EP1316768A1 - Procédé et dispositif pour la production d'un liquide ultra pur à partir d'une charge cryogénique en liquide moins pur - Google Patents

Procédé et dispositif pour la production d'un liquide ultra pur à partir d'une charge cryogénique en liquide moins pur Download PDF

Info

Publication number
EP1316768A1
EP1316768A1 EP02024690A EP02024690A EP1316768A1 EP 1316768 A1 EP1316768 A1 EP 1316768A1 EP 02024690 A EP02024690 A EP 02024690A EP 02024690 A EP02024690 A EP 02024690A EP 1316768 A1 EP1316768 A1 EP 1316768A1
Authority
EP
European Patent Office
Prior art keywords
liquid
separation column
storage tank
evaporator
fraction
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Withdrawn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
EP02024690A
Other languages
German (de)
English (en)
Inventor
Gunther Hauck
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
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP1316768A1 publication Critical patent/EP1316768A1/fr
Withdrawn legal-status Critical Current

Links

Images

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
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • F25J2215/44—Ultra high purity nitrogen, i.e. generally less than 1 ppb impurities
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/44—Separating high boiling, i.e. less volatile components from nitrogen, e.g. CO, Ar, O2, hydrocarbons
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a method for producing a high-purity cryogenic Liquid product from a less pure cryogenic feed liquid, in which a first stream of less pure cryogenic feed liquid from a storage tank into a first separation column is introduced, a second stream less pure cryogenic
  • the feed liquid evaporates from the storage tank in a pressure build-up evaporator and returned to the storage tank, a gaseous fraction from the top Area of the first separation column liquefied in a condenser-evaporator and at from which a highly pure liquid product is obtained.
  • Such a system can be used, for example, to produce high-purity nitrogen be used. It can be obtained more cheaply at the location of the consumer less pure nitrogen can be transported in liquid form; from this less pure cryogenic liquid becomes the required with a relatively uncomplicated apparatus highly pure product made.
  • the procedure is also based on other substances applicable and can for example for the production of high purity oxygen or high pure argon can be used.
  • the invention has for its object such a method and / or specify appropriate device that are particularly simple in terms of equipment.
  • This object is achieved in that a gaseous fraction from the Storage tank is removed and fed to the first separation column.
  • compressed gas e.g. from a pipeline system
  • this can be introduced into the storage tank.
  • a liquid fraction from the bottom of the first Separation column removed and used to cool the condenser-evaporator. This eliminates the need for external cooling to cool the first separation column. If the process is designed as a one-column process, the liquid fraction be introduced directly into the evaporation chamber of the condenser-evaporator. Alternatively, intermediate steps are possible, even those that have the composition change the liquid fraction.
  • the method can also be designed as a two-pillar process by the liquid fraction is introduced into a second separation column and the condenser-evaporator is designed as a reboiler of the second separation column, for example as Bottom reboiler. Since the concentration difference between the head of the first and Sump of the second separation column is relatively low, the operating pressure of the first one Separation column to be only slightly higher than that of the second separation column. As a result, a higher yield is high with the same amount of energy being used pure product possible. This can, for example, also be gaseous from the second Separation column are withdrawn.
  • the combination of the two separation columns and the condenser-evaporator is preferably a classic double column educated.
  • no compressors or pumps are used in the process.
  • no fluid is compressed by a machine to heat or cold for the operation of the separation column (s).
  • a refrigeration cycle intended.
  • the invention also relates to a device according to claim 7.
  • a storage tank 1 stored, the less pure cryogenic feed liquid in the embodiment forms.
  • the tank 1 can, for example, by means of tank vehicles or a pipeline be filled (not shown).
  • Liquid 2 ("second stream of less pure cryogenic Feed liquid ") from the tank is evaporated in a pressure build-up evaporator 3, which is heated with water or air, for example.
  • the resulting one Gaseous nitrogen 4 is introduced into the gas space of the storage tank 1. He flows through heat exchanger tubes 5 and thereby enters indirect heat exchange with the liquid stored in the tank. In this way the pressure level in the Storage tank 1 kept at 5 to 12 bar without the need for external energy would be necessary.
  • the medium for heating the pressure build-up evaporator is in generally available free of charge or at negligible costs.
  • the first Separation column 7 is in the example part of a double column system, which is also a second separation column 8 and a condenser-evaporator 9. Besides, will Steam 10 from the storage tank 1 as a gaseous feed fraction in the first Separation column 7 fed.
  • Top gas 11 of the first separation column 7 is liquefied in the condenser-evaporator 9.
  • Condensate 12 obtained in this way becomes a first part 13 as a return to the first separation column 7 abandoned.
  • a second part 14 is called a high purity liquid product removed and fed to a pure nitrogen tank 15.
  • the rest 16 serves as a return for the second separation column 8.
  • Impure liquid 17 from the bottom of the first separation column 7 is a liquid fraction of the second separation column 8 at an intermediate point fed.
  • a residual liquid 18 is drawn off from the bottom of the second separation column 8.
  • Liquid 20 from the pure nitrogen tank 15 can be vaporized (21) and via line 22 can also be sent to a consumer.
  • Figure 2 differs from Figure 1 in that a compressed gas stream from a external source, for example from a pipeline network for nitrogen technical Purity that is introduced into the system.
  • a compressed gas stream from a external source for example from a pipeline network for nitrogen technical Purity that is introduced into the system.
  • the compressed gas flow 24 in one Heat exchanger 25 cooled and introduced via line 26 into the storage tank 1, in the example together with the steam 4 from the pressure build-up evaporator 3.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP02024690A 2001-11-28 2002-11-05 Procédé et dispositif pour la production d'un liquide ultra pur à partir d'une charge cryogénique en liquide moins pur Withdrawn EP1316768A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10158330 2001-11-28
DE10158330A DE10158330A1 (de) 2001-11-28 2001-11-28 Verfahren und Vorrichtung zur Herstellung eines hoch reinen tiefkalten Flüssigprodukts aus einer weniger reinen tiefkalten Einsatzflüssigkeit

Publications (1)

Publication Number Publication Date
EP1316768A1 true EP1316768A1 (fr) 2003-06-04

Family

ID=7707236

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02024690A Withdrawn EP1316768A1 (fr) 2001-11-28 2002-11-05 Procédé et dispositif pour la production d'un liquide ultra pur à partir d'une charge cryogénique en liquide moins pur

Country Status (2)

Country Link
EP (1) EP1316768A1 (fr)
DE (1) DE10158330A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3084736B1 (fr) * 2018-08-01 2022-04-15 Air Liquide Procede et appareil de production d'argon par distillation cryogenique de l'air

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH02183789A (ja) * 1989-01-06 1990-07-18 Hitachi Ltd 超高純度窒素の製造方法及び装置
JPH0486474A (ja) * 1990-07-31 1992-03-19 Nippon Sanso Kk 窒素の精製方法及び装置
JPH04208385A (ja) * 1990-11-30 1992-07-30 Daido Sanso Kk 超高純度窒素製造装置
JPH0719723A (ja) * 1993-06-22 1995-01-20 Teisan Kk 高純度窒素ガス製造装置
US5421164A (en) * 1992-10-09 1995-06-06 Brugerolle; Jean-Renaud Process and installation for the production of ultra-pure nitrogen under pressure
EP0756144A2 (fr) * 1995-07-26 1997-01-29 Teisan Kabushiki Kaisha Générateur de gaz pour la production d'azote de haute pureté

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH02183789A (ja) * 1989-01-06 1990-07-18 Hitachi Ltd 超高純度窒素の製造方法及び装置
JPH0486474A (ja) * 1990-07-31 1992-03-19 Nippon Sanso Kk 窒素の精製方法及び装置
JPH04208385A (ja) * 1990-11-30 1992-07-30 Daido Sanso Kk 超高純度窒素製造装置
US5421164A (en) * 1992-10-09 1995-06-06 Brugerolle; Jean-Renaud Process and installation for the production of ultra-pure nitrogen under pressure
JPH0719723A (ja) * 1993-06-22 1995-01-20 Teisan Kk 高純度窒素ガス製造装置
EP0756144A2 (fr) * 1995-07-26 1997-01-29 Teisan Kabushiki Kaisha Générateur de gaz pour la production d'azote de haute pureté

Non-Patent Citations (4)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN vol. 014, no. 460 (M - 1032) 4 October 1990 (1990-10-04) *
PATENT ABSTRACTS OF JAPAN vol. 016, no. 311 (M - 1277) 8 July 1992 (1992-07-08) *
PATENT ABSTRACTS OF JAPAN vol. 016, no. 549 (M - 1338) 18 November 1992 (1992-11-18) *
PATENT ABSTRACTS OF JAPAN vol. 1995, no. 04 31 May 1995 (1995-05-31) *

Also Published As

Publication number Publication date
DE10158330A1 (de) 2003-06-18

Similar Documents

Publication Publication Date Title
DE69214693T2 (de) Verfahren zur Herstellung von gasförmigem Sauerstoff unter Druck
EP0669509B1 (fr) Procédé et appareil permettant d'obtenir d l'argon pur
EP1067345B1 (fr) Procédé et dispositif pour la séparation cryogénique des constituants de l'air
EP0955509B1 (fr) Procédé et appareil pour la production d'oxygène à haute pureté
DE3874731T2 (de) Kryogene luftspaltung mit einem aufkocher mit totalkondensation durch kompression/expansion.
DE10013073A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE69917131T2 (de) Stickstoffgenerator mit mehreren Säulen und gleichzeitiger Sauerstofferzeugung
DE69209572T2 (de) Verfahren zur Herstellung von reinstem Stickstoff
EP2322888B1 (fr) Procédé et dispositif d'obtention d'un concentré d'hélium-néon à partir d'air
DE3107151A1 (de) Verfahren und vorrichtung zur verfluessigung und zerlegung von luft
EP4065910A1 (fr) Procédé et installation pour fractionnement à basse température de l'air
DE69004647T2 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft.
DE69301418T2 (de) Kryogenisches Rektifikationssystem mit doppelter Wärmepumpe
DE19933558B4 (de) Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
DE10232430A1 (de) Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft
DE10205096A1 (de) Verfahren und Vorrichtung zur Gewinnung hoch reinen Sauerstoffs aus weniger reinem Sauerstoff
EP1300640A1 (fr) Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air
EP1316768A1 (fr) Procédé et dispositif pour la production d'un liquide ultra pur à partir d'une charge cryogénique en liquide moins pur
EP1001236B1 (fr) Procédé de production d'azote à ultra haute pureté
DE60020500T2 (de) Verfahren zur Luftzerlegung durch Tieftemperaturdestillation
EP1316769A1 (fr) Procédé et dispositif pour la production d'azote ultra pur à partir d'azote moins pur
DE202018006161U1 (de) Anlage zur Tieftemperaturzerlegung von Luft
DE10332862A1 (de) Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung
DE102013017590A1 (de) Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
EP4127583B1 (fr) Procédé et installation de séparation d'air à basse température

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

AX Request for extension of the european patent

Extension state: AL LT LV MK RO SI

17P Request for examination filed

Effective date: 20031107

AKX Designation fees paid

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LI LU MC NL PT SE SK TR

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LINDE AKTIENGESELLSCHAFT

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LINDE AG

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20090603