US3735599A - Process for automatic control of air separation apparatus - Google Patents

Process for automatic control of air separation apparatus Download PDF

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US3735599A
US3735599A US00104986A US3735599DA US3735599A US 3735599 A US3735599 A US 3735599A US 00104986 A US00104986 A US 00104986A US 3735599D A US3735599D A US 3735599DA US 3735599 A US3735599 A US 3735599A
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air
evaporator
condenser
control valve
pressure
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US00104986A
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T Izumichi
S Nakanishi
M Miyazaki
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Kobe Steel Ltd
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Kobe Steel Ltd
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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
    • F25J3/04248—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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
    • 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

  • ABSTRACT In an air separation apparatus which comprises a reversing heat exchanger, an air liquefier, a single column rectifier provided with a condenser-evaporator and a cold generation device and wherein air is cooled in the reversing heat exchanger and liquefied in the air liquefier, the liquefied air is rectified in the single column rectifier to separate into liquid air abundantly containing oxygen and highly pure nitrogen gas, the liquid air being subjected to heat exchange in the condenser-evaporator, the resulting gasified air being subjected to heat exchange in the air liquefier and sent through the reversing heat exchanger to the cold generation device and the resultant liquefied air being sent through the air liquefier and the reversing heat exchanger to release, a process for controlling the generation of cold which is
  • the present invention relates to a process for automatic control of an air separation apparatus. More particularly, it relates to a process for automatically controlling the rectifying conditions in a single column rectifier and the cold generating conditions of a cold generation device with the stabilized operation of an air separation apparatus.
  • the starting material i.e., a single column rectifier provided with a condenser-evaporator and a cold generation device such as an intermediate pressure expansion turbine
  • the starting material i.e., a single column rectifier provided with a condenser-evaporator and a cold generation device such as an intermediate pressure expansion turbine
  • the liquefied air is rectified in the single column rectifier and the waste gas formed in the condenser-evaporator is sent to the cold generation device for utilization as the source of cold.
  • factors for generation of cold in the cold generation device such as the pressures at the inlet and the outlet,
  • the pressure at the inlet and the flow volume are closely related to the pressure on the evaporation side and the evaporation volume in the condenser-evaporator of the single column rectifier.
  • the over-and-under rate of the cold in the entire air separation apparatus is judged on whether the liquid level of the evaporation side in the condenser-evaporator is in an ascending direction or in a descending direction.
  • the pressure at the inlet of the cold generation device is required to rise or the flow volume in the cold generation device must be increased.
  • the pressure at the inlet of the cold generation device is required to fall or the flow volume in the cold generation device should be decreased.
  • the pressure and the volume of air being treated in the single column rectifier should not be abruptly changed.
  • the waste gas fonned in the condenser-evaporator provided on the single column rectifier is supplied to the cold generation device. Therefore, the raising or lowering of the pressure at the inlet of the cold generation device results in raising or lowering of the pressure at the evaporation side of the condenser-evaporator.
  • Such variations in the pressure will inevitably cause a considerable change in the pressure and the volume of air being treated in the single column rectifier so that stabilized conditions for rectification can not be assured.
  • the maintenance of the pressure on the condensation side constant will result in a change of the temperature difference between the condensation side and the evaporation side whereby the heat exchange is increased or decreased, i.e., the volume of air being treated in the single column rectifier will change. If the volume of air being treated is kept constant, then the pressure on the condensation side must be varied so as to make constant the temperature difl'erence between the condensation side and the: evaporation side.
  • Rate of heat transfer Q 33,200 Kcal/h.
  • the temperature difference of the condenserevaporator is AT 2 i 05C.
  • the change of pressure corresponding to the afore-mentioned temperature will 5 come to 0.35 kglcm and, in turn, with the magnitude of pressure being 6.4 i 0.35 atg, the rate of variation of pressure on the condensation side becomes 1 5.5 percent.
  • the pressure variation on the condensation side of the condenser-evaporator exerts a great influence on the rectifying conditions in the single column rectifier.
  • it is indispensable to regulate the pressure on the evaporation side i.e., the inlet pressure of the cold generation device, when the heat balance of the entire apparatus is taken into consideration.
  • a method for controlling the generation of cold in an air separation apparatus comprising a single column rectifier provided with a'condenser-evaporator, a cold generation device and a passage connecting the condenserevaporator and the cold generation device, the passage having a by-pass channel connected to the outlet side of the cold generation device, where the starting air is liquefied with the cold generated in the cold generation device, the liquefied air is rectified in the single column rectifier, and the waste gas formed in the condenserevaporator is partly supplied to the cold generation device through the passage and the remaining waste gas to the by-pass channel, which is characterized in that the flow volume of the waste gas to the by-pass channel is controlled by the variation of the liquid level on the evaporation side of the condenser-evaporator.
  • FIG. 1 is a flow sheet showing a nitrogen producing apparatus as a preferred embodiment of the invention
  • FIG. 2 is a diagram with curves showing an example of the controlling of the liquid level and the pressure on the evaporation side of the condenser-evaporator by the opening of a control valve provided on the by-pass channel.
  • the starting air is supplied through tube 1 and compressed in a compressor 2.
  • compression can be up to around 6 to 7 kglcm
  • compression up to around 8 to 9 kg/cm can be effected.
  • the compressed air goes through a conduit tube 3 to the higher temperature portion 4 and the lower temperature portion 5 of a reversing heat exchanger where heat exchange with returning gas is performed.
  • the air thus cooled nearly to the liquefying temperature is sent through a check valve 6 and a conduit tube 7 and enters into the bottom portion of a single column rectifier 8 where the air is liquefied and separated into liquefied air containing an abundant amount of oxygen and gaseous air containing nitrogen in a high concentration.
  • the gaseous air taken out through a conduit tube 10 is heat exchanged with returning gas in an air liquefier 9 and the resulting liquefied air is returned through a conduit tube 11 to the bottom portion of the rectifier 8.
  • the liquid air at the bottom portion of the rectifier 8 is sent through a conduit tube 12 to a filter 13 where impurities such as CO and hydrocarbons are absorbed and eliminated. Then, the filtered liquid goes on through a flow control valve 14 where the pressure is reduced to around 3 to 4 kg/cm and enters into the evaporation side 15 of a condenser-evaporator 16.
  • the liquid air is heat exchanged with the nitrogen gas of high purity from the top portion of the rectifier 8 through a conduit tube 17 whereby the nitrogen gas is liquefied.
  • the liquefied nitrogen flows through a conduit tube 18 to the top portion of the rectifier 8.
  • the liquid air is vaporized as the result of the heat exchange and goes on through a conduit tube 19 for utilization as returning gas.
  • a major portion of the above vaporized air flowing through the conduit tube 19 is sent through a conduit tube 20 to the liquefier 9 and flows through a conduit tube 21 where it is separated into two portions, one of them going through a control valve 22 and a conduit tube 23 to the lower temperature portion 5 for heat exchange with the starting air coming from the compressor 2 to liquefy CO therein and then flowing through a conduit tube 24 and a control valve 25 to an expansion turbine 26.
  • the other portion is sent from the conduit tube 21 through a control valve 27 and combined with the above returning gas.
  • the combined gas is expanded in the expansion turbine 26 nearly to atmospheric pressure whereby any thermo-dynamic exterior work is performed and the temperature is lowered remarkably to generate the cold sufficient to fulfill the demand for the apparatus.
  • the expanded gas flows through conduit tubes 28 and 29 to the liquefier 9 and then goes through a conduit tube 30 and the check valve 6 to the reversing heat exchanger.
  • the gas is warmed to room temperature as the result of the heat exchange with the starting material air and then discharged through a conduit tube 31.
  • the control valve 32 regulates the flow volume and the pressure at the inlet of the expansion turbine 26 and thus controls the generation of cold.
  • the control valve 32 moves toward the closed position whereby the flow volume in the expansion turbine 26 is increased and the level of the liquid air in the condenser evaporator increases toward the set level.
  • the control valve 32 is operated to move toward the open position whereby the flow volume in the expansion turbine is decreased and the level of the liquid air decreases toward the set level.
  • control valve 32 when the control valve 32 is moved toward the closed position in such a manner that the pressure on the evaporation side 15 of the condenser-evaporator 16 is increased abruptly, there is a danger of disturbing the stabilized rectifying conditions of the single column rectifier; and besides, there will be a considerable time lag from the action of the control valve 32 to the actual return to the set liquid level.
  • FIG. 2 which shows the operation of the apparatus under the control of such a mechanism
  • sh wn the relative variations of the liquid level L of the liquid air on the evaporation side 15 of the condenserev porator 16
  • the control valve 32 is activated to move toward the closed position so as to increase the flow volume in the expansion turbine 26.
  • the controlling arrangement should be such that a drastic pressure variation does not occur with respect to the liquid level.
  • the control valve 32 When the control valve 32 is moved toward the closed position, if the liquid level restores itself as indicated at e in the diagram and, along with it, the pressure P as well as the degree of valve opening V also respectively move up to the initial values Po and V0, then the control is deemed satisfactory. In the event, however, that the liquid level lowering still continues and does not cease and, in turn, the pressure raises to P then a control measure is taken to maintain the degree of valve opening at V, which is the degree of opening for pressure P An appropriate value for P may be P(,+0.05-O.l kg/cm.
  • the cold balance is successfully achieved without allowing the pressure on the evaporation side to go through a large change in the time lag from the start of movement of the control valve 32 to the actual recovery of the liquid level; in other words, the cold balance can be maintained without impairing or disturbing the rectifying conditions. If during the time the 7 degree of valve opening is maintained at V if the liquid level shows a tendency to be restored as shown at d in the diagram, then the pressure which has been maintained at Pg until the recovery of the liquid level to L0 will start to return towards Po as the valve starts opening. If the liquid level still continues to fall, then a control measure is taken to close the valve further so that the pressure P goes up at the time when the liquid level has dropped to L,,.
  • the liquid level When the apparatus is in a stable stage of operation, the liquid level generally restores itself at the time or t and further supplementary control is seldom needed unless the heat balance is disturbed by some external factor. But, the set value may be appropriately changed depending on the temperature change with the seasons after the time The above illustration is for the case where the liquid level falls but the same may be applied to the case where the liquid level ascends.
  • an air separation apparatus which comprises a reversing heat exchanger, a single column rectifier connected to said reversing heat exchanger for receiving cooled air therefrom, said rectifier having a condenserevaporator, an air liquifier connected to said rectifier for receiving gaseous air therefrom and returning it to said rectifier after cooling it, a vaporized air line from the rectifier on the evaporater side of said condenser evaporator to said air liquifier, a cold generation device coupled to said air liquifier for receiving air from the air liquifier through the reversing heat exchanger and expanding it, and an expanded air line from said cold generation device to said air liquifier, the liquified air from the air liquifier being rectified in the rectifier to separate into liquid air rich in oxygen and highly pure nitrogen gas, the liquid air being subjected to heat exchange in the condenser-evaporator and the resulting vaporized air being subjected to heat exchange in the air li
  • control means stops the control valve at the time when the pressure on the evaporation side of the condenser-evaporator has varied to a certain extent from a set value so as to control the time lag during recovery of the liquid level.
  • a method for automatic control of an air separation apparatus having a single column rectifier pro vided with a condenser evaporator which comprises flowing vaporized air from the evaporator side of said condenser-evaporator through an air liquifier, a heat exchanger and an expansion type cold generation device and then back through said air liquifier, by-passing 5 a portion of the vaporized air through a control valve from the evaporator condenser to the output side of the cold generation device, changing the degree of opening of the control valve in response to the level of liquid air on the evaporation side of the condenser-evaporator for controlling the flow of the bypassed part of the vaporized air to adjust the flow ratio of said part relative to that of the other part of said vaporized air which is passed through a cold generating device and fixing the amount of opening of the control valve when the pressure on the evaporation side has varied to a predetermined extent from the pressure existing before the change of the degree of opening of the valve.
US00104986A 1970-01-09 1971-01-08 Process for automatic control of air separation apparatus Expired - Lifetime US3735599A (en)

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JP45002800A JPS4940071B1 (de) 1970-01-09 1970-01-09

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JP (1) JPS4940071B1 (de)
DE (1) DE2100397B2 (de)
FR (1) FR2076020B1 (de)
GB (1) GB1329222A (de)

Cited By (15)

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Publication number Priority date Publication date Assignee Title
US4299607A (en) * 1979-05-16 1981-11-10 Hitachi, Ltd. Process for recovering nitrogen in low pressure type air separation apparatus
US4400188A (en) * 1981-10-27 1983-08-23 Air Products And Chemicals, Inc. Nitrogen generator cycle
US4731102A (en) * 1985-08-12 1988-03-15 Daidousanso Co., Ltd. Oxygen gas production apparatus
US4732595A (en) * 1985-08-23 1988-03-22 Daidousanso Co., Ltd. Oxygen gas production apparatus
US4783210A (en) * 1987-12-14 1988-11-08 Air Products And Chemicals, Inc. Air separation process with modified single distillation column nitrogen generator
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
US4931070A (en) * 1989-05-12 1990-06-05 Union Carbide Corporation Process and system for the production of dry, high purity nitrogen
US4934148A (en) * 1989-05-12 1990-06-19 Union Carbide Corporation Dry, high purity nitrogen production process and system
US4957524A (en) * 1989-05-15 1990-09-18 Union Carbide Corporation Air separation process with improved reboiler liquid cleaning circuit
US5004482A (en) * 1989-05-12 1991-04-02 Union Carbide Corporation Production of dry, high purity nitrogen
US5116396A (en) * 1989-05-12 1992-05-26 Union Carbide Industrial Gases Technology Corporation Hybrid prepurifier for cryogenic air separation plants
US5257206A (en) * 1991-04-08 1993-10-26 Praxair Technology, Inc. Statistical process control for air separation process
US5333463A (en) * 1992-07-29 1994-08-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Production and installation for the production of gaseous nitrogen at several different purities
US20090120129A1 (en) * 2007-11-14 2009-05-14 Henry Edward Howard Cryogenic variable liquid production method
USRE43121E1 (en) * 2000-04-04 2012-01-24 Venturedyne Limited Cascade refrigeration system

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Publication number Priority date Publication date Assignee Title
DE2335096C2 (de) * 1973-07-10 1982-03-18 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Gewinnung von gasförmigem Sauerstoff und gasförmigem Stickstoff
DE4206923A1 (de) * 1992-03-05 1993-09-09 Linde Ag Verfahren und vorrichtung zur zerlegung eines gasgemisches
US5996373A (en) * 1998-02-04 1999-12-07 L'air Liquide, Societe Ananyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus

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US3375673A (en) * 1966-06-22 1968-04-02 Hydrocarbon Research Inc Air separation process employing work expansion of high and low pressure nitrogen

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DE1222088B (de) * 1965-06-16 1966-08-04 Linde Ag Verfahren und Vorrichtung zum Zerlegen eines Gasgemisches bei tiefer Temperatur

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US2460859A (en) * 1944-05-01 1949-02-08 Kellogg M W Co Method of gas separation including impurity removing steps
US2552560A (en) * 1945-12-05 1951-05-15 Hydrocarbon Research Inc Process of producing oxygen
US2537044A (en) * 1946-11-29 1951-01-09 Hydrocarbon Research Inc Continuous method of producing oxygen involving the use of a thermophore and the purging thereof
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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4299607A (en) * 1979-05-16 1981-11-10 Hitachi, Ltd. Process for recovering nitrogen in low pressure type air separation apparatus
US4400188A (en) * 1981-10-27 1983-08-23 Air Products And Chemicals, Inc. Nitrogen generator cycle
US4731102A (en) * 1985-08-12 1988-03-15 Daidousanso Co., Ltd. Oxygen gas production apparatus
US4732595A (en) * 1985-08-23 1988-03-22 Daidousanso Co., Ltd. Oxygen gas production apparatus
US4783210A (en) * 1987-12-14 1988-11-08 Air Products And Chemicals, Inc. Air separation process with modified single distillation column nitrogen generator
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
US5116396A (en) * 1989-05-12 1992-05-26 Union Carbide Industrial Gases Technology Corporation Hybrid prepurifier for cryogenic air separation plants
US4931070A (en) * 1989-05-12 1990-06-05 Union Carbide Corporation Process and system for the production of dry, high purity nitrogen
US4934148A (en) * 1989-05-12 1990-06-19 Union Carbide Corporation Dry, high purity nitrogen production process and system
US5004482A (en) * 1989-05-12 1991-04-02 Union Carbide Corporation Production of dry, high purity nitrogen
US4957524A (en) * 1989-05-15 1990-09-18 Union Carbide Corporation Air separation process with improved reboiler liquid cleaning circuit
US5257206A (en) * 1991-04-08 1993-10-26 Praxair Technology, Inc. Statistical process control for air separation process
US5333463A (en) * 1992-07-29 1994-08-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Production and installation for the production of gaseous nitrogen at several different purities
USRE43121E1 (en) * 2000-04-04 2012-01-24 Venturedyne Limited Cascade refrigeration system
US20090120129A1 (en) * 2007-11-14 2009-05-14 Henry Edward Howard Cryogenic variable liquid production method
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

Also Published As

Publication number Publication date
FR2076020B1 (de) 1973-12-07
FR2076020A1 (de) 1971-10-15
DE2100397A1 (de) 1971-08-12
JPS4940071B1 (de) 1974-10-30
DE2100397B2 (de) 1981-04-16
GB1329222A (en) 1973-09-05

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