EP1020695B1 - Leistungsersparnisse für die Gastrennung bei Teillastbetrieb - Google Patents

Leistungsersparnisse für die Gastrennung bei Teillastbetrieb Download PDF

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Publication number
EP1020695B1
EP1020695B1 EP99300202A EP99300202A EP1020695B1 EP 1020695 B1 EP1020695 B1 EP 1020695B1 EP 99300202 A EP99300202 A EP 99300202A EP 99300202 A EP99300202 A EP 99300202A EP 1020695 B1 EP1020695 B1 EP 1020695B1
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Prior art keywords
column
flow rate
pressure
feed
compressor
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EP99300202A
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English (en)
French (fr)
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EP1020695A1 (de
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Laura Ann Boulton
Gregory Scott Weyrich
Joseph Michael Petrowski
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Priority to EP99300202A priority Critical patent/EP1020695B1/de
Priority to DE69911905T priority patent/DE69911905T2/de
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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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • 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
    • 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
    • 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
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods

Definitions

  • the invention relates to operation of cryogenic separation at a flow rate below the optimum ("design") flow rate of the separation (i.e. at "turndown").
  • a flow rate below the optimum (“design") flow rate of the separation i.e. at "turndown”
  • Such a process is known from GB-A-2126700. It has particular, but not exclusive, application to the separation of air to provide a nitrogen product.
  • Gaseous mixtures comprising a "light” component and a "heavy” component having a higher boiling point than the light component can be separated by cryogenic separation to provide a gaseous light component product.
  • the gaseous mixture is compressed and fed to a distillation column system in which the gaseous mixture is rectified to provide the light component product.
  • the distillation column system comprises one or more distillation columns as is well known in the art. When there are two or more columns arranged in series, they operate at different pressures with the upstream column(s) operating at a higher pressure than the downstream column(s).
  • a cryogenic separation process providing a light component product is designed to operate at optimum efficiency when providing the light component product at a predetermined design flow rate.
  • the demand for the product varies and the design flow rate is not always required. Accordingly, there are occasions upon which the separation process is operated at below design capacity (so-called "turndown").
  • turndown has typically been limited by the centrifugal compressor conventionally used to compress the gaseous mixture feed to the distillation column system.
  • the extent to which the flow rate through the compressor can be reduced is limited by surge which damages the compressor and causes fluctuations in the discharge pressure.
  • US-A-5,501,078 discloses an integrated gas turbine and air separation unit ("ASU") in which the feed air to the ASU is compressed by the gas turbine and the ASU operates to produce oxygen at a first purity and pressure when the gas turbine operates at design flow but to produce oxygen at lower purity and pressure when the gas turbine operates at a turndown pressure.
  • the oxygen product from the ASU is compressed and fed to a fuel gasifier feeding the gas turbine.
  • Control means responsive to a turndown state of the gas turbine causes the ASU to operate in its reduced purity/reduced pressure mode.
  • the reduction in purity of the oxygen product limits the reduction in oxygen product pressure resultant from reduced feed air pressure on turbine turndown compared with maintaining oxygen product purity and hence a lower compression ratio is required across the oxygen product compressor.
  • the ASU is a conventional dual column system in which nitrogen product from the lower pressure column is compressed and fed to the combustion chamber of the gas turbine.
  • the ASU is fed with gas turbine compressed feed air at 160 psi (1.1 MPa) and supplies oxygen (95% purity) and nitrogen from the lower pressure column at 48.1 psia (332 kPa) and 47.1 psia (325 kPa) respectively.
  • the feed air pressure is reduced to 130 psia (0.9 MPa).
  • the oxygen and nitrogen supply pressures from the lower pressure column are reduced by about 22% to 37.4 psia (258 kPa) and 36.7 psia (253 kPa) respectively.
  • these design supply pressures are reduced by about 16% to 40.4 psia (279 kPa) and 39.7 psia (274 kPa) respectively.
  • GB-A-2126700 (corresponding to US-A-4,566,887) discloses process and apparatus for the cryogenic fractionation of air to produce variable quantities of nitrogen from a constant supply of air.
  • the characterising feature of the process is that compressed air in excess of that required by the fractionation is expanded to provide additional refrigeration enabling a higher proportion of the nitrogen to be withdrawn as liquid and stored for use in a subsequent period of increased nitrogen demand.
  • a Pressure Indicator Controller will throttle to maintain the system pressure.
  • PIC Pressure Indicator Controller
  • Suction throttling is well known as a means of increasing part-load efficiency of centrifugal compressors. It decreases the suction pressure on the compressor and enables the compressor to operate with lower mass flow without encountering surge or severe guide vane angles.
  • the effect of suction throttling of centrifugal compressors is discussed by, for example, J. R. Gaston in "Centrifugal Compressor Operation & Control, Part II, Compressor Operation (Adv. Instrum. 31 (1976), Proc. 31st Annual ISA Conf. & Exhb., Houston, Texas, October 10-14 1976); F. B. Horowitz in “Graphical Interpretation of Centrifugal Compressor Controls" (Proc. Inst. Mech. Eng. IMechE Conf.
  • Figures 1 and 2 show the effect of suction throttling on the turndown of a centrifugal compressor.
  • Figure 1 the effect on turndown from design compressor flow (100%, point A) to 70% (point B) through the use of guide vane angle changes is shown.
  • the discharge pressure drops slightly due to lower pressure drops in the air separation plant. Further turndown cannot be achieved because of the approach to compressor surge.
  • Figure 2 shows the reduction in mass flow at turndown from 70 to 50% resulting from guide vane angle changes when suction throttling has reduced the discharge pressure to 70% of design pressure. Since both the suction and discharge pressures are reduced, the compressor curves shift significantly compared with Figure 1. The lower pressures decrease the density of the air and thereby cause an increase in actual volumetric flow compared with the same flow rate at design (i.e. normal operation pressures) thereby maintaining the compressor stage efficiencies at design levels.
  • the prior art requires that the same pressure conditions should be maintained in the distillation column system at turndown as at design flow and hence essentially the same discharge pressure is required from the supply feed compressor.
  • cryogenic gas separation to provide product at design pressure can be selectively operated at design flow or at turndown, especially at high turndown (i.e. greater than 30% turndown; less than 70% design flow), by suction throttling the supply feed compressor at turndown to reduce the supply feed pressure to the distillation column system and operating the distillation column system at sufficiently reduced product recovery to maintain the product pressure.
  • operation at high turndown required the use of two or more supply feed compressors with accompanying increases in capital cost and power requirement at design flow.
  • Use of suction throttling in accordance with the present invention incurs little capital cost, does not increase power requirement at design flow, and has equivalent power requirement at turndown to the use of two or more supply feed compressors.
  • the present invention provides a process for the cryogenic separation of a gaseous mixture, comprising a "light” component and a "heavy” component having a higher boiling point than the light component wherein a feed of said gaseous mixture in an amount selected from at least two flow rates is compressed in a centrifugal compressor; the compressed feed is fed to a distillation column system comprising a "high" pressure (“HP") column and a “low” pressure (“LP”) column operating at a lower pressure than the HP column; the compressed feed is rectified in the HP column to form a HP column gaseous overhead and a HP column liquid bottoms; at least a portion of the HP column liquid bottoms is fed to the LP column and is rectified therein to provide a gaseous light component product at essentially a constant pressure independent of said flow rates, and a heavy component-rich waste stream; at least a portion of the HP column gaseous overhead is condensed against LP column liquid bottoms to provide reboil to the LP column and condense the HP column
  • the upper flow rate will be the design rate for the compressor and the lower flow rate will be 50 to 70% of the design flow rate because conventional modifications such as guide vane angle variation can provide for turndown of up to 30%.
  • the centrifugal compressor has variable angle guide vanes and the selectable feed flow rates include an amount intermediate the higher and lower rates and at which intermediate flow rate the guide vane angles differ from those at the higher flow rate but the compressor supplies compressed feed to the HP column at the same pressure as at the higher flow rate.
  • the intermediate flow rate usually will be greater than 70% of the higher flow rate and the lower flow rate will be between 50 and 70% of the higher flow rate.
  • the invention has particular, but not exclusive, application to the separation of air to provide a gaseous nitrogen product. It has especial application to a nitrogen generator process in which the distillation column system comprises a "high" pressure (“HP") column and a “low” pressure (“LP”) column operating at a lower pressure than the HP column; the compressed air feed is fed to the HP column and rectified therein to form a HP column gaseous overhead and a HP column liquid bottoms; at least a portion of the HP column liquid bottoms is fed to the LP column and is rectified therein into the gaseous nitrogen product and an oxygen-rich waste stream; at least a portion of the HP column gaseous overhead is condensed against LP column liquid bottoms to provide reboil to the LP column and condense the HP column overhead; and respective portions of the condensed HP column overhead provide reflux to the HP column and LP column.
  • HP high pressure
  • LP low pressure
  • the HP and LP columns can be the only rectification columns in the distillation system and/or all of the HP column gaseous overhead suitably is condensed against LP column liquid bottoms to provide reboil to the LP column and fully condense the HP column overhead.
  • feed air 100 is compressed in a multistage centrifugal compressor 1 with interstage coolers and an after cooler (not shown). Water condensed from the air is removed in a separation pot or from the coolers and the compressed feed air is passed to a front end clean-up system 2 where remaining water, carbon dioxide and other contaminants are removed.
  • the clean, dry air 101 is cooled to near its dew point in main heat exchanger 3 against a nitrogen product stream 106 and a waste oxygen-rich stream 108.
  • the cooled air 102 is fed to a high pressure column 4 where it is rectified into a gaseous nitrogen-rich overhead and crude liquid oxygen bottoms.
  • the nitrogen overhead is condensed in reboiler/condenser 5 located in the bottom of a low pressure column 6.
  • a portion of the condensed nitrogen overhead is returned to the high pressure column 4 and the remainder 104 is reduced in pressure across a valve 7 and fed to the top of the low pressure column 6.
  • the crude liquid oxygen bottoms 103 is reduced in pressure across a valve 8 and fed to an intermediate location in the low pressure column 6.
  • the feed 103 and 104 to the low pressure column 6 is rectified in the column to provide a gaseous nitrogen overhead stream 105 and a waste oxygen-rich stream 107.
  • the nitrogen stream 105 provides the nitrogen product stream 106.
  • the waste stream 107 is partially warmed in the main heat exchanger 3, expanded in expander 9 to recover refrigeration and warmed in main heat exchanger 3 before removal as waste stream 108.
  • This waste stream 108 can be discharged to atmosphere and/or used as regeneration gas in the front end clean-up system 2.
  • the mass flow of air 100 to the main compressor is reduced without any significant reduction in the supply or discharge pressure of the main compressor 1.
  • the reduction in mass flow of the supply air to the main compressor is limited to avoid surge and severe guide vane angles in the compressor.
  • the operational pressures of the high pressure column 4 and low pressure column 6 remain unchanged compared with design flow and accordingly the nitrogen pressure and recovery remain essentially constant.
  • the turndown is to 70% of design flow
  • the amount of nitrogen product is reduced to 70% of design flow but the nitrogen product pressure and recovery (as a proportion of feed air) is substantially unchanged.
  • Turndown of the compressor to less than 70% design flow cannot be obtained because of the onset of surge in the compressor 1 at the maximum guide vane angle. If the distillation column system is to be turned down by more than 30%, the compressor must be operated at 30% turndown and the excess compressed air vented or recycled.
  • Figure 4 differs from Figure 3 only in so far as a butterfly, or other suction throttle, valve 10 is provided in the air supply 100 to the main compressor 1.
  • the process of Figure 4 operates in the same manner as the process of Figure 3 and can be operated at up to 30% turndown (70% design flow) by increasing the guide vane angle.
  • the throttle valve 10 is operated to throttle the feed to the compressor 1 and the rate of removal of nitrogen product in stream 106 is reduced by an amount proportionally greater than the reduction in air feed from the compressor 1.
  • the relative reduction of the nitrogen removal rate results in an increase in the nitrogen content of the waste stream 107 and hence a reduction in pressure in the high pressure column 4, thereby permitting the compression ratio across the compressor 1 to remain unchanged.
  • the Table below compares the material balance, pressures, relative capital and relative power of the system of Figure 3 of 30% turndown (70% of base flow) with the system of Figure 4 at 50% turndown. It also provides a comparison with the prior art modification of the system of Figure 3 in which the main compressor is replaced by two 60% compressors.
  • the present invention provides comparable performance at turndown with the prior art system using two compressors but with minimal capital expenditure increase and no power penalty when operating under design conditions.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (7)

  1. Verfahren für die Kryogene bzw. Tieftemperatur-Trennung bzw. Zerlegung eines gasförmigen Gemisches mit einer "leichten" Komponente und einer "schweren" Komponente, die einen höheren Siedepunkt als die leichte Komponente hat, wobei eine Einspeisung der gasförmigen Mischung in einer Menge, die aus wenigstens zwei Strömungsraten ausgewählt wird, in einem Zentrifugalkompressor bzw. Kreiselverdichter komprimiert wird; die komprimierte Einspeisung wird der HP Kolonne eines Destillationskolonnensystems mit einer "Hoch-" Druck- ("HP" für high pressure) Kolonne und einer "Nieder-" Druck- ("LP" für low pressure) Kolonne zugeführt, die bei dem niedrigeren Druck als die HP Kolonne arbeitet; die komprimierte Einspeisung wird in der HP Kolonne rektifiziert, um ein gasförmiges Kopfprodukt der HP Kolonne und ein flüssiges Bodenprodukt der HP Kolonne zu bilden; wenigstens ein Teil des flüssigen Bodenproduktes der HP Kolonne wird der LP Kolonne zugeführt und darin rektifiziert, um ein gasförmiges Produkt aus leichten Komponenten bei im wesentlichen einem konstanten Druck unabhängig von diesen Strömungsraten und einen Abfallstrom zur Verfügung zu stellen, der reich an der schweren Komponente ist; wenigstens ein Teil des gasförmigen Kopfproduktes der HP Kolonne wird gegen das flüssige Bodenprodukt der LP Kolonne kondensiert, um Aufkochen bzw. Reboil für die LP Kolonne zur Verfügung zu stellen und das Kopfprodukt der HP Kolonne zu kondensieren; die jeweiligen Anteile des kondensierten Kopfproduktes der HP Kolonne stellen Rückfluss für die HP Kolonne und die LP Kolonne zur Verfügung,
    dadurch gekennzeichnet, dass
    bei der unteren, aber nicht bei der höheren, der beiden Strömungsraten die Einspeisung zu dem Kompressor sauggedrosselt und die Gewinnung (relativ zu der Einspeisung) des Produktes aus der leichten Komponente reduziert werden (im Vergleich mit bei der höheren Strömungsrate), um den Druck der komprimierten Einspeisung zu der HP Kolonne im wesentlichen ohne Reduktion des Drucks des Produktes aus der leichteren Komponente von der LP Kolonne zu reduzieren (im Vergleich mit bei der höheren Strömungsrate).
  2. Verfahren nach Anspruch 1, wobei die niedrigere Strömungsrate 50 bis 70% der höheren Strömungsrate beträgt.
  3. Verfahren nach Anspruch 1 oder Anspruch 2, wobei der Kreiselverdichter Führungsflügel bzw. -schaufeln mit variablem Winkel hat, und wobei die auswählbaren Strömungsraten der Einspeisung eine Menge bzw. einen Betrag bzw. eine Rate zwischen der höheren und der niedrigeren Rate enthält, und wobei bei dieser Zwischen-Strömungsrate die Winkel der Führungsschaufeln sich von denen bei der höheren Strömungsrate unterscheiden, der Kompressor jedoch die komprimierte Einspeisung der HP Kolonne bei dem gleichen Druck wie bei der höheren Strömungsrate zuführt.
  4. Verfahren nach Anspruch 3, wobei die Zwischen-Strömungsrate größer als 70% der höheren Strömungsrate ist und die niedrigere Strömungsrate zwischen 50 und 70% der höheren Strömungsrate liegt.
  5. Verfahren nach einem der vorhergehenden Ansprüche, wobei das gasförmige Gemisch Luft ist und das gasförmige Produkt aus der leichten Komponente ein gasförmiges Stickstoff-Produkt ist.
  6. Verfahren nach einem der vorhergehenden Ansprüche, wobei die einzigen Rektifikations-Kolonnen in dem Destillationssystem die HP und die LP Kolonne sind.
  7. Verfahren nach einem der vorhergehenden Ansprüche, wobei das gesamte gasförmige Kopfprodukt der HP Kolonne gegen das flüssige Bodenprodukt der LP Kolonne kondensiert wird, um Aufkochen bzw. Reboil für die LP Kolonne zur Verfügung zu stellen und das Kopfprodukt der HP Kolonne vollständig zu kondensieren.
EP99300202A 1999-01-12 1999-01-12 Leistungsersparnisse für die Gastrennung bei Teillastbetrieb Expired - Lifetime EP1020695B1 (de)

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EP99300202A EP1020695B1 (de) 1999-01-12 1999-01-12 Leistungsersparnisse für die Gastrennung bei Teillastbetrieb
DE69911905T DE69911905T2 (de) 1999-01-12 1999-01-12 Leistungsersparnisse für die Gastrennung bei Teillastbetrieb

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EP99300202A EP1020695B1 (de) 1999-01-12 1999-01-12 Leistungsersparnisse für die Gastrennung bei Teillastbetrieb

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EP1020695B1 true EP1020695B1 (de) 2003-10-08

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8429933B2 (en) * 2007-11-14 2013-04-30 Praxair Technology, Inc. Method for varying liquid production in an air separation plant with use of a variable speed turboexpander

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2126700B (en) * 1982-09-15 1985-12-18 Petrocarbon Dev Ltd Improvements in the production of pure nitrogen
AT387454B (de) * 1986-05-14 1989-01-25 Voest Alpine Ag Einrichtung zum zerlegen von luft mit speicherung von produktgas in fluessiger form
US5081845A (en) * 1990-07-02 1992-01-21 Air Products And Chemicals, Inc. Integrated air separation plant - integrated gasification combined cycle power generator

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DE69911905T2 (de) 2004-09-02
EP1020695A1 (de) 2000-07-19

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