EP1316769A1 - Procédé et dispositif pour la production d'azote ultra pur à partir d'azote moins pur - Google Patents

Procédé et dispositif pour la production d'azote ultra pur à partir d'azote moins pur Download PDF

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Publication number
EP1316769A1
EP1316769A1 EP02024691A EP02024691A EP1316769A1 EP 1316769 A1 EP1316769 A1 EP 1316769A1 EP 02024691 A EP02024691 A EP 02024691A EP 02024691 A EP02024691 A EP 02024691A EP 1316769 A1 EP1316769 A1 EP 1316769A1
Authority
EP
European Patent Office
Prior art keywords
separation column
nitrogen
evaporator
pure nitrogen
column
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP02024691A
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 EP1316769A1 publication Critical patent/EP1316769A1/fr
Withdrawn legal-status Critical Current

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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
    • F25J3/08—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double 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
    • 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 high purity nitrogen from less pure nitrogen, in which a first stream of less pure nitrogen is converted into a first Separation column is initiated and the first separation column a first highly pure Nitrogen product is removed
  • the invention has for its object such a method and / or to specify appropriate device that has a particularly high yield of high have pure nitrogen.
  • the process is therefore designed as a two-pillar process. This makes the same permanent use of energy a higher yield of highly pure product is possible. This can, for example, be withdrawn in gaseous form from the second separation column.
  • the first separation column and the second separation column via a condenser evaporator in heat exchanging Connect.
  • the condenser-evaporator there is preferably one gaseous fraction liquefied from the upper area of the first separation column.
  • the condenser-evaporator is, for example, a reboiler for the second separation column trained, for example as a sump reboiler. Because the difference in concentration between the head of the first and the sump of the second separation column is relatively small the operating pressure of the first separation column is only slightly higher than that of second column to be.
  • the combination of the two separation columns and the The condenser-evaporator is preferably designed as a classic double column.
  • the liquid formed in the condenser-evaporator can firstly Part of it can be obtained as the first high purity nitrogen product. Another part can be given as a return to the second separation column.
  • the first stream of less pure nitrogen is, for example, in liquid form in the first separation column initiated.
  • a second stream can be less pure Nitrogen gas are introduced into the first separation column. This can help a separate heat exchanger for generating rising steam for the first separation column can be dispensed with.
  • the one required to operate the separation column For example, steam (second stream) is taken directly from the storage tank.
  • a liquid from the first separation column can be in one Boilers are evaporated to produce rising steam.
  • compressed gas e.g. from a pipeline system
  • this can be introduced into the storage tank.
  • 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 12.
  • a storage tank 1 which in the exemplary embodiment forms the less pure cryogenic feed liquid.
  • the tank 1 can for example be filled by means of tank vehicles or a pipeline (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, for example, with water or air.
  • the resulting gaseous nitrogen 4 is introduced into the gas space of the storage tank 1. It flows through heat exchanger tubes 5 and thereby enters into indirect heat exchange with the liquid stored in the tank. In this way, the pressure level in the storage tank 1 is kept at 5 to 12 bar without the need for external energy.
  • the medium for heating the pressure build-up evaporator is usually 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.
  • FIG. 2 differs from FIG. 1 in that a compressed gas stream from an external source, for example from a pipeline network for nitrogen of technical purity, is introduced into the system.
  • the compressed gas stream 24 is cooled in a heat exchanger 25 and introduced into the storage tank 1 via line 26, in the example together with the steam 4 from the pressure build-up evaporator 3.
  • FIG. 3 also shows a modification of the process shown in FIG. 1.
  • the introduction of a gaseous feed fraction into the first separation column 7 is dispensed with here. Instead, this column has a sump evaporator 28, in which rising steam is generated by indirect heat exchange with a heating medium.
  • the heating means can be formed by any suitable medium.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP02024691A 2001-11-28 2002-11-05 Procédé et dispositif pour la production d'azote ultra pur à partir d'azote moins pur Withdrawn EP1316769A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10158327 2001-11-28
DE10158327A DE10158327A1 (de) 2001-11-28 2001-11-28 Verfahren und Vorrichtung zur Herstellung hoch reinen Stickstoffs aus weniger reinem Stickstoff

Publications (1)

Publication Number Publication Date
EP1316769A1 true EP1316769A1 (fr) 2003-06-04

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP02024691A Withdrawn EP1316769A1 (fr) 2001-11-28 2002-11-05 Procédé et dispositif pour la production d'azote ultra pur à partir d'azote moins pur

Country Status (2)

Country Link
EP (1) EP1316769A1 (fr)
DE (1) DE10158327A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104482719B (zh) * 2014-12-16 2017-01-04 新余钢铁集团有限公司 低温液体返灌装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
EP0701099A1 (fr) * 1994-09-12 1996-03-13 Liquid Air Engineering Corporation Procédé et installation de production d'azote de haute pureté
EP0754923A2 (fr) * 1995-07-21 1997-01-22 Teisan Kabushiki Kaisha Procédé et dispositif de production d'azote d'ultra haute pureté
DE19929798A1 (de) * 1998-11-11 2000-05-25 Linde Ag Verfahren zur Gewinnung von ultrareinem Stickstoff

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
EP0701099A1 (fr) * 1994-09-12 1996-03-13 Liquid Air Engineering Corporation Procédé et installation de production d'azote de haute pureté
EP0754923A2 (fr) * 1995-07-21 1997-01-22 Teisan Kabushiki Kaisha Procédé et dispositif de production d'azote d'ultra haute pureté
DE19929798A1 (de) * 1998-11-11 2000-05-25 Linde Ag Verfahren zur Gewinnung von ultrareinem Stickstoff

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
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) *

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Publication number Publication date
DE10158327A1 (de) 2003-06-18

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