CN101341370B - Air separating device by means of cryogenic distillation - Google Patents

Air separating device by means of cryogenic distillation Download PDF

Info

Publication number
CN101341370B
CN101341370B CN2006800479541A CN200680047954A CN101341370B CN 101341370 B CN101341370 B CN 101341370B CN 2006800479541 A CN2006800479541 A CN 2006800479541A CN 200680047954 A CN200680047954 A CN 200680047954A CN 101341370 B CN101341370 B CN 101341370B
Authority
CN
China
Prior art keywords
pipeline
destilling tower
exchange pipeline
air
sent
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.)
Active
Application number
CN2006800479541A
Other languages
Chinese (zh)
Other versions
CN101341370A (en
Inventor
B·达维迪安
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.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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 LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of CN101341370A publication Critical patent/CN101341370A/en
Application granted granted Critical
Publication of CN101341370B publication Critical patent/CN101341370B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • F25J3/02—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
    • F25J3/04624—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 integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • 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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
    • 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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface

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)

Abstract

The invention relates to an air separating device by means of cryogenic distillation for producing nitrogen, comprising an exchange line (3), a simple distillation column (7) containing plates and/or structured packings, a supply line for delivery of compressed purified air (1) to the exchange line, a supply line for delivery of the compressed purified and cooled air from the exchange line to the distillation column, a line for withdrawal of a liquid (11) enriched in oxygen from the distillation column for delivery to the exchange line, said exchange line having two sections, a rectifying section (3B) and a heat exchange section (3A), the rectifying section being connected to the column and the line for the enriched liquid and the heat exchange section being connected to the air supply line and the rectifying section.

Description

Utilize the air separation equipment of low temperature distillation
Technical field
The present invention relates to a kind of by separating air by cryogenic distillation, be used in particular for producing the equipment of nitrogen.
Background technology
The nitrogenous generator of describing in US-A-5899093 comprises exchange pipeline and destilling tower, and air to be distilled cools off in this exchange pipeline, and air is separated into the oxygen-rich stream of the nitrogen-enriched stream and the tower bottom of top of tower in this destilling tower.For backflow is provided, the part of nitrogen-enriched stream is sent in evaporimeter-condenser, and here it is by carrying out heat exchange and condensation with oxygen-rich stream.Perhaps, nitrogen can condensation in fractionating column.Be sent in the phase-splitter and the liquid that forms in this phase-splitter flows in the fractionating column again at the rich solution of fractionating column vaporized in part.The objective of the invention is to remove condenser-reboiler, described condenser-reboiler has been forced multiple restriction:
Cost of investment especially for liquid recirculation
Concentrated (CnHm, the N of impurity 2O, CO 2Deng)
Liquid cleans
Liquid level keeps
Level gauging
Summary of the invention
According to one object of the present invention, a kind of equipment by separating air by cryogenic distillation is provided, this equipment comprises:
A) exchange pipeline,
B) accommodate plate and/or form the simple and easy destilling tower of the filler (structured packing) of structure,
C) be used for compression and the air that purifies are sent to the air supply line of described exchange pipeline,
D) being used for will compression, purify and the air of cooling is sent to the pipeline of described destilling tower from described exchange pipeline,
E) be used for extracting the oxygen enriched liquid pipeline that oxygen enriched liquid also is sent to this oxygen enriched liquid described exchange pipeline from described destilling tower,
It is characterized in that described exchange pipeline comprises two parts, fractionation part and heat exchange section; Described fractionation partly is connected to described destilling tower and described oxygen enriched liquid pipeline, described heat exchange section is connected to described air supply line and described fractionation part, and described fractionation partly is connected to described heat exchange section and makes that oxygen enriched liquid evaporates fully and formed gas is sent to described heat exchange section under the situation of not leaving described exchange pipeline in described fractionation part; Described exchange pipeline is placed in the top of described destilling tower; Described fractionation partial fixing is in the top of described destilling tower.
According to optional aim:
-described equipment comprises the device that is used for injecting the device of feed and/or is used to make the device that the air from compression, purification and the cooling of described exchange pipeline expands or the oxygen enriched liquid that extracts from described destilling tower is expanded;
-the pipeline that the described air that is used for compressing, to purify and to cool off is sent to described destilling tower from described exchange pipeline is connected to the cold junction of described heat exchange section;
-described equipment comprises the device of the passage between heat exchange section and the fractionation part that is used to reallocate;
-described exchange pipeline is made by copper or aluminium, and/or described destilling tower is made by stainless steel;
-described exchange pipeline and destilling tower are made of aluminum;
-described exchange pipeline is the soldering plate fin type heat exchanger.
According to another aspect of the present invention; Providing a kind of is comprising the exchange pipeline and is accommodating plate and/or form in the equipment of simple and easy destilling tower of filler of structure method by separating air by cryogenic distillation; Wherein, The air that will compress and purify by the air supply line is sent in the described exchange pipeline; The air of compression, purification and cooling is sent to described destilling tower from described exchange pipeline; By the oxygen enriched liquid pipeline oxygen enriched liquid stream is extracted and is sent to described exchange pipeline from described destilling tower
It is characterized in that described exchange pipeline comprises two parts, fractionation part and heat exchange section; Described fractionation partly is connected to described destilling tower and described oxygen enriched liquid pipeline, described heat exchange section is connected to described air supply line and described fractionation part, and described fractionation partly is connected to described heat exchange section and makes that oxygen enriched liquid evaporates fully and formed gas is sent to described heat exchange section under the situation of not leaving described exchange pipeline in described fractionation part; Described exchange pipeline is placed in the top of described destilling tower; Described fractionation partial fixing is in the top of described destilling tower.
The present invention propose the coldest part by utilizing heat exchanger as fractionating column with condensation nitrogen wherein, thereby in main heat exchanger in conjunction with " evaporation-condensation " function.Advantage of the present invention is as follows:
Provide " nature " of rich solution to clean, this rich solution only concentrates (as pumping unit) slightly by evaporation.
Because do not need diluent liquid to clean, this helps:
Zero eliminates related with it equipment, comprises the rubble groove (or purge tank) that regular cleaning is essential and comprises and be used to guarantee the reliability of cleaning and the equipment of validity;
The gain of zero cooling capacity/cold (increase, gain) (for the equipment with injection feed, the consumption of liquid nitrogen sharply reduces, thereby reduces operating cost),
Zero alleviates/reduces the operation supervise and control to this cleaning, and this monitoring is " key " at secure context.
Eliminate level gauging, pulse connector heating tongs, optional burner and spirit level, and alleviate the operation supervise and control to this measurement, this monitoring is " key " at secure context.
Eliminate recirculation tank.
If the part of cooling capacity gain transforms in (thereby less) exchange pipeline of poor efficiency a little, then the extra cost of heat exchanger is unessential, or even is zero.
Because heat exchanger is above tower, ice chest is higher, but more narrow, obtains significantly gain thus.
Description of drawings
Describe the present invention with reference to the accompanying drawings in further detail, this accompanying drawing illustrates according to air separation equipment of the present invention.
The specific embodiment
Compressed air stream purifies and is sent to the hot junction of exchange pipeline 3 in the clean unit (not shown).The exchange pipeline comprises conventional heat exchange section 3A and fractionation part 3B.These two parts adjacent and the exchange pipeline be the soldering plate fin type heat exchanger.
Air 1 cooling in the exchange pipeline is left the bottom that the exchange pipeline is sent to simple and easy destilling tower 7 then up to the cold junction of part 3A.Tower 7 accommodates filler or the plate 9 that forms structure.
Air is separated into oxygen-rich stream 11 and nitrogen-enriched stream.Oxygen-rich stream 11 is extracted and is sent to the cold junction of part 3B from tower 7 with the form of liquid.Nitrogen-enriched stream directly leaves the top of tower by the passage of part 3B.Preferably, exchange pipeline 3 has the width identical with the top of tower 7 and is welded on the housing of tower (by circle-square or circle-rectangle adapter).
Distill desired cooling capacity and supply by the injection feed of liquid nitrogen 13, this liquid nitrogen 13 obtains from memory cell in the own known mode of describing among the EP-A-0452177.The rich solution turbine of air turbine 1 or evaporation alternatively or additionally, can be provided.
Part 3B comprises two nitrogen passages of a passage that is used for rich solution.Rich solution evaporates so that change into gas fully in the part 3B of exchange pipeline 3 fully.Nitrogen is condensation partly: the part of condensation is because gravity falls into tower as refluxing, and exchange pipeline 3 (by direct welding or alternatively by suitable pipe-line system) is installed in the tower top.The residue of nitrogen continues to rise through whole exchange pipeline 3.
The part 3A of exchange pipeline comprises conventional main exchange pipeline.The rich solution of nitrogen and evaporation is by input air 1 heating.
In order to make exchange pipeline 3 optimizations, between two parts, at the interface, reallocate between nitrogen to be heated that the dinitrogen passage of fractionation part 3B can be in part 3A and the air to be cooled.This can be by fluid inlet/outlet (distributor box) or preferably finishes by inner reallocation (using the demarcation strip of bar and perforation).
Exchange pipeline 3 is preferably made by copper or aluminium, and tower 7 is made by stainless steel.If the exchange pipeline is made of aluminum and tower is made by stainless steel, then one or more portions that are connected must be set between the two.Otherwise exchange pipeline 3 and tower 7 can be made of aluminum.

Claims (7)

1. equipment by separating air by cryogenic distillation comprises:
A) exchange pipeline (3),
B) accommodate plate and/or form the simple and easy destilling tower (7) of the filler of structure,
C) be used for compression and the air that purifies are sent to the air supply line (1) of described exchange pipeline,
D) being used for will compression, purify and the air of cooling is sent to the pipeline of described destilling tower from described exchange pipeline,
E) be used for extracting the oxygen enriched liquid pipeline (11) that oxygen enriched liquid also is sent to this oxygen enriched liquid described exchange pipeline from described destilling tower,
It is characterized in that described exchange pipeline comprises two parts, fractionation part (3B) and heat exchange section (3A); Described fractionation partly is connected to described destilling tower and described oxygen enriched liquid pipeline, described heat exchange section is connected to described air supply line and described fractionation part, and described fractionation partly is connected to described heat exchange section and makes that oxygen enriched liquid evaporates fully and formed gas is sent to described heat exchange section under the situation of not leaving described exchange pipeline in described fractionation part; Described exchange pipeline (3) is placed in the top of described destilling tower (7); Described fractionation part (3B) is fixed in the top of described destilling tower (7).
2. equipment according to claim 1 comprises the device that is used for injecting the device of feed (13) and/or is used to make the device (5) that the air from compression, purification and the cooling of described exchange pipeline (3) expands or the oxygen enriched liquid that extracts from described destilling tower is expanded.
3. equipment according to claim 1 is characterized in that, the pipeline that the described air that is used for compressing, to purify and to cool off is sent to described destilling tower from described exchange pipeline is connected to the cold junction of described heat exchange section (3A).
4. equipment according to claim 1 comprises the device of the passage between heat exchange section and the fractionation part that is used to reallocate.
5. equipment according to claim 1 is characterized in that, described exchange pipeline (3) is made by copper or aluminium, and/or described destilling tower (7) is made by stainless steel.
6. equipment according to claim 1 is characterized in that, described exchange pipeline (3) and destilling tower (7) are made of aluminum.
One kind comprise exchange pipeline (3) and accommodate plate and/or the equipment of simple and easy destilling tower (7) of the filler of formation structure in method by separating air by cryogenic distillation, wherein, the air that will compress and purify by the air supply line is sent in the described exchange pipeline, the air of compression, purification and cooling is sent to described destilling tower from described exchange pipeline, oxygen enriched liquid stream is extracted and be sent to described exchange pipeline from described destilling tower by the oxygen enriched liquid pipeline; It is characterized in that described exchange pipeline comprises two parts, fractionation part (3B) and heat exchange section (3A); Described fractionation partly is connected to described destilling tower and described oxygen enriched liquid pipeline, and described heat exchange section is connected to described air supply line and described fractionation part; And described fractionation partly is connected to described heat exchange section and makes that oxygen enriched liquid evaporates fully and formed gas is sent to described heat exchange section under the situation of not leaving described exchange pipeline in described fractionation part; Described exchange pipeline (3) is placed in the top of described destilling tower (7); Described fractionation part (3B) is fixed in the top of described destilling tower (7).
CN2006800479541A 2005-12-20 2006-12-15 Air separating device by means of cryogenic distillation Active CN101341370B (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0553971A FR2895069B1 (en) 2005-12-20 2005-12-20 APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR0553971 2005-12-20
PCT/FR2006/051366 WO2007074276A2 (en) 2005-12-20 2006-12-15 Air separating device by means of cryogenic distillation

Publications (2)

Publication Number Publication Date
CN101341370A CN101341370A (en) 2009-01-07
CN101341370B true CN101341370B (en) 2011-09-14

Family

ID=36660838

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2006800479541A Active CN101341370B (en) 2005-12-20 2006-12-15 Air separating device by means of cryogenic distillation

Country Status (9)

Country Link
US (1) US20080271481A1 (en)
EP (1) EP1966554B1 (en)
JP (1) JP5074416B2 (en)
CN (1) CN101341370B (en)
DK (1) DK1966554T3 (en)
ES (1) ES2689041T3 (en)
FR (1) FR2895069B1 (en)
PL (1) PL1966554T3 (en)
WO (1) WO2007074276A2 (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2026025A1 (en) * 2007-07-30 2009-02-18 Linde Aktiengesellschaft Process and device for producing high pressure nitrogen by cryogenic separation of air in a single column
FR2929384A1 (en) * 2008-03-27 2009-10-02 Air Liquide Air separating apparatus, has distillation column comprising head condenser with dephlegmator whose horizontal section covers seventy percentage of section of column, and extracting unit extracting nitrogen enriched product in column head
WO2009063146A1 (en) * 2008-03-28 2009-05-22 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchanger and cryogenic-distillation-based air separation device including one such exchanger
FR2973486B1 (en) * 2011-03-31 2013-05-03 Air Liquide AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION
US20220065528A1 (en) * 2019-01-25 2022-03-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for supplying a backup gas under pressure

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5144809A (en) * 1990-08-07 1992-09-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus for production of nitrogen
US5899093A (en) * 1998-05-22 1999-05-04 Air Liquide Process And Construction, Inc. Process and apparatus for the production of nitrogen by cryogenic distillation
CN1295227A (en) * 1999-11-03 2001-05-16 普拉塞尔技术有限公司 Low-temp. rectifying method for production of nitrogen and liquid nitrogen
US6351969B1 (en) * 2001-01-31 2002-03-05 Praxair Technology, Inc. Cryogenic nitrogen production system using a single brazement
EP1146302A3 (en) * 2000-04-14 2003-01-08 Praxair Technology, Inc. Cryogenic air separation system with integrated mass and heat transfer
CN1423108A (en) * 2001-10-04 2003-06-11 林德股份公司 Technology and apparatus producing high-purity nitrogen through low-temp. air fraction distilation

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1472402A (en) * 1973-07-18 1977-05-04 Cryoplants Ltd Air separation
JP2716762B2 (en) * 1988-12-12 1998-02-18 大同ほくさん株式会社 High-purity nitrogen gas production equipment
FR2660741A1 (en) 1990-04-10 1991-10-11 Air Liquide PROCESS AND PLANT FOR GENERATING GASEOUS NITROGEN AND CORRESPONDING NITROGEN SUPPLY SYSTEM THEREFOR.
FR2675568B1 (en) * 1991-04-19 1993-07-16 Air Liquide PROCESS FOR THE CRYOGENIC SEPARATION OF MIXTURES CONTAINING OXYGEN AND TRIMS ORGANIZED FOR THE IMPLEMENTATION OF THIS PROCESS.
FR2690231B1 (en) * 1992-04-17 1994-06-03 Air Liquide RUNOFF HEAT EXCHANGER AND AIR DISTILLATION SYSTEM COMPRISING SUCH AN EXCHANGER.
US5275004A (en) * 1992-07-21 1994-01-04 Air Products And Chemicals, Inc. Consolidated heat exchanger air separation process
US5410885A (en) * 1993-08-09 1995-05-02 Smolarek; James Cryogenic rectification system for lower pressure operation
JP3957842B2 (en) * 1997-11-25 2007-08-15 大陽日酸株式会社 Nitrogen production method and apparatus
US6079223A (en) * 1999-05-04 2000-06-27 Praxair Technology, Inc. Cryogenic air separation system for producing moderate purity oxygen and moderate purity nitrogen
US6237366B1 (en) * 2000-04-14 2001-05-29 Praxair Technology, Inc. Cryogenic air separation system using an integrated core
JP4520667B2 (en) * 2001-07-17 2010-08-11 大陽日酸株式会社 Air separation method and apparatus
US6907751B2 (en) * 2002-07-30 2005-06-21 Air Products And Chemicals, Inc. Liquid distributor
JP4230213B2 (en) * 2002-12-24 2009-02-25 大陽日酸株式会社 Air liquefaction separation apparatus and method

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5144809A (en) * 1990-08-07 1992-09-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus for production of nitrogen
US5899093A (en) * 1998-05-22 1999-05-04 Air Liquide Process And Construction, Inc. Process and apparatus for the production of nitrogen by cryogenic distillation
CN1295227A (en) * 1999-11-03 2001-05-16 普拉塞尔技术有限公司 Low-temp. rectifying method for production of nitrogen and liquid nitrogen
EP1146302A3 (en) * 2000-04-14 2003-01-08 Praxair Technology, Inc. Cryogenic air separation system with integrated mass and heat transfer
US6351969B1 (en) * 2001-01-31 2002-03-05 Praxair Technology, Inc. Cryogenic nitrogen production system using a single brazement
CN1423108A (en) * 2001-10-04 2003-06-11 林德股份公司 Technology and apparatus producing high-purity nitrogen through low-temp. air fraction distilation

Also Published As

Publication number Publication date
DK1966554T3 (en) 2018-10-15
WO2007074276A3 (en) 2007-09-13
EP1966554A2 (en) 2008-09-10
FR2895069A1 (en) 2007-06-22
CN101341370A (en) 2009-01-07
PL1966554T3 (en) 2018-11-30
WO2007074276A2 (en) 2007-07-05
US20080271481A1 (en) 2008-11-06
FR2895069B1 (en) 2014-01-31
EP1966554B1 (en) 2018-08-15
ES2689041T3 (en) 2018-11-08
JP5074416B2 (en) 2012-11-14
JP2009520176A (en) 2009-05-21

Similar Documents

Publication Publication Date Title
JP2833594B2 (en) Low temperature process and equipment for oxygen product production
CN101479550B (en) Cryognic air separation system
CN101341370B (en) Air separating device by means of cryogenic distillation
JP5489805B2 (en) Cryogenic air separation method and apparatus
CN108697970A (en) Method and apparatus in the cryogenic air separation unit integrated with pressure swing adsorption system for argon recycling
US20110067445A1 (en) Method And Apparatus For Separating Air By Cryogenic Distillation
CN102230716A (en) Method and device for separating air through air pressurization, backflow expansion and internal compression
CN101981399A (en) Distillation method and apparatus
JP2009030966A (en) Method and device for producing argon by low-temperature air separation
FR2993353A1 (en) PROCESS AND APPARATUS FOR PURIFYING A LOW TEMPERATURE CARBON DIOXIDE RICH MIXTURE
CN104185767B (en) For the method and apparatus producing two strands of partial air flow purified
CN101535755B (en) Cryogenic air separation system
CN102706097B (en) The equipment of low temperature air separating
CN101198834B (en) Nitrogen generating device and apparatus for use therefor
CN1117260C (en) Air separation method and apparatus thereof
CN1084870C (en) Air separation
CN101071035B (en) Method for delivering purity raised gas and purity improved overheat gas
JP2006284075A (en) Air separating method and its device
KR100275859B1 (en) A manufacturing method for high purity nitrogen gas
CN103988037B (en) Air separating method and device
CN202109724U (en) Air pressurization backflow expansion inner compression air separation device
JP2006275378A (en) Air liquefaction separation method and device
JP3957842B2 (en) Nitrogen production method and apparatus
JP2001165564A (en) Low-temperature air separation method and device
RU2406047C1 (en) Method of producing krypton-xenon mixture and special purity oxygen and device for realising said method

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant