EP1495274A1 - Procede de production d'argon par separation de l'air a basse temperature - Google Patents

Procede de production d'argon par separation de l'air a basse temperature

Info

Publication number
EP1495274A1
EP1495274A1 EP03722379A EP03722379A EP1495274A1 EP 1495274 A1 EP1495274 A1 EP 1495274A1 EP 03722379 A EP03722379 A EP 03722379A EP 03722379 A EP03722379 A EP 03722379A EP 1495274 A1 EP1495274 A1 EP 1495274A1
Authority
EP
European Patent Office
Prior art keywords
column
argon
rectification
sections
section
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Withdrawn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
EP03722379A
Other languages
German (de)
English (en)
Inventor
Reinhard Glatthaar
Christian Kunz
Harald Ranke
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 DE2002116269 external-priority patent/DE10216269A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP03722379A priority Critical patent/EP1495274A1/fr
Publication of EP1495274A1 publication Critical patent/EP1495274A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
    • F25J3/04933—Partitioning walls or sheets
    • F25J3/04939—Vertical, e.g. dividing wall columns
    • 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
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods
    • 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
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the invention relates to a method for the production of argon by low-temperature separation of air in a rectification system which has three rectification sections arranged in series, the first and second and the second and third rectification sections being connected to one another on the gas and liquid side, and the second rectifying section has two sections, which are not connected to one another on the gas and liquid side and are flowed through in parallel, a fluid containing oxygen and argon being introduced into the first of the two sections and a stream containing oxygen and argon being withdrawn from the second of the two sections.
  • the boiling point of argon is between the boiling points of oxygen and nitrogen.
  • the argon accumulates in a central area of the low-pressure column.
  • a gaseous fraction which essentially consists of oxygen and argon, is usually removed from this area.
  • This fraction enriched with about 10% argon, is fed to the so-called crude argon column, in which a rectification separation of oxygen and argon is carried out.
  • Argon can be drawn off at the top of the crude argon column and an essentially oxygen-containing liquid collects in its sump, which is then returned to the low-pressure column.
  • the two sections are connected on the flow side.
  • a three-component mixture introduced into the section on one side of the dividing wall can be broken down into three fractions in a single column.
  • the component with the lowest boiling point can be at the top of the dividing wall column, the medium boiler on the side of the dividing wall opposite the feed and the high-boiling component
  • Component can be obtained from the swamp. In comparison to a column without a dividing wall, higher concentrations of the medium boiler can be achieved with the dividing wall column at the side draw.
  • EP 0638778 B1 describes a process for the low-temperature separation of air in a dividing wall column.
  • the low pressure column is divided in a central area by a partition.
  • Sump liquid is fed from the pressure column on one side of the partition, while the argon-containing fluid is drawn off on the other side of the partition.
  • a waste fluid is removed on the side of the partition wall on which the bottom liquid is introduced.
  • the process parameters are selected so that the argon-containing fluid obtained has an argon concentration of at least 70%.
  • the object of the present invention is therefore to demonstrate an improved process for the production of argon by low-temperature air separation.
  • the argon concentration in the stream taken from the second section being between 15% and 50%, preferably between 15% and 40%, particularly preferably between 20% and 35%.
  • the invention is based on the knowledge that, given the quantity and purity of the argon product, an increase in the initial concentration of argon in the stream introduced into the crude argon column leads to a reduction in the quantity of steam to be transferred. This is positive in that the cross-section of the crude argon column can be reduced accordingly and costs can be saved.
  • the rectification system has at least one air separation column, which has three rectification sections arranged in series, each of which adjoining rectification sections are connected to one another on the gas and liquid side.
  • the middle rectification section has a dividing wall which divides the rectification section into two sections. Within the second rectification section, gas and liquid exchange between the two sections is prevented by the partition. However, both sections are connected on the flow side to the rectification section above and below.
  • the division into two sections through which the flow is parallel can also be carried out by means of two columns arranged parallel to one another. Liquid is drawn off from a first air separation column at an intermediate point and fed to a second column. Gas is led out of the first air separation column at a second intermediate point and introduced into the second column. Gas and liquid formed at the top of the second column from the bottom of the second column are returned to the first air separation column, preferably at the two intermediate points.
  • the two sections separated on the flow side are not realized by a partition, but by two columns connected in parallel.
  • the current withdrawn from the second section is preferably conducted into a crude argon column.
  • the sump liquid obtained there, which essentially contains oxygen, is preferably in the second subsection returned, that is, in the section from which the argon-containing fraction is also removed.
  • the invention is preferably suitable for a rectification system which has a pressure column and a low-pressure column, the dividing wall being arranged in the low-pressure column, and an oxygen-enriched fluid, preferably bottom liquid, being introduced from the pressure column into the first section.
  • the advantages of the process according to the invention are particularly evident when argon with a high purity of more than 95%, preferably more than 98% and / or argon with an oxygen content of less than 100 ppm, preferably less than 10 ppm, is obtained in the crude argon column shall be.
  • the invention is particularly advantageous when more than 100 theoretical trays, preferably between 150 and 200 theoretical trays, are used in the raw argon column. In these cases, the height of the raw argon column is determined by the number of theoretical plates required for the high final purity.
  • the diameter of the crude argon column can, however, be significantly reduced compared to conventional processes without a dividing wall column.
  • Packings for rectification are preferably used in the air separation column. It is advantageous here if the packs are arranged in a plurality of areas, so-called beds, one above the other, the liquid to be rectified and / or the gas to be rectified being collected between two beds and redistributed to the next pack bed. Are other internals or devices for rectification in the air separation column.
  • Air separation column used it has also proven to be useful to provide collectors and / or distributors in the air separation column at certain intervals, so as to counteract distribution in the column.
  • the partition between the two divided areas in the air separation column preferably ends at the upper or lower end of a packing bed, or when using other column internals at the upper or lower end of the corresponding area, which is separated from the adjacent area by a collector / distributor. Since collectors / distributors are already arranged at these joints between two pillar areas, the partition must be used no additional collectors / distributors are provided. Only the collector / distributor located directly above the partition wall has to be converted in such a way that it distributes the liquid in the desired manner over the two sections separated from one another by the partition wall. The same applies if, instead of a dividing wall column, a second column arranged parallel to the first air separation column is used.
  • mass transfer elements are preferably used, which bring about the same pressure drop for the rising gas.
  • FIG. 1 shows a device for carrying out the method according to the invention
  • FIG. 2 shows another embodiment according to the invention
  • FIG. 3 shows the specific amount of steam to be fed to the crude argon column as a function of its argon concentration
  • Figure 4 shows the argon yield as a function of the argon concentration in the vapor supplied to the crude argon column.
  • FIG. 1 shows the rectification part of a low-temperature air separation plant with argon extraction.
  • feed air 1 is introduced into the pressure column 2.
  • the oxygen-enriched liquid accumulating in the sump of the pressure column 2 is transferred via line 3 into the low pressure column 4.
  • the low pressure column 4 is designed as a dividing wall column. 4 packs are provided as rectification elements in the low-pressure column, which are arranged in a plurality of beds 19, 20, 21, 22 lying one above the other, each having a height of approximately 6 m.
  • Collectors / distributors 23, 24, 25, 26, 27 are provided between each two beds for collecting and distributing the liquid flowing downward in the low-pressure column 4.
  • a partition 5 is arranged such that the low-pressure column 4 is divided into two sections 6, 7.
  • the partition 5 extends over the entire length of the two middle
  • the low-pressure column 4 is fed into the divided subsection 6 via line 3 sump liquid from the pressure column 2. Turbine air can also be introduced into the low-pressure column 4 via line 12. At the top of the low-pressure column 4, gaseous product nitrogen can be obtained via line 8. Furthermore, a deduction 9 for impure nitrogen is provided above the divided sections 6, 7. Gaseous or liquid product oxygen can be removed from the sump of the low-pressure column 4 via the lines 10 and 11.
  • Liquid is distributed to the two sections 6, 7 by means of distributors 24, 25.
  • the same amount of liquid is preferably applied to both sections 6, 7.
  • it can make sense to provide different liquid throughputs in sections 6 and 7.
  • the distribution of the rising steam over the two sections 6, 7 is advantageous as a function of the counter-flowing amounts of liquid and the pressure losses in the packing beds 20, 21.
  • a stream 13 essentially containing argon and oxygen with an argon concentration of 35% is drawn off from the section 7 and introduced into a crude argon column 14 provided with packings.
  • the oxygen-argon mixture is rectified in the crude argon column 14.
  • the argon formed is condensed in a top condenser 15 and in part obtained as product 16 with a residual oxygen content of less than 10 ppm, and in part 17 is returned to the crude argon column 14 as reflux liquid.
  • Liquid oxygen collects in the sump of the crude argon column 14 and is returned via line 18 to the divided section 7 of the low-pressure column 4.
  • Partition 5 a parallel side column 30 is provided.
  • the same elements are provided with the same reference numbers in both figures.
  • the low-pressure column 4 is designed in this case without a partition.
  • the liquid flowing down from the rectification section 22 is distributed on the one hand by means of the distributor 24 to the beds 20, 21 which form the first section.
  • the second section is implemented by the side column 30.
  • a portion of the liquid flowing down from the packing bed 22 is drawn off from the low-pressure column 4 via line 31 and fed to the side column 30 at the top. Gas formed at the top of the side column 30 is via line 32 above the
  • the specific i.e. determines the amount of steam based on the amount of argon product as a function of the argon concentration of the steam.
  • the determined dependency is shown in FIG. 3.
  • the solid curve shows the theoretical minimum amount of steam with an infinite theoretical number of trays.
  • the dashed curve shows the course of the states calculated for a theoretical number of plates of 50. Both curves have essentially the same course. However, it can be seen from the curve for a finite number of trays that in this case approximately 30 to 40% larger amounts of steam have to be used compared to the theoretical curve.
  • the number of theoretical plates in the crude argon column 14 cannot be significantly reduced by increasing the argon concentration in the steam 13 to be supplied at a desired product purity of 98.5%, since the number of plates is not due to the final concentration to be achieved at high product purities is determined by the initial concentration.
  • the low-pressure column 4 is operated according to the invention in such a way that an argon concentration of 45% is achieved in the side draw 13. At this concentration, the amount of steam introduced into the raw argon column 14 can be minimized and the diameter of the raw argon column 14 can be reduced in accordance with the amount of steam.
  • FIG. 4 shows the argon yield as a function of the argon concentration of the vapor fed into the argon column.
  • the solid curve shows the calculated values for a short partition, the dashed curve for a long partition.
  • the number of trays in the low pressure column was kept constant.
  • the solid curve shows that the argon yield remains essentially constant in a range between 10 and 25% argon concentration in the supplied steam.
  • the curve breaks off at 25% because no higher argon concentrations can be achieved with the assumed partition wall length.
  • an essentially constant argon yield can also be found in the range of higher argon concentrations above 30% to 90%. Accordingly, increasing the argon concentration does not have a negative effect on the yield.

Landscapes

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

Abstract

L'invention concerne un procédé permettant de produire de l'argon par séparation de l'air à basse température. Le système de rectification (2, 4) présente au moins une colonne de séparation de l'air (4) qui comporte une cloison de séparation (5) s'étendant dans le sens longitudinal de la colonne. La colonne de séparation de l'air (4) se trouve ainsi subdivisée à la hauteur de la cloison de séparation (5), en une première et en une seconde section partielle (6, 7). Un fluide (3) contenant de l'oxygène et de l'argon est introduit dans la première section partielle (6). Un courant (13) contenant de l'oxygène et de l'argon et dont la concentration en argon est comprise entre 15 et 30 % est prélevé de la seconde section partielle.
EP03722379A 2002-04-12 2003-04-01 Procede de production d'argon par separation de l'air a basse temperature Withdrawn EP1495274A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP03722379A EP1495274A1 (fr) 2002-04-12 2003-04-01 Procede de production d'argon par separation de l'air a basse temperature

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
DE10216269 2002-04-12
DE2002116269 DE10216269A1 (de) 2002-04-12 2002-04-12 Verfahren zur Gewinnung von Argon durch Tieftemperaturluftzerlegung
EP02011058 2002-05-17
EP02011058 2002-05-17
PCT/EP2003/003395 WO2003087686A1 (fr) 2002-04-12 2003-04-01 Procede de production d'argon par separation de l'air a basse temperature
EP03722379A EP1495274A1 (fr) 2002-04-12 2003-04-01 Procede de production d'argon par separation de l'air a basse temperature

Publications (1)

Publication Number Publication Date
EP1495274A1 true EP1495274A1 (fr) 2005-01-12

Family

ID=29251755

Family Applications (1)

Application Number Title Priority Date Filing Date
EP03722379A Withdrawn EP1495274A1 (fr) 2002-04-12 2003-04-01 Procede de production d'argon par separation de l'air a basse temperature

Country Status (9)

Country Link
US (1) US20060005574A1 (fr)
EP (1) EP1495274A1 (fr)
JP (1) JP2005527767A (fr)
KR (1) KR20040101453A (fr)
CN (1) CN1646869A (fr)
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JP6204231B2 (ja) * 2014-03-11 2017-09-27 大陽日酸株式会社 空気液化分離装置及び方法
PL3133361T3 (pl) * 2015-08-20 2018-11-30 Linde Aktiengesellschaft System kolumn destylacyjnych i urządzenie do wytwarzania tlenu przez niskotemperaturowy rozkład powietrza
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US20060005574A1 (en) 2006-01-12
WO2003087686A1 (fr) 2003-10-23
CA2502706A1 (fr) 2003-10-23
RU2303211C2 (ru) 2007-07-20
CN1646869A (zh) 2005-07-27
AU2003229590A1 (en) 2003-10-27
RU2004133324A (ru) 2006-01-27
KR20040101453A (ko) 2004-12-02
JP2005527767A (ja) 2005-09-15

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