EP0567360B1 - Verfahren und Apparat zum Überführen einer Flüssigkeit - Google Patents

Verfahren und Apparat zum Überführen einer Flüssigkeit Download PDF

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Publication number
EP0567360B1
EP0567360B1 EP19930400745 EP93400745A EP0567360B1 EP 0567360 B1 EP0567360 B1 EP 0567360B1 EP 19930400745 EP19930400745 EP 19930400745 EP 93400745 A EP93400745 A EP 93400745A EP 0567360 B1 EP0567360 B1 EP 0567360B1
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EP
European Patent Office
Prior art keywords
column
pressure
liquid
point
expansion valve
Prior art date
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Expired - Lifetime
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EP19930400745
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English (en)
French (fr)
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EP0567360B2 (de
EP0567360A1 (de
Inventor
Bernard Darredeau
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • 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
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C6/00—Methods and apparatus for filling vessels not under pressure with liquefied or solidified gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2270/00—Applications
    • F17C2270/05—Applications for industrial use
    • F17C2270/0509—"Dewar" vessels
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/06—Lifting of liquids by gas lift, e.g. "Mammutpumpe"
    • 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
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • 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
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the present invention relates to a method for transferring a liquid, via a riser fitted with an expansion valve, from a first distillation column operating at a first pressure, typically relatively high, to equipment, in particular to a second distillation column, operating at a second pressure, typically relatively low, lower than the first pressure.
  • Apparatuses for the separation of gases from air by cryogenic distillation most often use the conventional double column scheme.
  • the liquids produced in the tank oxygen-rich liquid
  • in the intermediate part lean liquid
  • liquid nitrogen liquid nitrogen
  • the medium pressure column or MP column
  • the low pressure column is placed above the medium pressure column. Liquids must therefore be sent to a point higher than the point where they are taken.
  • the pressure difference between the medium pressure column and the low pressure column is greater than the hydrostatic pressure of the liquid column between the sampling point in the MP column and the arrival point of the LP column.
  • the invention aims to allow, in a simple and effective manner, a safe transfer of liquids, without the use of a pump.
  • the process according to the invention is characterized in that a lightening gas available at a pressure higher than the pressure created by a column of said liquid is injected into the riser, downstream of the expansion valve. between the point of injection of the gas and the point of introduction of the liquid into said equipment.
  • the subject of the invention is a process for transferring a liquid, via a rising pipe fitted with an expansion valve, from a first distillation column operating at a first pressure to equipment, in particular a second distillation column, operating at a second pressure, lower than the first pressure, characterized in that the liquid is sub-cooled before its expansion, with the exception of a minority fraction of this liquid, so as to produce a controlled quantity of flash gas, this flash gas is injected downstream or upstream of the expansion valve and serves as liquid lightening gas.
  • the invention also relates to a distillation installation intended for the implementation of such a process.
  • this installation of the type comprising a first distillation column operating at a first pressure, equipment, in particular a second distillation column, operating at a second pressure, lower than the first pressure, and a riser pipe equipped with '' an expansion valve and connecting a point of withdrawal of liquid from the first column to a point of introduction of liquid into said equipment, is characterized in that it comprises means for injecting into the riser, downstream of the expansion valve, a lightening gas available at a pressure higher than the pressure created by a column of said liquid between the point of injection of the gas and the point of introduction of the liquid into said equipment.
  • the installation according to the invention of the type comprising a first distillation column operating at a relatively high pressure, equipment, in particular a second distillation column, operating at a relatively low pressure, and a riser fitted an expansion valve and connecting a point of withdrawal of liquid from the first column to a point of introduction of liquid from said equipment, is characterized in that the riser pipe passes through a sub-cooler upstream of the expansion valve and is provided with a bypass of this subcooler.
  • the air distillation installation represented in FIG. 1 essentially comprises a double distillation column 1.
  • This comprises a medium pressure column 2 surmounted by a low pressure column 3.
  • a vaporizer-condenser 4 puts in relation to heat exchange the top vapor of column 2, consisting of practically pure nitrogen, and the bottom liquid of column 3, consisting of oxygen at a determined purity.
  • FIG. 1 also shows pipes 15 for the production of gaseous oxygen leaving the tank of column 3, 16 for the production of pure nitrogen, starting from the top of this column 3, 17 for blowing air in. an intermediate point in column 3, and 18 for discharging residual gas (impure nitrogen) from the upper part of this column.
  • an air line 19 is pricked on the supply line 5 and is divided into two branches 20, 21.
  • Each of these branches is equipped with an expansion valve 22, 23 and joins the lines 6 and 9 respectively just downstream of their expansion valves 7 and 10.
  • a gas line 24 equipped with an expansion valve 25 starts from the top of column 2 and joins line 12 just downstream of the expansion valve 13.
  • Another gas line 26, equipped with an expansion valve (not shown) starts from a location in the column 2 next to the point of withdrawal of the lean liquid (line 11) and joins this line 11 just downstream of the expansion valve thereof.
  • the air bubbles lighten the rich liquid and reduce the pressure necessary to make it rise up to column 2.
  • a low air flow conveyed by the pipe 19, 21 is expanded in the expansion valve 23 and injected into the rich liquid which has just been expanded in the expansion valve 10.
  • the air flow total deflected by line 19 is low, typically less than 1% of the air flow entering the installation.
  • the corresponding lightening gas in line 24 must be practically pure nitrogen.
  • the compositions of the rich liquid and of the lean liquid are not critical, so that the corresponding lightening gases may have compositions slightly different from these liquids, provided that they do not pollute them, all the more that the flow rate of these gases is very low.
  • the main expansion valves 7, 10 and 13 are placed as low as possible to guarantee their supply with clean liquid, and gas bubbles are introduced just downstream of these expansion valves to assist propulsion towards the top of the liquids in question. More precisely, the pressure of the lightening gases must be sufficient to overcome the height of liquid which overcomes the point of injection of the gas, and this pressure is obtained, in the example shown, thanks to the fact that each gas, which is available at the pressure of column 3, is injected above the point of withdrawal of the associated liquid.
  • FIGS 2 and 3 illustrate, in the case of the rise of liquid nitrogen via line 12, two variants for obtaining the lightening gas. In these two variants, the pipe 24 and the expansion valve 25 are eliminated.
  • a controlled minority flow of liquid nitrogen conveyed by the pipe 12 by-passes the sub-cooler 14 via a by-pass pipe 24A equipped, preferably at its lowest point, with an expansion valve 25A and terminating downstream of the expansion valve 13.
  • the liquid thus derived, not being sub-cooled, produces by expansion, a relatively large and adjustable quantity of flash gas, which serves as lightening gas.
  • the expansion valve 25A is omitted, and there is provided, in line 12, a three-way valve 27 having an inlet connected to line 12 upstream of the subcooler 14, an outlet connected at the inlet of this subcooler and another outlet connected to the 24A bypass line.
  • this pipe 24A ends upstream of the expansion valve 13.
  • FIGS. 2 and 3 although based on the same idea as that of FIG. 1, are less effective in the sense that they make it possible to lighten the rising liquids while limiting the production of gases to a minimum. of flash, which is unfavorable to distillation, but that they do not allow the restarting of the installation in the event of accidental blockage of the risers.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Gas Separation By Absorption (AREA)

Claims (10)

  1. Verfahren zum Überführen einer Flüssigkeit über eine mit einem Druckminderventil (7, 10, 13) ausgestattete Steigleitung (6, 9, 11, 12) von einer ersten Destillationskolonne (2), die bei einem ersten Druck arbeitet, zu einer Einrichtung (3), insbesondere einer zweiten Destillationskolonne, die bei einem tieferen Druck als dem ersten Druck arbeitet, dadurch gekennzeichnet, daß man in die Steigleitung stromauf von dem Druckminderventil ein Verdünnungsgas einleitet, das bei einem Druck vorliegt, der höher ist als der von einer Flüssigkeitskolonne zwischen dem Einleitungspunkt des Gases und dem Einführungspunkt der Flüssigkeit in die Einrichtung (3) erzeugte Druck.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Verdichtungsgas bei dem Druck der ersten Destillationskolonne (2) vorliegt und in die Flüssigkeit in der Steigleitung oberhalb des Entnahmepunktes der Flüssigkeit eingeleitet wird.
  3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß man als Verdünnungsgas ein an einem Punkt der ersten Kolonne entnommenes Gas verwendet, das derart ausgewählt wird, daß die Zusammensetzung der überführten Flüssigkeit nicht wesentlich verändert wird.
  4. verfahren nach Anspruch 2 zum Überführen der Wannenflüssigkeit von einer Mitteldruck-Kolonne (2) einer doppelten Luftdestillationskolonne (1) zu einem Zwischenpunkt einer Niederdruck-Kolonne (3), welche über die Mitteldruck-Kolonne hinausragt, und/oder zu dem Kopfkondensator einer mit der Niederdruck-Kolonne (3) verbundenen Sauerstoff/Argon-Tremkolonne, dadurch gekennzeichnet, daß man als Verdünnungsgas einen geringen Durchfluß an Zufuhrluft der doppelten Kolonne (1) verwendet.
  5. Verfahren zum Überführen einer Flüssigkeit über eine mit einem Druckminderventil (7, 10, 13) ausgestattete Steigleitung (6, 9, 11, 12) von einer ersten Destillationskolonne (2), die bei einem ersten Druck arbeitet, zu einer Einrichtung (3), insbesondere einer zweiten Destillationskolonne, die bei einem zweiten tieferen Druck als dem ersten Druck arbeitet, dadurch gekennzeichnet, daß man die Flüssigkeit vor ihrer Entspannung mit Ausnahme eines kleinen Bruchteils der Flüssigkeit derart unterkühlt, daß eine kontrollierte Menge an Flash-Gas erzeugt wird, wobei das Flash-Gas stromab oder stromauf von dem Druckminderventil (7, 10, 13) eingeleitet wird und als Verdünnungsgas der Flüssigkeit dient.
  6. Destillationsanlage mit einer ersten Destillationskolonne (2), die bei einem ersten Druck arbeitet, einer Einrichtung (3), insbesondere einer zweiten Destillationskolonne, die bei einem zweiten tieferen als dem ersten Druck arbeitet und einer mit einem Druckminderventil (7, 10, 13) ausgestatteten Steigleitung (6, 9, 11, 12), die einen Entnahmepunkt der Flüssigkeit der ersten Kolonne (2) mit einem Einführungspunkt der Flüssigkeit in die Einrichtung (3) verbindet, der sich oberhalb des Entnahmepunktes befindet dadurch gekennzeichnet, daß sie stromab von dem Druckminderventil in der Steigleitung eine Einrichtung (19 bis 26) zum Einleiten eines Verdünnungsgases aufweist, das bei einem Druck vorliegt, der höher ist als der von einer Flüssigkeitskolonne zwischen dem Einleitungspunkt des Gases und dem Einführungspunkt der Flüssigkeit in die Einrichtung (3) erzeugte Druck.
  7. Anlage nach Anspruch 6, dadurch gekennzeichnet, daß das Verdünnungsgas in der ersten Kolonne (2) oder an deren Eingang abgezweigt wird und daß die Einleit-Einrichtung (19 bis 26) in die Steigleitung (6, 9, 11, 12) in einer Höhe oberhalb des Ausgangspunktes der Leitung mündet.
  8. Anlage nach Anspruch 7, dadurch gekennzeichnet, daß die Einleit-Einrichtung eine mit einem Druckminderventil (25) ausgestattete Gasleitung (11, 24) aufweist, die von einem zu dem Entnahmepunkt der Flüssigkeit benachbarten Punkt der ersten Kolonne (2) aus verläuft.
  9. Anlage nach Anspruch 7, bei welcher die erste Kolonne (2) die Mitteldruck-Kolonne (2) einer doppelten Luftdestillationskolonne (1) ist und die Einrichtung (3) die Niederdruck-Kolonne (3) ist, die über die Mitteldruck-Kolonne der doppelten Kolonne und/oder den Kopfkondensator einer mit der Niederdruck-Kolonne (3) verbundenen Sauerstoff/Argon-Trennkolonne hinausragt, dadurch gekennzeichnet, daß die Einleit-Einrichtung eine mit einem Druckminderventil (22, 23) ausgestattete Leitung (19 bis 21) aufweist, die von der Ankunftsleitung (5) der zu destillierenden Luft oder von der Wanne der Mitteldruck-Kolonne (2) aus verläuft.
  10. Destillationsanlage mit einer ersten Destillationskolonne (2), die bei einem relativ hohen Druck arbeitet, einer Einrichtung (3), insbesondere einer zweiten Destillationskolonne, die bei einem relativ tiefen Druck arbeitet, und einer mit einem Druckminderventil (7, 10, 13) ausgestatteten Steigleitung (6, 9, 11, 12), die einen Entnahmepunkt der Flüssigkeit der ersten Kolonne (2) mit einem Einführungspunkt der Flüssigkeit in die Einrichtung (3) verbindet, dadurch gekennzeichnet, daß die Steigleitung (6, 12) eine Unterkühl-Einrichtung (8, 14) stromauf von dem Druckminderventil (7, 13) durchläuft und eine Umgehungsleitung (24A) der Unterkühl-Einrichtung hat.
EP19930400745 1992-03-24 1993-03-23 Verfahren und Apparat zum Überführen einer Flüssigkeit Expired - Lifetime EP0567360B2 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9203500 1992-03-24
FR9203500A FR2689223B1 (fr) 1992-03-24 1992-03-24 Procede et installation de transfert de fluide en provenance d'une colonne de distillation, notamment d'air.

Publications (3)

Publication Number Publication Date
EP0567360A1 EP0567360A1 (de) 1993-10-27
EP0567360B1 true EP0567360B1 (de) 1996-05-15
EP0567360B2 EP0567360B2 (de) 2002-06-12

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EP19930400745 Expired - Lifetime EP0567360B2 (de) 1992-03-24 1993-03-23 Verfahren und Apparat zum Überführen einer Flüssigkeit

Country Status (8)

Country Link
US (1) US5337569A (de)
EP (1) EP0567360B2 (de)
JP (1) JPH0618162A (de)
CN (1) CN1078946C (de)
CA (1) CA2092139C (de)
DE (1) DE69302619T2 (de)
ES (1) ES2086895T5 (de)
FR (1) FR2689223B1 (de)

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Publication number Priority date Publication date Assignee Title
FR2753638B1 (fr) * 1996-09-25 1998-10-30 Procede pour l'alimentation d'une unite consommatrice d'un gaz
GB9705889D0 (en) * 1997-03-21 1997-05-07 Boc Group Plc Heat exchange method and apparatus
CN1073883C (zh) * 1998-05-15 2001-10-31 中国石油化工总公司 一种采用管壁补气与排气实现循环流化床多段化操作的方法及其装置
DE19921949A1 (de) * 1999-05-12 2000-11-16 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE19933558C5 (de) * 1999-07-16 2010-04-15 Linde Ag Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
EP1338856A3 (de) * 2002-01-31 2003-09-10 L'AIR LIQUIDE, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Verfahren und Vorrichtung zur Zerlegung von Luft durch Tieftemperaturdestillation
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Also Published As

Publication number Publication date
FR2689223A1 (fr) 1993-10-01
EP0567360B2 (de) 2002-06-12
DE69302619D1 (de) 1996-06-20
CA2092139C (fr) 2004-05-04
FR2689223B1 (fr) 1994-05-06
EP0567360A1 (de) 1993-10-27
CN1078946C (zh) 2002-02-06
ES2086895T5 (es) 2002-12-16
CA2092139A1 (fr) 1993-09-25
JPH0618162A (ja) 1994-01-25
US5337569A (en) 1994-08-16
ES2086895T3 (es) 1996-07-01
CN1076775A (zh) 1993-09-29
DE69302619T2 (de) 1996-09-26

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