EP0952415A1 - Procédé et installation de distillation d'air avec production variable d'argon - Google Patents

Procédé et installation de distillation d'air avec production variable d'argon Download PDF

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Publication number
EP0952415A1
EP0952415A1 EP99400957A EP99400957A EP0952415A1 EP 0952415 A1 EP0952415 A1 EP 0952415A1 EP 99400957 A EP99400957 A EP 99400957A EP 99400957 A EP99400957 A EP 99400957A EP 0952415 A1 EP0952415 A1 EP 0952415A1
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EP
European Patent Office
Prior art keywords
column
argon
installation
medium pressure
pressure column
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.)
Withdrawn
Application number
EP99400957A
Other languages
German (de)
English (en)
French (fr)
Inventor
François De Bussy
Frédéric Staine
Bernard Saulnier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from FR9804972A external-priority patent/FR2777641B1/fr
Priority claimed from FR9816245A external-priority patent/FR2787562B1/fr
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0952415A1 publication Critical patent/EP0952415A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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
    • F25J3/048—Argon recovery
    • F25J3/04806—High purity argon purification
    • 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—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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    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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    • 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
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
    • 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
    • F25J2250/58—One fluid being argon or crude argon
    • 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
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

Definitions

  • the invention relates to an air distillation process with production of argon by means of an air distillation installation comprising an air distillation apparatus and at least one column for producing impure argon, the installation being intended to supply argon with a nominal yield ⁇ n of argon extraction at the outlet of said column for producing impure argon.
  • the invention applies in particular to the production of argon by means of air distillation plants with double distillation column.
  • medium pressure nitrogen is generally taken off at the head of the medium pressure column of the double column.
  • This medium pressure nitrogen is used, generally after expansion in a turbine, as a cooling source, in particular for cooling the air to be distilled.
  • part of the cooling energy supplied to the air to be distilled can be recovered and therefore limit the operating costs of such an installation.
  • Such an installation is sized to meet nominal argon production needs, with a nominal yield ⁇ n of argon extraction at the outlet of the impure argon production column, known as the mixture column.
  • ⁇ n nominal yield of argon extraction at the outlet of the impure argon production column
  • the object of the invention is to provide an air distillation process with production of argon which makes it possible to optimize the operating costs when the needs for production of argon are lower than the nominal needs.
  • the subject of the invention is a process for the distillation of air with the production of argon by means of an air distillation installation comprising an apparatus for air distillation and at least one impure argon production column, the installation being dimensioned to supply argon with a nominal output pn of argon extraction at the outlet of said impure argon production column, characterized in that for reduced argon production requirements corresponding to a necessary yield p of argon extraction at the outlet of the impure argon production column, with ⁇ ⁇ ⁇ o ⁇ ⁇ n where ⁇ o is a predetermined optimal yield , the argon extraction yield at the outlet of the impure argon production column is maintained substantially at the po value.
  • the invention also relates to an installation for implementing the method as defined above, characterized in that it comprises an air distillation apparatus, at least one column for producing impure argon, a heat exchanger, in particular crossed by a line for supplying air to be distilled, and at at least one bypass line for sending at least an excess part of the extracted argon to said heat exchanger.
  • FIG. 5 is a view similar to FIG. 1, illustrating a third embodiment of an air distillation installation according to the invention.
  • FIG. 6 is a view similar to FIG. 3, illustrating a fourth embodiment of an air distillation installation according to the invention.
  • FIG. 1 illustrates an installation 1 for air distillation with production of argon.
  • This installation 1 essentially comprises a double column 2 for air distillation, a column 3 for the production of impure argon known as the mixture column, a column 4 for the production of pure argon known as the denitrogenation column, a main heat exchange line 5, a main air compressor to be distilled 6 and an air purifying apparatus to be distilled 7.
  • the double column 2 comprises a medium pressure column 8, operating under a medium pressure for example of 6 bar absolute, a low pressure column 9, operating under a low pressure below the medium pressure, for example a pressure slightly greater than 1 bar absolute , and a main vaporizer-condenser 10.
  • the column 3 for producing impure argon comprises a head condenser 12 for partially condensing the impure argon at the head of column 3.
  • the column 4 for the production of pure argon comprises an overhead condenser 13 and a tank vaporizer 14.
  • a gas pipe 19 connects an outlet from the head condenser 12 of column 3 to an intermediate level of column 4 for producing roughly pure argon.
  • This pipe draws off the non-condensed part in the condenser 12 of the impure argon at the head of the column 3.
  • This pipe 19 passes successively from the column 3, a heat exchanger 20, to condense the impure argon gas, and a expansion valve 21, to relax this impure condensed argon.
  • the gaseous air to be distilled, compressed by the compressor 6 and purified of water and CO 2 , for example by adsorption, in the apparatus 7, is divided into two primary streams.
  • the first primary air flow is cooled in the main heat exchange line 5 and then divided into two secondary flows.
  • the first secondary flow is injected into the tank of the medium pressure column near its dew point.
  • the second secondary flow is sent to the tank vaporizer 14 of the column 4 for the production of pure argon, where this second secondary flow is liquefied by vaporizing the tank argon of this column 4.
  • the liquid thus produced is sent by a line 23 to the tank of the medium pressure column 8.
  • the second primary flow of compressed and purified air is compressed by a compressor 230, then liquefied at the crossing of the main heat exchange line 5 and expanded in an expansion valve 231 substantially until the pressure prevailing in the middle column pressure 8.
  • a first part of this flow is then injected at a level intermediate of the medium pressure column 8.
  • the other part of this flow is sub-cooled through a heat exchanger 24, then expanded in an expansion valve 240 and injected at the intermediate level of the low pressure column 9.
  • the vaporizer-condenser 10 vaporizes liquid oxygen in the bottom of the low pressure column 9 by condensing nitrogen at the top of the medium pressure column 8.
  • Lean liquid (almost pure nitrogen) LP is taken from the upper part of the medium pressure column 8, then sub-cooled in the heat exchanger 24, and finally divided into three streams.
  • the first flow is expanded in an expansion valve 30 then injected at the top of the low pressure column 9.
  • the second flow is expanded in an expansion valve 31 then vaporized in the heat exchanger 20, condensing the impure channeled argon via line 19, then this vaporized flow is again expanded in an expansion valve 32.
  • This second flow is then returned by a waste line 33 to the heat exchanger 24, where this second flow is heated by cooling the liquids LP and LR passing through the exchanger 24.
  • This second flow is finally sent to the main heat exchange line 5, where this second flow is heated by participating in the cooling of the air to be distilled.
  • Third lean liquid flow is relaxed in an expansion valve 34 before being sent to the condenser 13 at the head of the column 4 for the production of pure argon, where this third stream is vaporized by condensation of the impure nitrogen at the head of the column 4.
  • the gas thus product is sent, after expansion in an expansion valve 35, in the waste pipe 33 to be heated on the one hand in the heat exchanger 24 while cooling the liquids LP and LR and, on the other hand, in the main heat exchange line 5 by participating in the cooling of the air to be distilled.
  • Impure or residual nitrogen NR withdrawn from the top of the low-pressure column 9, is sent to the waste pipe 33, where this impure nitrogen is heated at the crossing of the heat exchanger 24, then of the main line heat exchange 5.
  • Liquid oxygen OL withdrawn from the tank of the low pressure column 9, is pumped by a pump 37 then sent by a pipe 38 to the main heat exchange line 5, where this liquid oxygen is vaporized while participating in the cooling of the air to be distilled.
  • NGMP medium pressure nitrogen gas is taken off at the head of the medium pressure column 8 and then sent via a pipe 39 to the heat exchange line 5 to participate in the cooling of the air to be distilled.
  • the medium pressure nitrogen gas is divided into two flows. The first flow crosses the rest of the line 5 where it is heated then it is distributed by a production line 40, for example to supply a consuming installation 140.
  • the second flow is expanded in a turbine 41 then sent to the waste line 33 at the cold end of the heat exchange line 5, to participate again in cooling the air to be distilled.
  • NLMP medium pressure liquid nitrogen is drawn off at the head of the medium pressure column 8 and then sent via a pipe 43 to the heat exchanger 24, where this liquid nitrogen is sub-cooled by heating the residual gases channeled through the residual 33.
  • This liquid nitrogen is then distributed, by supplying for example, after expansion in an expansion valve 143, a storage tank 144.
  • the installation 1 further comprises a bypass line 48 whose inlet 49 is connected to line 19, between the heat exchanger 20 and the expansion valve 21, and whose outlet 50 opens into the waste line 33 , just upstream of the heat exchanger 24.
  • This bypass line 48 will be described later.
  • the medium pressure column 8 has for example 40 theoretical plates, and the low pressure column 9 has for example 65 theoretical plates.
  • Plant 1 is dimensioned, for example, to treat an air flow of 1,000 Nm 3 / h and extract 207.4 Nm 3 / h of pure oxygen, 6.4 Nm 3 / h of pure argon and 160 Nm 3 / h of medium pressure nitrogen gas.
  • the extraction efficiency ⁇ of argon at the outlet of column 3 necessary to satisfy these reduced needs is less than ⁇ o.
  • the extraction yield is maintained at the value ⁇ o and the excess of argon thus extracted is returned at the outlet of column 3 for the production of impure argon towards the waste pipe 33 via the waste pipe. bypass 48.
  • Case 1 corresponds to the nominal operating conditions of installation 1.
  • Cases 2A and 2B correspond to the operation of the installation for requirements for the supply of argon lower than the nominal requirements and corresponding to a necessary argon extraction yield ⁇ at the outlet of column 3 approximately equal to 30%.
  • Cases 3A and 3B correspond to the operation of installation 1 of argon for supply needs of argon zero and therefore corresponding to a necessary argon extraction yield ⁇ equal to 0%.
  • a and B correspond respectively to the implementation of a method according to the prior art and to the implementation of a method according to the invention. It is assumed in these cases that the liquid medium pressure nitrogen is withdrawn with a constant flow rate.
  • the method according to the invention makes it possible to maintain the quantity of gaseous medium pressure nitrogen withdrawn at its maximum level.
  • the excess of medium pressure nitrogen gas thus extracted that is to say D ( ⁇ o) -D ( ⁇ ) makes it possible to reduce the energy necessary for the operation of installation 1 by approximately 3% in the case 2B compared to case 2A, and around 6% in case 3B compared to case 3A.
  • the medium pressure excess nitrogen obtained by carrying out the process can be used in different ways.
  • this excess can be taken in liquid and / or gaseous form at the top of the medium pressure column 8, valued by supplying it to a consuming installation, or used as a refrigerating source in installation 1. It is thus possible, for example, to increase the amount of medium pressure nitrogen gas expanded in the turbine 41 and therefore, for example, reducing the amount of liquid oxygen passing through the main heat exchange line 5.
  • a pipe 52 (shown in dotted lines in FIG. 1) can allow direct production of liquid oxygen.
  • the bypass line 48 makes it possible to recover the refrigerating energy of the excess argon extracted at the outlet of the column 3 for the production of impure argon.
  • This excess argon is in fact used as a refrigeration source in the heat exchanger 24 and in the heat exchange line 5.
  • this bypass line 48 can be eliminated, the excess argon extracted then being vented, or the inlet of this bypass line 48 can thus be connected to other places in the installation. 1.
  • the inlet 49 of the pipe 48 can be connected to the tank or to the head of the column 4 for the production of pure argon, in order to take the excess of argon extracted by the column 3.
  • the inlet 49 of the pipe 48 can also be connected to the head of the column 3 for the production of impure argon to take off impure argon gas, as illustrated in FIG. 2.
  • bypass pipe 48 can independently cross the heat exchanger 24 and / or the main heat exchange line 5, without the excess extracted argon being mixed with a waste gas.
  • the optimal efficiency ⁇ o may be different from the nominal efficiency ⁇ n. This yield ⁇ o is generally less than ⁇ n.
  • the extraction efficiency of argon is maintained at the value ⁇ o for needs in supply of argon corresponding to a necessary yield ⁇ ⁇ o ⁇ n.
  • the extraction yield ⁇ o is optimal relative to the quantity of medium pressure nitrogen which can be drawn off at the head of the medium pressure column 8.
  • a first example, illustrated by FIG. 3, relates to air distillation installations where the cold resistance is ensured by an air blowing turbine.
  • this turbine 501 is disposed in a pipe 502 which connects the outlet of the air cleaning device 7 to an intermediate level of the column low pressure 9, and which at least partially crosses the heat exchange line 5.
  • the turbine 501 expands at low pressure, to the pressure drop, air purified by the device 7 then compressed by an auxiliary compressor 503 coupled to the turbine 501.
  • This air blowing turbine 501 ensures the cold behavior of the installation 1 in place of the turbine 41 of FIG. 1.
  • the efficiency ⁇ o can be the optimal efficiency , for a predetermined quantity of medium pressure nitrogen gas withdrawn at the head of the medium pressure column 9, with respect to the quantity of air expanded in the air blowing turbine.
  • FIG. 4 illustrates a second example where the air distillation apparatus 2 is a simple distillation column.
  • impure NC nitrogen is drawn off at the top of column 2, then reheated in a heat exchanger 51, compressed in a compressor 52, and cooled in exchanger 51 by heat exchange with nitrogen NC at compress.
  • This compressed and cooled nitrogen is then liquefied, ensuring the vaporization of the tank oxygen in column 2.
  • the liquefied nitrogen is then expanded in an expansion valve 53 and then reintroduced at the top of column 2.
  • the yield ⁇ o then corresponds substantially at the minimum flow rate of impure nitrogen overhead NC to be used to vaporize the tank oxygen. Maintaining the extraction efficiency of argon at ⁇ o during periods of reduced argon supply requirements makes it possible to reduce the compression energy supplied to the cycle compressor 52 and therefore the operating costs of the installation 1 .
  • the liquid argon from the condenser 20 is sent to point 50 where it mixes with impure nitrogen (lower lean liquid) withdrawn at an intermediate level from the medium pressure column 8 and sent to line 133.
  • the mixture is partly sent in head of the low pressure column 9 after expansion in the valve 30.
  • a part of the mixture is sent after expansion in the valve 31 to the condenser 20 and another part is sent after expansion in the valve 34 to the condenser 13.
  • the rest of the apparatus is identical to that of FIG. 1.
  • the gas produced by vaporization in the condenser 13 is expanded in the valve 35 and mixed with the residual nitrogen from the low pressure column 9.
  • the liquid argon from the tank of column 4 is sent partly in line 33.
  • the gas vaporized by the condenser 20 is expanded at 32 and possibly mixed with the liquid argon in the bypass line 48.
  • the liquid argon is then mixed with the lower lean liquid of the medium pressure column and sent to the head of the low pressure column after expansion. All the impure argon from line 19 is sent to column 4 for the production of pure argon.
  • the method according to the invention makes it possible to reduce the energy to be supplied to air distillation installations with production of argon.
  • the frigories of the device can be produced in part by a Claude turbine or a hydraulic turbine.
  • the process can also produce pressurized nitrogen by drawing liquid nitrogen from the medium pressure column, pressurizing and vaporizing it in the exchange line.
  • the process does not necessarily include the pressurization of a liquid before its vaporization in the exchange line.
  • the air separation apparatus can be a triple column or can include a mixing column.

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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)
EP99400957A 1998-04-21 1999-04-20 Procédé et installation de distillation d'air avec production variable d'argon Withdrawn EP0952415A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
FR9804972 1998-04-21
FR9804972A FR2777641B1 (fr) 1998-04-21 1998-04-21 Procede et installation de distillation d'air avec production d'argon
FR9816245A FR2787562B1 (fr) 1998-12-22 1998-12-22 Procede et installation de distillation d'air avec production d'argon
FR9816245 1998-12-22

Publications (1)

Publication Number Publication Date
EP0952415A1 true EP0952415A1 (fr) 1999-10-27

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Country Status (6)

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US (1) US6269659B1 (pt)
EP (1) EP0952415A1 (pt)
JP (1) JP2002511136A (pt)
AU (1) AU743283B2 (pt)
BR (1) BR9906366A (pt)
WO (1) WO1999054673A1 (pt)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7093649B2 (en) 2004-02-10 2006-08-22 Peter Dawson Flat heat exchanger plate and bulk material heat exchanger using the same
EP1143216B1 (fr) * 2000-04-04 2012-03-07 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil de production d'un fluide enrichi en oxygène par distillation cryogénique
FR3110685A1 (fr) * 2020-05-20 2021-11-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d’air par distillation cryogénique
EP4023983A1 (en) * 2020-12-31 2022-07-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for transfer of liquid

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2791762B1 (fr) * 1999-03-29 2001-06-15 Air Liquide Procede et installation de production d'argon par distillation cryogenique
US20060005574A1 (en) * 2002-04-12 2006-01-12 Reinhard Glatthaar Method for extracting argon by low-temperature air separation
US7113450B2 (en) * 2003-05-20 2006-09-26 Timex Group B.V. Wearable electronic device with multiple display functionality
FR2911392A1 (fr) * 2007-01-16 2008-07-18 Air Liquide Procede et appareil de production d'argon par distillation cryogenique
FR2943773B1 (fr) * 2009-03-27 2012-07-20 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US8899075B2 (en) * 2010-11-18 2014-12-02 Praxair Technology, Inc. Air separation method and apparatus
JP2017536523A (ja) * 2014-10-16 2017-12-07 リンデ アクチエンゲゼルシャフトＬｉｎｄｅ Ａｋｔｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ 極低温分離によってアルゴンを可変的に取得する方法及び装置
EP3048401A1 (de) 2015-01-20 2016-07-27 Linde Aktiengesellschaft Verfahren und vorrichtung zur variablen gewinnung von argon durch tieftemperturzerlegung von luft
CN109764638B (zh) * 2018-12-13 2021-11-19 包头钢铁（集团）有限责任公司 一种大型制氧机组氩系统变负荷方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3447331A (en) * 1966-06-01 1969-06-03 British Oxygen Co Ltd Air separation employing waste nitrogen reheated by incoming air in work expansion
US4932212A (en) * 1988-10-12 1990-06-12 Linde Aktiengesellschaft Process for the production of crude argon
EP0384213A2 (de) * 1989-02-23 1990-08-29 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Luftzerlegung durch Rektifikation
EP0540900A1 (en) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4317916A1 (de) * 1993-05-28 1994-12-01 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Argon
FR2716816B1 (fr) * 1994-03-02 1996-05-03 Air Liquide Procédé de redémarrage d'une colonne auxiliaire de séparation argon/oxygène par distillation, et installation correspondante.
US5682767A (en) * 1996-11-18 1997-11-04 Air Liquide Process And Construction Argon production

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3447331A (en) * 1966-06-01 1969-06-03 British Oxygen Co Ltd Air separation employing waste nitrogen reheated by incoming air in work expansion
US4932212A (en) * 1988-10-12 1990-06-12 Linde Aktiengesellschaft Process for the production of crude argon
EP0384213A2 (de) * 1989-02-23 1990-08-29 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Luftzerlegung durch Rektifikation
EP0540900A1 (en) * 1991-10-10 1993-05-12 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1143216B1 (fr) * 2000-04-04 2012-03-07 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil de production d'un fluide enrichi en oxygène par distillation cryogénique
US7093649B2 (en) 2004-02-10 2006-08-22 Peter Dawson Flat heat exchanger plate and bulk material heat exchanger using the same
FR3110685A1 (fr) * 2020-05-20 2021-11-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d’air par distillation cryogénique
US11852408B2 (en) 2020-05-20 2023-12-26 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for separating air by cryogenic distillation
EP4023983A1 (en) * 2020-12-31 2022-07-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for transfer of liquid
US11828532B2 (en) 2020-12-31 2023-11-28 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for transfer of liquid

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Publication number Publication date
JP2002511136A (ja) 2002-04-09
WO1999054673A1 (fr) 1999-10-28
AU743283B2 (en) 2002-01-24
US6269659B1 (en) 2001-08-07
AU3336899A (en) 1999-11-08
BR9906366A (pt) 2000-09-19

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