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EP2662654A1 - Processus et appareil pour la séparation de lýair par distillation cryogénique - Google Patents

Processus et appareil pour la séparation de lýair par distillation cryogénique Download PDF

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Publication number
EP2662654A1
EP2662654A1 EP12305506.3A EP12305506A EP2662654A1 EP 2662654 A1 EP2662654 A1 EP 2662654A1 EP 12305506 A EP12305506 A EP 12305506A EP 2662654 A1 EP2662654 A1 EP 2662654A1
Authority
EP
European Patent Office
Prior art keywords
column
heat exchanger
oxygen
nitrogen
liquid
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Withdrawn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
EP12305506.3A
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German (de)
English (en)
Inventor
Jean-Renaud Brugerolle
Bao Ha
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
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 Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP12305506.3A priority Critical patent/EP2662654A1/fr
Publication of EP2662654A1 publication Critical patent/EP2662654A1/fr
Withdrawn legal-status Critical Current

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    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • 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
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
    • F25J3/04248—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate 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
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air

Definitions

  • the present invention relates to a process and apparatus for the separation of air by cryogenic distillation.
  • An Integrated Gasified Combined Cycle is usually selected to generate clean energy from coal. This clean energy production technique is especially suited for new coal-based power generation projects specified to operate efficiently and with minimal pollution to the environment.
  • the air separation unit (ASU) for the IGCC is a combination of an oxygen plant and a nitrogen generator plant.
  • the air separation process frequently used for this type of application is the elevated pressure process.
  • air separation units operating with this concept have good energy efficiency and reduced power consumption, it is not always possible to use this sort of ASU because the nitrogen/oxygen ratio is generally fixed at a value close to that found for air, ie close to 3.6. If the required ratio is higher than this value, for example about 5, then an elevated pressure plant would be required to use an excess air to generate the needed quantity of nitrogen and by doing so it will generate wastefully an excess of oxygen under pressure, which reduces the efficiency of the process. It can be seen that a different process cycle needs to be used in this situation to satisfy the requirement of nitrogen/oxygen ratio and at the same time yielding good cycle efficiency.
  • An object of the present invention is to provide an air separation unit with reduced energy consumption but which is capable of producing nitrogen and oxygen with a nitrogen/oxygen ratio of greater than 3.6, preferably greater than 4.
  • FR-A-2930328 describes an air separation process in which liquid oxygen is vaporized in the top condenser of a low pressure column, which is heated using a double reboiler system.
  • an apparatus for the separation of air by cryogenic distillation comprising a column system having a first column of a column system operating at between 9 and 17 bars abs and at least a second column operating at a pressure lower than that of the first column, the second column having a top condenser and a bottom vaporizer, a heat exchanger for cooling purified air, a conduit for sending nitrogen enriched liquid from the first column to the second column, a conduit and possibly separation means for sending oxygen enriched liquid from the first column or a liquid derived therefrom to the second column, a pump for pressurizing oxygen rich liquid removed from the bottom of the second column, a conduit for sending pressurized oxygen rich liquid to be vaporized in the heat exchanger, a conduit for removing vaporized pressurized oxygen rich liquid as a pressurized gaseous oxygen product, a conduit for removing nitrogen rich fluid from at least one column of the column system and for sending the nitrogen rich fluid to be warmed in the heat exchanger and removed as a
  • figure 1 shows a process according to the invention.
  • An oxygen enriched fluid contains at least 30% mol. oxygen and an oxygen rich fluid contains at least 80% mol oxygen.
  • a nitrogen enriched fluid contains at least 85% nitrogen and a nitrogen rich fluid contains at least 90% mol. nitrogen.
  • Figure 1 shows a double column having a first column 100 operating at between 12 and 17 bars abs and a second column 200 operating at between 4.2 and 6.3 bars abs.
  • the reboiler 70 at the bottom of the second column is warmed using nitrogen rich gas from the top of the first column in order to vaporize the bottom liquid of the second column 200.
  • Air is cooled using a brazed aluminum plate fin heat exchanger 400.
  • the cold compressed air is removed as stream 8 from the heat exchanger and is then expanded in a dense fluid expander 89 or a valve and sent to the first column 100 and possibly to the second column 200.
  • Fraction 5 of the air is cooled in the heat exchanger at the outlet pressure of booster 94 to a temperature T3 colder than T1, removed as stream 16 and expanded in a turbine 91 to form expanded stream 6 before being sent to the first column 100 in gaseous form.
  • Fraction 11 is boosted in a booster 95, cooled in the heat exchanger 400, removed as stream 15 to a temperature T4 colder than T1 and sent to turbine 92 to produce expanded stream 7 and thence to first column 100.
  • Part 4 of the air from the main compressor is cooled at the pressure of the first column in heat exchanger 100 and introduced as stream 9 into the first column 100 in gaseous form.
  • Turbine 91 is preferably coupled to compressor 93 and turbine 92 is preferably coupled to compressor 95.
  • Oxygen enriched liquid 10 from the bottom of the first column 100 is expanded in valve and sent to a third column 300 operating at a pressure between the pressure of the first column and the pressure of the second column 200.
  • the oxygen enriched liquid is separated in the third column forming a bottom liquid further enriched in oxygen 31. Part of this liquid is sent as stream 34 to the top condenser 72 of the third column 300 after expansion in a valve.
  • the vaporized liquid 36 is then sent to the second column 200.
  • the rest 35 is expanded in a valve and sent to the second column 200.
  • An intermediate liquid stream 20 is removed from the first column 100, expanded and sent to the second column 200.
  • Nitrogen enriched liquid 40 from the top of the first column is expanded in a valve and sent to the top of the second column 200.
  • Nitrogen enriched gas from the top of the first column is used to heat bottom reboiler 71 of the third column 300.
  • the liquid produced is sent in part back to the top of the first column 100 and in part as part of stream 40 to the top of the second column.
  • Nitrogen enriched liquid 44 from the top of the third column 300 is expanded and sent to the top of the second column 200.
  • Oxygen rich liquid 30 containing at least 80% oxygen is removed from the bottom of the second column 200, pressurized in pump 90 and sent as liquid to the heat exchanger 400 where it vaporizes to form 217 Nm 3 /h of pressurized oxygen rich gas 51 containing 95% oxygen at 67 bars.
  • Nitrogen rich gas 60 from the top of the second column 200 is warmed in heat exchanger and removed as 713 Nm 3 /h of gas 52 at 5 bars abs.
  • Nitrogen rich gas 42 containing at least 85% nitrogen is removed from the top of the first column 100, warmed in exchanger 400 and removed as 70 Nm 3 /h of nitrogen rich gas 50 at 15 bars abs.
  • the ratio between nitrogen rich gas (50 and 51) and the oxygen rich gas (51) is in the region of 3.6.
  • the solution according to the invention is to vaporize part of the oxygen from the bottom of the second column 100 in a top condenser 73 of the second column 200.
  • Part 26 of oxygen rich liquid 30 is taken at the pressure of the second column 200, divided from stream 30, expanded to just above atmospheric pressure in a valve and sent to the top condenser 73 wherein it is vaporized to form a waste gas 25, warmed in heat exchanger 400 to form waste stream 53.
  • Nitrogen rich gas from the top of the second column 200 is condensed in the top condenser 73.
  • a nitrogen rich gaseous stream 60 is removed from the top of the second column, warmed in heat exchanger 400 to form stream 52.
  • the figure shows a triple column but the invention applies equally to a double column process in which the oxygen enriched liquid 10 is sent directly from the first to the second column.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP12305506.3A 2012-05-07 2012-05-07 Processus et appareil pour la séparation de lýair par distillation cryogénique Withdrawn EP2662654A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP12305506.3A EP2662654A1 (fr) 2012-05-07 2012-05-07 Processus et appareil pour la séparation de lýair par distillation cryogénique

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP12305506.3A EP2662654A1 (fr) 2012-05-07 2012-05-07 Processus et appareil pour la séparation de lýair par distillation cryogénique

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EP2662654A1 true EP2662654A1 (fr) 2013-11-13

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111433545A (zh) * 2017-12-28 2020-07-17 乔治洛德方法研究和开发液化空气有限公司 在包括裂芯式主热交换器的空气分离单元中产生的富氮流的利用
US20220090855A1 (en) * 2020-09-18 2022-03-24 L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5901576A (en) * 1998-01-22 1999-05-11 Air Products And Chemicals, Inc. Single expander and a cold compressor process to produce oxygen
EP0924486A2 (fr) * 1997-12-19 1999-06-23 The BOC Group plc Séparation d'air
EP0955509A1 (fr) * 1998-04-30 1999-11-10 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté
US6116052A (en) * 1999-04-09 2000-09-12 Air Liquide Process And Construction Cryogenic air separation process and installation
US6196023B1 (en) * 1996-10-30 2001-03-06 Linde Aktiengesellschaft Method and device for producing compressed nitrogen
FR2864213A1 (fr) * 2003-12-17 2005-06-24 Air Liquide Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air
FR2930328A1 (fr) 2008-04-22 2009-10-23 Air Liquide Procede et appareil de separation d'air par distillation cryogenique

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6196023B1 (en) * 1996-10-30 2001-03-06 Linde Aktiengesellschaft Method and device for producing compressed nitrogen
EP0924486A2 (fr) * 1997-12-19 1999-06-23 The BOC Group plc Séparation d'air
US5901576A (en) * 1998-01-22 1999-05-11 Air Products And Chemicals, Inc. Single expander and a cold compressor process to produce oxygen
EP0955509A1 (fr) * 1998-04-30 1999-11-10 Linde Aktiengesellschaft Procédé et appareil pour la production d'oxygène à haute pureté
US6116052A (en) * 1999-04-09 2000-09-12 Air Liquide Process And Construction Cryogenic air separation process and installation
FR2864213A1 (fr) * 2003-12-17 2005-06-24 Air Liquide Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air
FR2930328A1 (fr) 2008-04-22 2009-10-23 Air Liquide Procede et appareil de separation d'air par distillation cryogenique

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111433545A (zh) * 2017-12-28 2020-07-17 乔治洛德方法研究和开发液化空气有限公司 在包括裂芯式主热交换器的空气分离单元中产生的富氮流的利用
CN111433545B (zh) * 2017-12-28 2022-03-04 乔治洛德方法研究和开发液化空气有限公司 在包括裂芯式主热交换器的空气分离单元中产生的富氮流的利用
US11635254B2 (en) 2017-12-28 2023-04-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Utilization of nitrogen-enriched streams produced in air separation units comprising split-core main heat exchangers
US20220090855A1 (en) * 2020-09-18 2022-03-24 L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen
US11988446B2 (en) * 2020-09-18 2024-05-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen

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