WO1999054673A1 - Procede et installation de distillation d'air avec production d'argon - Google Patents
Procede et installation de distillation d'air avec production d'argon Download PDFInfo
- Publication number
- WO1999054673A1 WO1999054673A1 PCT/FR1999/000931 FR9900931W WO9954673A1 WO 1999054673 A1 WO1999054673 A1 WO 1999054673A1 FR 9900931 W FR9900931 W FR 9900931W WO 9954673 A1 WO9954673 A1 WO 9954673A1
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- WO
- WIPO (PCT)
- Prior art keywords
- column
- argon
- installation
- medium pressure
- pressure column
- Prior art date
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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
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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- 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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- 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
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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
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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
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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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- 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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- 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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- F25J3/04406—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
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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
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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
- 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 pn of extraction of argon 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 dimensioned to meet nominal argon production needs, with a nominal output pn of argon extraction at the outlet of the impure argon production column, known as the mixture column.
- a nominal output pn of argon extraction at the outlet of the impure argon production column known as the mixture 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 air distillation apparatus and at least one column for the production of impure argon, 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 argon production needs reduced corresponding to a necessary yield p of argon extraction at the outlet of the impure argon production column, with p ⁇ po ⁇ pn where po is a predetermined optimal yield, the argon extraction yield is maintained in outlet from the impure argon production column substantially at the po value.
- the process can comprise one or more of the following characteristics, taken individually or according to all technically possible combinations: the argon extracted in excess with respect to the necessary extraction yield p is used as a refrigerating source in the 'air distillation installation, for example to cool the air to be distilled;
- this withdrawn part is sent to at least one exchanger. heat from the installation or to the air distillation apparatus;
- the air distillation apparatus comprising a double column itself comprising a medium pressure column, a low pressure column and a vaporizer-condenser for connecting the heat exchange head of the medium pressure column with the tank from the low pressure column, medium pressure nitrogen is withdrawn from the head of the medium pressure column, po is the yield for which one can extract a maximum flow rate D (po) of medium pressure nitrogen, and for a yield d 'necessary extraction p less than in. a medium pressure nitrogen flow greater than D (p) is drawn off;
- the air distillation apparatus comprising a double column itself comprising a medium pressure column, a low pressure column and a vaporizer-condenser for connecting the heat exchange head of the medium pressure column with the tank from the low pressure column, medium pressure nitrogen is withdrawn from the head of the medium pressure column, po is the output for which one can relax a maximum air flow D '(po) of air at low pressure, with production of external work, with a view to injecting it into the low pressure column, and for a necessary extraction yield p less than in., an air flow greater than D 1 is relaxed at low pressure, with production of external work (po), and in particular equal to D '(po).
- 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 least one bypass pipe for send at least a part in excess of 1 • extracted argon to said heat exchanger.
- the installation can include one or more of the following characteristics, taken in isolation or according to all technically possible combinations:
- An inlet of said bypass pipe is connected to an outlet of liquid or gaseous argon from the head of the column for the production of impure argon;
- the installation comprises an almost pure argon production column connected to the impure argon production column, and an inlet of said bypass pipe is connected to an outlet for gas or liquid from the tank or the head of the almost pure argon production column;
- Said bypass line is connected to a waste fluid outlet of one of the columns of the installation for mixing a waste fluid with the argon channeled in said bypass line;
- said bypass line is connected to a fluid inlet of one of the columns of the installation for mixing the fluid with the argon channeled in said bypass line;
- the distillation apparatus comprises a double distillation column itself comprising a medium pressure column, a low pressure column and a vaporizer-condenser for connecting heat exchange to the head of the medium pressure column and to the tank of the low pressure column, the head of the medium pressure column has a medium pressure nitrogen outlet, and a pipe connects said medium pressure nitrogen outlet to a heat exchanger of the installation, which is notably crossed by a pipe supply of air to be distilled;
- the installation includes a purge air blower in the low pressure column.
- FIG. 1 is a schematic view of an air distillation installation with production of argon according to the invention
- FIG. 2 is a partial enlarged view of a variant of the installation of FIG. 1, illustrating the vicinity of the column for producing impure argon,
- FIG. 3 is a view similar to Figure 1, illustrating a second embodiment of an air distillation installation according to the invention and, - Figure 4 is a schematic partial view of another embodiment of an air distillation installation according to the invention
- FIG. 5 is a view similar to FIG. 1, illustrating a third embodiment of an air distillation installation according to the invention and
- 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 deazotation 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 producing pure argon comprises an overhead condenser 13 and a tank vaporizer 14. 6
- 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 with water and C0 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 an intermediate level of the medium pressure column 8.
- the other part of this flow is sub-cooled through a heat exchanger 24, then expanded in a valve 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. 7
- Lean liquid (almost pure nitrogen) LP is taken from the upper part of the medium pressure column 8, then sub-cooled in one 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 and then vaporized in one 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.
- Impure or residual nitrogen NR withdrawn from the top of the low-pressure column 9, is sent to the waste line 33, where this impure nitrogen is heated at the crossing of the heat exchanger 24, then of the line main 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 waste 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, the inlet 49 of which is connected to the pipe 19, between the heat exchanger 20 and the expansion valve 21, and the outlet 50 of which opens into the waste pipe 33, 9
- 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
- the extraction efficiency p of argon at the outlet of column 3 necessary to meet these reduced needs is less than in.
- the extraction yield is maintained at the value po and the excess of argon thus extracted is returned at the outlet of the column 3 for the production of impure argon towards the waste pipe 33 via the waste pipe. bypass 48.
- the flow rate D of medium pressure nitrogen which can be drawn off at the head of the medium pressure column 8 is maintained at the maximum value D (po).
- 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 an argon extraction yield required p at the outlet of column 3 approximately equal to 30%.
- Cases 3A and 3B correspond to the operation of the argon installation 1 for needs in supplying zero argon and therefore corresponding to a necessary argon extraction yield p 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 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 argon produced in excess is in fact used as a refrigerating 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 line 48 can independently pass through the heat exchanger 24 and / or the 12
- the optimal efficiency po may be different from the nominal efficiency pn. This yield po is generally less than pn.
- the extraction efficiency of argon is maintained at the value po for the purposes of supplying argon corresponding to a necessary yield p ⁇ po ⁇ pn.
- the extraction yield po 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 low pressure column 9, and which at least partially crosses the line of heat exchange 5.
- the turbine 501 expands at low pressure, to the pressure drop, air purified by the device 7 and then compressed by an auxiliary compressor 503 coupled to the turbine 501.
- This turbine 501 for blowing air ensures the cold behavior of the installation 1 in place of the turbine 41 of FIG. 1.
- the efficiency po may be the optimal efficiency, for a predetermined quantity of medium-pressure nitrogen gas withdrawn at the head of the medium pressure column 9, vis-à-vis 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 nitrogen NC is drawn off at the head of column 2 then heated 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 po then corresponds substantially at the minimum flow rate of impure nitrogen overhead NC to be used to vaporize the tank oxygen. Maintaining the argon extraction efficiency at po 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.
- 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 to the 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 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 to 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 14
- the frigories of the apparatus 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 it 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.
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/446,356 US6269659B1 (en) | 1998-04-21 | 1999-04-20 | Method and installation for air distillation with production of argon |
JP55257399A JP2002511136A (ja) | 1998-04-21 | 1999-04-20 | アルゴンの製造を伴う空気精留プロセスおよびプラント |
BR9906366-2A BR9906366A (pt) | 1998-04-21 | 1999-04-20 | Processo e unidade de destilação de ar com produção de argÈnio |
AU33368/99A AU743283B2 (en) | 1998-04-21 | 1999-04-20 | Method and installation for air distillation with production of argon |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR98/04972 | 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 |
FR98/16245 | 1998-12-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1999054673A1 true WO1999054673A1 (fr) | 1999-10-28 |
Family
ID=26234280
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR1999/000931 WO1999054673A1 (fr) | 1998-04-21 | 1999-04-20 | Procede et installation de distillation d'air avec production d'argon |
Country Status (6)
Country | Link |
---|---|
US (1) | US6269659B1 (fr) |
EP (1) | EP0952415A1 (fr) |
JP (1) | JP2002511136A (fr) |
AU (1) | AU743283B2 (fr) |
BR (1) | BR9906366A (fr) |
WO (1) | WO1999054673A1 (fr) |
Families Citing this family (13)
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 |
FR2807150B1 (fr) * | 2000-04-04 | 2002-10-18 | Air Liquide | Procede et appareil de production d'un fluide enrichi en oxygene par distillation cryogenique |
WO2003087686A1 (fr) * | 2002-04-12 | 2003-10-23 | Linde Aktiengesellschaft | Procede de production d'argon par separation de l'air a basse temperature |
US7113450B2 (en) * | 2003-05-20 | 2006-09-26 | Timex Group B.V. | Wearable electronic device with multiple display functionality |
US7093649B2 (en) | 2004-02-10 | 2006-08-22 | Peter Dawson | Flat heat exchanger plate and bulk material heat exchanger using the same |
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 |
KR20170070172A (ko) * | 2014-10-16 | 2017-06-21 | 린데 악티엔게젤샤프트 | 저온 분리에 의해 아르곤을 가변적으로 획득하기 위한 방법 및 디바이스 |
EP3048401A1 (fr) | 2015-01-20 | 2016-07-27 | Linde Aktiengesellschaft | Procédé et dispositif destinés à l'extraction variable d'argon par la séparation cryogénique de l'air |
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 |
FR3110685B1 (fr) * | 2020-05-20 | 2022-12-23 | Air Liquide | Procédé et appareil de séparation d’air par distillation cryogénique |
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 |
Citations (4)
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 (fr) * | 1989-02-23 | 1990-08-29 | Linde Aktiengesellschaft | Procédé et dispositif de rectification d'air |
EP0540900A1 (fr) * | 1991-10-10 | 1993-05-12 | Praxair Technology, Inc. | Système de rectification cryogénique pour la production d'oxygène ultra-pure |
Family Cites Families (3)
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 |
-
1999
- 1999-04-20 EP EP99400957A patent/EP0952415A1/fr not_active Withdrawn
- 1999-04-20 WO PCT/FR1999/000931 patent/WO1999054673A1/fr active IP Right Grant
- 1999-04-20 US US09/446,356 patent/US6269659B1/en not_active Expired - Fee Related
- 1999-04-20 AU AU33368/99A patent/AU743283B2/en not_active Ceased
- 1999-04-20 JP JP55257399A patent/JP2002511136A/ja active Pending
- 1999-04-20 BR BR9906366-2A patent/BR9906366A/pt not_active IP Right Cessation
Patent Citations (4)
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 (fr) * | 1989-02-23 | 1990-08-29 | Linde Aktiengesellschaft | Procédé et dispositif de rectification d'air |
EP0540900A1 (fr) * | 1991-10-10 | 1993-05-12 | Praxair Technology, Inc. | Système de rectification cryogénique pour la production d'oxygène ultra-pure |
Also Published As
Publication number | Publication date |
---|---|
US6269659B1 (en) | 2001-08-07 |
BR9906366A (pt) | 2000-09-19 |
AU743283B2 (en) | 2002-01-24 |
JP2002511136A (ja) | 2002-04-09 |
AU3336899A (en) | 1999-11-08 |
EP0952415A1 (fr) | 1999-10-27 |
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