichterstation in Betrieb sind und einen Turbinenstrom und einen Drosselstrom liefern.Strongly fluctuating quantities of DGOX and pressure nitrogen (DRGAN) are required to supply a steel mill. In order to supply the gas market, the liquid products LOX, LIN and liquid argon (LAR) are also to be produced in order to increase the efficiency of the production plant. The investment decision is made in favor of a plant with a turbine / booster unit and double-column rectification because no energy may be fed into the local power grid and because a high level of oxygen purity is required. Except for the argon production, which is not shown, this corresponds to a plant as shown in FIG. For four main operating modes A1, A2, A3 and A4 of the system, the table shows the product flows, the alternating storage flows, for the (circuit and throttle air) compressor station the number of compressors in operation, the air flows and the energy requirements of the system. All gas and liquid flows are given in m 3 / h, with m 3 / h in the normal state at 1 atm and 273 K respectively. The operating cases A1, A2 and A3 are characterized in that both compressors of the compressor station are in operation and deliver a turbine flow and a throttle flow.

    Im Betriebsfall A1 werden zusätzlich zur Flüssigproduktion 10.000 m3/h DGOX erzeugt. Für eine Belieferung des Stahlwerks mit 13.000 m3/h DGOX wie in Betriebsfall A2 werden zusätzlich 3000 m3/h als LOX einem LOX-Tank flüssig entnommen und innenverdichtet als DGOX abgegeben. Der Kälteinhalt des LOX wird genutzt und reicht aus, um den LIN Tank mit 2.800 m3/h zu füllen. Im Betriebsfall A3 werden nur 7.000 m3/h DGOX an das Stahlwerk abgegeben. Der beispielsweise im Betriebsfall A2 entleerte LOX-Tank wird mit 3000 m3/h LOX wieder befüllt. Die hierzu benötigte Kälte wird mit LIN aus dem vom Betriebsfall A2 her gefüllten LIN-Tank zugeführt.In operation A1, 10,000 m 3 / h DGOX are generated in addition to liquid production. To supply the steelworks with 13,000 m 3 / h DGOX, as in operating case A2, an additional 3000 m 3 / h as LOX are removed from a LOX tank in liquid form and released internally compressed as DGOX. The cold content of the LOX is used and is sufficient to fill the LIN tank with 2,800 m 3 / h. In operation A3, only 7,000 m 3 / h DGOX are released to the steelworks. The LOX tank emptied, for example, in operating mode A2, is refilled with 3000 m 3 / h LOX. The cold required for this is supplied with LIN from the LIN tank filled from operating case A2.

    Im Betriebsfall A4 ist in der Verdichterstation nur ein Kompressor in Betrieb. Er liefert den Drosselstrom, Flüssigkeit wird nicht erzeugt. Selbst für die im Stahlwerk maximal benötigte DGOX Menge von 13.000 m3/h ist die hierfür benötige Kälteleistung um eine Größenanordnung kleiner als in den Betriebsfällen A1, A2 und A3, der äquivalent benötigte Turbinenstrom müßte nur 4000 m3/h betragen. Der Kältekreislauf der Anlage wird deshalb günstig durch Flüssigkeit aus den Tanks gedeckt und der Turbinenstrom abgeschaltet. Andere Betriebsfälle sind denkbar. Die genannten Betriebsfälle zeichnen sich dadurch besonders aus, daß alle betrieblichen Anforderungen energetisch günstig erfüllt werden, weil die Maschinen in ihrem Auslegungspunkt bei etwa 100 % Leistung betrieben werden. Der Stromverbrauch der Anlage ist in der überwiegenden Zeit nahezu konstant. Deshalb kann bei den Elektroversorgungsuntenehmen ein günstiger Stromtarif erzielt werden. Betriebsfall A1 A2 A3 A4 Eintrittsluft m3/h 65.000 65.000 65.000 65.000 Produkte DGOX m3/h 10.000 13.000 7.000 13.000 LOX m3/h 3.000 3.000 3.000 - LIN m3/h 4.000 3.000 4.300 - DRGAN m3/h 2.000 2.000 2.000 2.000 LAR m3/h 430 430 430 430 Wechselpeicherströme LOX zum Tank m3/h - - 3.000 - LIN zum Tank m3/h - 2.800 - - LOX vom Tank m3/h - 3.000 - - LIN vom Tank m3/h - - 2.800 - Verdichterstation Anzahl der betriebenen Kompressoren m3/h 2 2 2 1 Turbinenstrom m3/h 51.000 43.500 57.000 4.000 Drosselstrom m3/h 21.000 23.000 17.000 23.000 Stromverbrauch kW 11.000 11.000 11.000 7.700 In operation case A4, only one compressor is in operation in the compressor station. It supplies the inductor current, liquid is not generated. Even for the maximum DGOX quantity of 13,000 m 3 / h required in the steelworks, the cooling capacity required for this is one order of size smaller than in operating cases A1, A2 and A3; the equivalent turbine flow would only have to be 4000 m 3 / h. The system's refrigeration cycle is therefore conveniently covered by liquid from the tanks and the turbine flow is switched off. Other operating cases are conceivable. The above-mentioned operating cases are characterized in particular by the fact that all operational requirements are met in terms of energy efficiency because the machines are operated at about 100% output in their design point. The electricity consumption of the system is almost constant in most of the time. Therefore, a favorable electricity tariff can be achieved with the electrical supply companies. Operating case A1 A2 A3 A4 Inlet air m 3 / h 65,000 65,000 65,000 65,000 Products DGOX m 3 / h 10,000 13,000 7,000 13,000 LOX m 3 / h 3,000 3,000 3,000 - LIN m 3 / h 4,000 3,000 4,300 - DRGAN m 3 / h 2,000 2,000 2,000 2,000 LAR m 3 / h 430 430 430 430 AC storage currents LOX to the tank m 3 / h - - 3,000 - LIN to the tank m 3 / h - 2,800 - - LOX from the tank m 3 / h - 3,000 - - LIN from the tank m 3 / h - - 2,800 - Compressor station Number of compressors operated m 3 / h 2nd 2nd 2nd 1 Turbine power m 3 / h 51,000 43,500 57,000 4,000 Inductor current m 3 / h 21,000 23,000 17,000 23,000 Power consumption kW 11,000 11,000 11,000 7,700

    Claims (12)

    Verfahren zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft, das zeitweise in einem Gasbetrieb und zeitweise in einem kombinierten Betrieb betrieben wird,
    wobei im Gasbetrieb und im kombinierten Betrieb gereinigte Einsatzluft unter Überdruck abgekühlt, teilweise verflüssigt und zur Gewinnung gasförmiger und flüssiger Fraktionen einer Rektifikation unterzogen wird, tiefkalte Flüssigkeit mindestens einer der flüssigen Fraktionen aus der Rektifikation unter erhöhtem Druck durch indirekten Wärmeaustausch mit Einsatzluft verdampft, angewärmt und als gasförmiges Druckprodukt gewonnen wird,
    wobei im kombinierten Betrieb     die hierzu benötigte Kälte in einem Luft-Kältekreislauf erzeugt wird, indem Luft in dem Kältekreislauf verdichtet und arbeitsleistend entspannt wird, der Luft hierbei Wärme entzogen wird und die arbeitsleistend entspannte Luft mindestens zum Teil im Gegenstrom mit der abzukühlenden Einsatzluft wieder angewärmt und dann rückverdichtet wird, tiefkalte Flüssigkeit erzeugt und mindestens zum Teil gespeichert wird,     dadurch gekennzeichnet, daß beim Gasbetrieb der Luftdurchsatz im Kältekreislauf auf Null reduziert wird und zu einer Kompensation von Kälteverlusten, die nicht mehr durch den Kältekreislauf gedeckt werden, tiefkalte gespeicherte Flüssigkeit verwendet wird.    Process for the production of gaseous pressure product by low-temperature separation of air, which is operated at times in a gas operation and at times in a combined operation,
    being in gas operation and in combined operation cleaned feed air is cooled under excess pressure, partially liquefied and subjected to rectification to obtain gaseous and liquid fractions, cryogenic liquid at least one of the liquid fractions from the rectification is vaporized under elevated pressure by indirect heat exchange with feed air, heated and obtained as a gaseous pressure product,
    being in combined operation     the cold required for this is generated in an air-cooling circuit by compressing air in the cooling circuit and relieving it to perform work, extracting heat from the air and at least partially reheating the relaxed work air in countercurrent with the feed air to be cooled and then recompressing it, cryogenic liquid is generated and at least partially stored,     characterized in that during gas operation the air throughput in the refrigeration cycle is reduced to zero and cryogenic stored liquid is used to compensate for cold losses which are no longer covered by the refrigeration cycle.         Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß tiefkalte Flüssigkeit mindestens einer flüssigen Fraktion aus der Rektifikation, beispielsweise Flüssigstickstoff (LIN), Flüssigsauerstoff (LOX) oder flüssige Luft, zur Kompensation von Kälteverlusten im Gasbetrieb in einem Tank zwischengespeichert wird, wobei als Tank zum Speichern dieser Fraktionen Pufferbehälter und/oder Produkttanks verwendet werden.A method according to claim 1, characterized in that cryogenic liquid at least one liquid fraction from the rectification, for example Liquid nitrogen (LIN), liquid oxygen (LOX) or liquid air, for Compensation for cold losses in gas operation in a tank is temporarily stored, being used as a tank for storing these fractions Buffer tanks and / or product tanks can be used. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß zeitweise unter Verwendung mindestens zweier Tanks eine Wechselspeicherung vorgenommen wird, wobei einerseits bei erhöhtem Drucksauerstoff (DGOX)-Bedarf zusätzlich zum LOX aus der Rektifikation aus dem einen Tank zwischengespeichertes LOX entnommen, verdichtet, im Gegenstrom verdampft und angewärmt und dann als DGOX-Produkt abgeben wird und hierbei im Gegenstrom Kälte zurückgewonnen und zur Erzeugung und Zwischenspeicherung von LIN-Produkt verwendet wird, wobei andererseits bei niedrigen DGOX Bedarf entsprechend wenig LOX aus dem Rektifiziersystem als DGOX abgeben und dafür mehr LOX zwischengespeichert wird.A method according to claim 1, characterized in that temporarily under Removable storage is made using at least two tanks on the one hand, with additional pressure oxygen (DGOX) requirements LOX cached from the rectification from the one tank removed, compressed, evaporated in countercurrent and warmed and then as DGOX product is released and thereby recovered cold in countercurrent and is used to generate and cache LIN product, on the other hand, with a low DGOX requirement, correspondingly little LOX from the Submit rectification system as DGOX and temporarily store more LOX becomes. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß ein Zweisäulenverfahren eingesetzt wird, wobei eine Kopfkühlung der Drucksäule mit einer Zwischenflüssigkeit aus einer Niederdrucksäule bewerkstelligt und eine Sumpfheizung der Niederdrucksäule durch indirekten Wärmeaustausch mit Luft vorgenommen wird.Method according to one of claims 1 to 3, characterized in that a Two-column process is used, with a head cooling of the pressure column with an intermediate liquid from a low pressure column and a Bottom heating of the low pressure column through indirect heat exchange with air is made. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß als Rektifiziersystem ein Dreisäulenverfahren eingesetzt wird, wobei eine Doppelsäule mit einem Hochdruckteil und einem Niederdruckteil und eine Zusatzsäule unter Zwischendruck eingesetzt wird.Method according to one of claims 1 to 3, characterized in that as Rectification system, a three-column process is used, with a double column with a high pressure part and a low pressure part and an additional column below Intermediate pressure is used. Verfahren nach einem der Ansprüche 1 bis 5 mit Gewinnung von gasförmigem Druckprodukt durch Verdampfen und Anwärmen von Flüssigkeit unter Druck wie in Anspruch 1, was auch Innenverdichtung genannt wird, im Gegenstrom mit warmer Luft, dadurch gekennzeichnet, daß Luft auf dem oberen Druckniveau der Verdichtung im Kältekreislauf verwendet wird oder solche, die von diesem Druckniveau ausgehend nachverdichtet wird.Method according to one of claims 1 to 5 with extraction of gaseous Printed product by evaporation and heating of liquid under pressure as in Claim 1, which is also called internal compression, in countercurrent with warm Air, characterized in that air at the upper pressure level of the Compression in the refrigeration cycle is used or those by this Pressure level is post-compressed. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß die arbeitsleistende Entspannung in mindestens einer Kälteturbine erfolgt, wobei die Leistung an der Welle einer solchen Turbine zum Antrieb entweder eines stromerzeugenden Generators oder eines Boosters verwendet wird, wobei der Booster beispielsweise zum Nachverdichten der Luft im Kältekreislauf eingesetzt wird.Method according to one of claims 1 to 6, characterized in that the work-related relaxation takes place in at least one refrigeration turbine, the Power on the shaft of such a turbine to drive either one power-generating generator or a booster is used, the Boosters are used, for example, to recompress the air in the refrigeration cycle becomes. Vorrichtung zur Durchführung des Verfahrens nach einem der Ansprüche 1 bis 7 mit einem Hauptverdichter für Einsatzluft, wobei der Austrittsdruck des Hauptluftverdichters auch Arbeitsdruck einer folgenden Reinigungseinheit ist, einer Reinluftleitung aus der Reinigungseinheit zu einer Verdichterstation für die Luft im Kältekreislauf und für die Luft zur Rektifikation und einer druckseitigen Leitung aus der Verdichterstation, die einerseits in einen Leitungsstrang des Kältekreislaufs mit mindestens einer Kälteturbine mündet und andererseits in eine Abzweigung für Drosselluft zu den Säulen, dadurch gekennzeichnet, daß die Verdichterstation mit mindestens zwei parallel angeordneten Verdichtem ausgeführt ist, die so ausgelegt sind, daß im Gasbetrieb nur einer der Verdichter im Betrieb ist, wobei dieser Verdichter Drosselluft liefert und der Kältekreislauf nicht mit Luft beaufschlagt ist, während im Betrieb mit Erzeugung von Druckprodukt und Flüssigprodukt mindestens zwei parallel angeordnete Verdichter in Betrieb sind und zusätzlich zum Liefern von Drosselluft auch der Kältekreislauf mit Luft beaufschlagt ist.Device for performing the method according to one of claims 1 to 7 with a main compressor for feed air, the outlet pressure of the main air compressor also being the working pressure of a subsequent cleaning unit, a clean air line from the cleaning unit to a compressor station for the air in the refrigeration cycle and for the air for rectification and a pressure-side line from the compressor station, which on the one hand opens into a line branch of the refrigeration circuit with at least one cooling turbine and, on the other hand, into a branch for throttle air to the columns, characterized in that the compressor station is designed with at least two compressors arranged in parallel, which are designed so that only one of the compressors is in operation in gas operation, this compressor supplies throttle air and the refrigeration circuit is not pressurized with air, while in operation with generation of the printed product and the liquid product, at least two compressors arranged in parallel are in operation and, in addition to supplying throttle air, the cooling circuit is also acted upon by air. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß die Kälteturbine im Leitungsstrang des Kältekreislaufs als Turbinen/Generator-Einheit ausgebildet ist.Apparatus according to claim 8, characterized in that the cooling turbine in Cable harness of the refrigeration circuit is designed as a turbine / generator unit. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß die Kälteturbine im Leitungsgang des Kältekreislaufs als Turbinen/Booster-Einheit ausgebildet ist, wobei der Booster im Leitungsstrang des Kältekreislaufs als Nachverdichter von Luft aus der Verdichterstation geschaltet ist. Apparatus according to claim 8, characterized in that the cooling turbine in Line passage of the refrigeration circuit is designed as a turbine / booster unit, the booster in the refrigeration circuit wiring harness as a secondary compressor of Air is switched from the compressor station. Vorrichtung nach Anspruch 8 oder 9, dadurch gekennzeichnet, daß im Leitungsstrang für die Drosselluft ein Nachverdichter für Luft aus der Verdichterstation angeordnet ist.Apparatus according to claim 8 or 9, characterized in that in Cable harness for the throttle air is a post-compressor for air from the Compressor station is arranged. Anwendung des Verfahrens nach einem der Ansprüche 1 bis 7 und der Vorrichtung nach einem der Ansprüche 8 bis 11 in einer Luftzeriegungsanlage zur Belieferung eines Stahlwerks mit Stickstoff und Sauerstoff.Application of the method according to one of claims 1 to 7 and the Device according to one of claims 8 to 11 in an air separation plant for Supplying a steel mill with nitrogen and oxygen.
    EP19990106715 1998-04-08 1999-04-01 Cryogenic air separation plant with two different operation modes Expired - Lifetime EP0949471B1 (en)

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    EP1120616A3 (en) * 2000-01-28 2002-08-28 The BOC Group plc Air separation method
    EP1120616A2 (en) * 2000-01-28 2001-08-01 The BOC Group plc Air separation method
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    EP1207362A1 (en) * 2000-10-23 2002-05-22 Air Products And Chemicals, Inc. Process and apparatus for the production of low pressure gaseous oxygen
    EP1227288A1 (en) * 2001-01-30 2002-07-31 Linde Aktiengesellschaft System with three columns for cryogenic separation of air
    US6598424B2 (en) 2001-03-09 2003-07-29 Linde Aktiengesellschaft Process and apparatus for separating a gas mixture with emergency operation
    EP1239246A1 (en) * 2001-03-09 2002-09-11 Linde Aktiengesellschaft Process and apparatus for separation of a gas mixture with failsafe operation
    WO2007129152A1 (en) * 2006-04-26 2007-11-15 L'air Liquide-Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process
    DE102009023900A1 (en) 2009-06-04 2010-12-09 Linde Aktiengesellschaft Method for cryogenic separation of air with distillation column system for nitrogen-oxygen separation, involves producing oxygen-enriched fraction and nitrogen fraction in high pressure column, and supplying nitrogen to low pressure column
    WO2014154361A2 (en) * 2013-03-28 2014-10-02 Linde Aktiengesellschaft Method and device for producing gaseous compressed oxygen having variable power consumption
    WO2014154361A3 (en) * 2013-03-28 2014-12-11 Linde Aktiengesellschaft Method and device for producing gaseous compressed oxygen having variable power consumption
    EP2824407A1 (en) * 2013-07-11 2015-01-14 Linde Aktiengesellschaft Method for generating at least one air product, air separation plant, method and device for generating electrical energy
    CN110608583A (en) * 2019-09-12 2019-12-24 北京首钢股份有限公司 Pressure control method and device
    CN110608583B (en) * 2019-09-12 2021-07-23 北京首钢股份有限公司 Pressure control method and device

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    CZ297724B6 (en) 2007-03-14
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    CZ9901213A3 (en) 2001-02-14
    HU9900988D0 (en) 1999-06-28

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