AU2007202735B8 - Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air - Google Patents

Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air Download PDF

Info

Publication number
AU2007202735B8
AU2007202735B8 AU2007202735A AU2007202735A AU2007202735B8 AU 2007202735 B8 AU2007202735 B8 AU 2007202735B8 AU 2007202735 A AU2007202735 A AU 2007202735A AU 2007202735 A AU2007202735 A AU 2007202735A AU 2007202735 B8 AU2007202735 B8 AU 2007202735B8
Authority
AU
Australia
Prior art keywords
pressurised
nitrogen
oxygen
heat exchanger
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.)
Ceased
Application number
AU2007202735A
Other versions
AU2007202735B2 (en
AU2007202735A1 (en
Inventor
Alain Guillard
Herve Le Bihan
Patrick Le Bot
Jean-Marc Peyron
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
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
Publication of AU2007202735A1 publication Critical patent/AU2007202735A1/en
Application granted granted Critical
Publication of AU2007202735B2 publication Critical patent/AU2007202735B2/en
Publication of AU2007202735B8 publication Critical patent/AU2007202735B8/en
Ceased legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • F25J3/04406—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
    • F25J3/04006—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
    • F25J3/04084—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 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
    • 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
    • F25J3/04248—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
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation

Description

AUSTRALIA Patents Act COMPLETE SPECIFICATION (ORIGINAL) Class Int. Class Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Priority Related Art: Name of Applicant: L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedes Georges Claude Actual Inventor(s): Alain Guillard, Jean-Marc Peyron, Herve Le Bihan, Patrick Le Bot Address for Service and Correspondence: PHILLIPS ORMONDE & FITZPATRICK Patent and Trade Mark Attorneys 367 Collins Street Melbourne 3000 AUSTRALIA Invention Title: PROCESS FOR THE PRODUCTION OF PRESSURISED OXYGEN AND NITROGEN BY CRYOGENIC DISTILLATION OF AIR Our Ref: 800277 POF Code: 1290/43509 The following statement is a full description of this invention, including the best method of performing it known to applicant(s): 6-1Q 1A Process for the production of pressurized oxygen and nitrogen by cryogenic distillation of air This application claims priority from Malaysian Application No.PI 20063064 filed on 28 June 2006, the contents of which are to be taken as incorporated herein by this reference. The present invention relates to a process for the production of pressurised 5 oxygen and nitrogen by cryogenic distillation of air. In certain application, an air separation unit provides at least two kinds of pressurised product, namely oxygen and nitrogen and sometimes also argon. The quantities required for each product may be continuous or variable and different systems are known to adapt the production of the air separation to the 10 instantaneous requirements of the consumer. However during start-up of his plant, the consumer sometimes requires very different amounts of the products than those requirements when the plant is in stable operation. Often very large quantities of inert gas, such as nitrogen, are required during 15 start-up whereas the requirements of the same gas during stable operation are negligible. Similarly, only very small amounts of oxygen are required during the start up phase. To supply these demands the nitrogen is obtained from an existing network 20 and is formed by vaporising liquid, which is both complex and inefficient. Additionally for projects in developing regions where there is no existing network, the provision of liquid can be problematic. Furthermore the nitrogen compressor has to be dimensioned for the maximum production even though this lasts for a short period during start-up. 25 The present invention is intended to overcome, or at least alleviate, one or more of the drawbacks of the prior art. According to one aspect of the invention, there is provided a process for operating an air separation unit according to first and second modes in which: - according to the first mode: 30 a) compressed and purified air is cooled in a heat exchanger and sent to an air separation unit having a column system including at least two distillation columns 2 b) a first quantity of liquid oxygen is removed from the system, pressurised and vaporised in the heat exchanger c) no liquid nitrogen or alternatively a first quantity of liquid nitrogen is removed from the system, pressurised and vaporised in the heat exchanger 5 - according to the second mode: a) compressed and purified air is cooled in the heat exchanger and sent to the air separation unit b) a second quantity of liquid nitrogen is removed from the system, pressurised and vaporised in the heat exchanger 10 c) no liquid oxygen or alternatively a second quantity of liquid oxygen is removed from the system, pressurised and vaporised in the heat exchanger d) wherein e) the first quantity of liquid nitrogen, if it exists, is less than the second quantity of liquid nitrogen and/or the second quantity of liquid oxygen, if it exists, 15 is less than the first quantity of liquid oxygen and f) the first quantity of liquid oxygen is greater than the first quantity of liquid nitrogen, if it exists, and the second quantity of .liquid nitrogen is greater than the second quantity of liquid oxygen, if it exists. Optionally: 20 - in at least one of the first and second modes liquid argon is removed from the system, pressurised and vaporised in the heat exchanger. - the pressure of the pressurised liquid oxygen and/or the pressurised liquid nitrogen is greater than 20 bars abs. - the ratio of the first quantity of liquid nitrogen and the second quantity of 25 liquid nitrogen is less than 0.2. - the volume of compressed air sent to the column system varies by not more than 10% between the first and second modes, preferably by not more than 5%. The invention will be described in further detail with reference to the Figure. 30 To simplify the figure, the usual reflux streams of the double column are not shown. Further details of the air separation unit may be found in "Oxygen enhanced combustion" CRC Press, 1998 in the section of on oxygen production.
3 Air 1 is compressed in a compressor 3 to approximately the pressure of the medium pressure column 27 and purified in purification unit 7 to form stream 9. Stream 9 is divided into three parts. Portion 11 is sent to compressor 19, 5 compressed to a high pressure therein and sent to the heat exchanger. It is then cooled as stream 21, divided in two (streams 23,25), expanded, liquefied and sent to the medium pressure and low pressure columns 27,29 respectively. This stream may be cooled in the heat exchanger at a subcritical or supercritical pressure. 10 Another stream 17 is cooled at the medium pressure and sent to the medium pressure column 27. Finally stream 13 is sent to a booster 15 and thence to the heat exchanger 33 where it is partially cooled. At an intermediate pressure of the heat exchanger 33 it is withdrawn and expanded in turbine 35 to the medium pressure. It is then 15 sent to the medium pressure column. The air compression, cooling and expansion system is described to give an example of an air separation unit according to the invention. However any suitable air compression, cooling and expansion system could be used. According to a first mode of operation which may correspond to the online 20 mode, a first quantity of oxygen is withdrawn from the bottom of the low pressure column, pressurised by pump 43 and sent to the heat exchanger 33 wherein it vaporises to form pressurised gas. A first quantity of liquid nitrogen is withdrawn from the medium pressure column 27, pressurised by pump 45 and sent to the heat exchanger 33 wherein it vaporises to form pressurised gas. The amount of 25 nitrogen produced is very small compared to the amount of oxygen. According to a second mode of operation which may correspond to the start up mode, a first quantity of oxygen is withdrawn from the bottom of the low pressure column, pressurised by pump 43 and sent to the heat exchanger 33 wherein it vaporises to form pressurised gas. A first quantity of liquid nitrogen is 30 withdrawn from the medium pressure column 27, pressurised by pump 45 and sent to the heat exchanger 33 wherein it vaporises to form pressurised gas. The amount of oxygen produced is small compared to the amount of nitrogen.
4 However much more nitrogen is produced according to the second mode than the first mode. For example, the ratio of nitrogen in the first mode to that in the second mode is less than 0.2, preferably less than 0.1, or even less than 0.05 or 0.03. 5 Since the compressors 3 and 19 produce volumes of air varying by not more than 10% between the first and second modes, the thermal equilibrium of the heat exchanger is not substantially modified between the first and second modes. If the amount of nitrogen produced in the second mode is not sufficient, additional nitrogen may be provided from a network 45 using compressor 43. 10 The air separation unit produces the gaseous pressurised products by vaporisation in the heat exchange line. Thus the air separation unit can be used in two different modes. During start up of the consumer's plant, the air separation unit operates in start up mode and during stable operation on the consumer's plant, the air separation unit operates 15 in online mode. During the start up mode, the air separation unit produces large quantities of pressurised nitrogen as well as small quantities of oxygen. Alternatively no oxygen may be produced. The pumps for pressurising the liquids are dimensioned to this end. 20 During the online mode, the amount of pressurised nitrogen produced will be much less and the amount of pressurised oxygen is increased. The following numerical example will help to illustrate the invention. On-line mode (first mode): production of products by pumping and subsequent vaporisation 25 Oxygen: 100 000 Nm3/h - 40 bara- 99.5% Nitrogen :2600 Nm3/h - 10 bara - 50 ppm 02 Start-up mode (second mode) production of products by pumping and subsequent vaporisation 30 Oxygen : 68000 Nm3/h - 40 bara-99.5% Nitrogen: 59 800 Nm3/h - 10 bara-50 ppm 02.
5 If the oxygen production stops, because an oxygen pump malfunctions, for example, large amounts of nitrogen may be required to prevent an accident in the client's plant (production of inert gas injection of inert gas to maintain combustion speed and to agitate liquid baths). The invention allows the air separation unit to 5 provide for these needs. A reference herein to a patent document or other matter which is given as prior art is not to be taken as an admission that that document or matter was known or that the information it contains was part of the common general knowledge as at 10 the priority date of any of the claims. 15 20 25 30

Claims (6)

1. Process for operating an air separation unit according to first and second 5 modes in which: according to the first mode: a) compressed and purified air is cooled in a heat exchanger and sent to an air separation unit having a column system including at least two distillation columns; 10 b) a first quantity of liquid oxygen is removed from the system, pressurised and vaporised in the heat exchanger c) no liquid nitrogen or alternatively a first quantity of liquid nitrogen is removed from the system, pressurised and vaporised in the heat exchanger according to the second mode: 15 a) compressed and purified air is cooled in the heat exchanger and sent to the air separation unit b) a second quantity of liquid nitrogen is removed from the system, pressurised and vaporised in the heat exchanger c) no liquid oxygen or alternatively a second quantity of liquid oxygen 20 is removed from the system, pressurised and vaporised in the heat exchanger wherein: d) the first quantity of liquid nitrogen, if it exists, is less than the second quantity of liquid nitrogen and/or the second quantity of liquid oxygen, if it exists, is less than the first quantity of liquid oxygen and 25 e) the first quantity of liquid oxygen is greater than the first quantity of liquid nitrogen, if it exists, and the second quantity of .liquid nitrogen is greater than the second quantity of liquid oxygen, if it exists.
2. Process according to Claim 1 wherein in at least one of the first and second 30 modes liquid argon is removed from the system, pressurised and vaporised in the heat exchanger. 7
3. Process according to Claim 1 or claim 2 wherein the pressure of the pressurised liquid oxygen and/or the pressurised liquid nitrogen is greater than 20 bars abs. 5
4. Process according to any one of the preceding claims wherein the ratio of the first quantity of liquid nitrogen and the second quantity of liquid nitrogen is less than 0.2. 10
5. Process according to any one of the preceding claims wherein the volume of compressed air sent to the column system varies by not more than 10% between the first and second modes.
6. A process for operating an air separation unit, substantially as hereinbefore 15 described with reference to the Figure.
AU2007202735A 2006-06-28 2007-06-13 Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air Ceased AU2007202735B8 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
MYPI20063064 MY143107A (en) 2006-06-28 2006-06-28 Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air
MYPI20063064 2006-06-28

Publications (3)

Publication Number Publication Date
AU2007202735A1 AU2007202735A1 (en) 2008-01-17
AU2007202735B2 AU2007202735B2 (en) 2010-09-16
AU2007202735B8 true AU2007202735B8 (en) 2011-01-20

Family

ID=38973101

Family Applications (1)

Application Number Title Priority Date Filing Date
AU2007202735A Ceased AU2007202735B8 (en) 2006-06-28 2007-06-13 Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air

Country Status (3)

Country Link
CN (1) CN101096269B (en)
AU (1) AU2007202735B8 (en)
MY (1) MY143107A (en)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5511381A (en) * 1994-03-16 1996-04-30 The Boc Group Plc Air separation
US5685173A (en) * 1995-09-29 1997-11-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and plant for the production of a gas under pressure by cryogenic distillation

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5832401B2 (en) * 1976-10-04 1983-07-13 株式会社神戸製鋼所 Air separation equipment operation control method
US5231837A (en) * 1991-10-15 1993-08-03 Liquid Air Engineering Corporation Cryogenic distillation process for the production of oxygen and nitrogen
FR2767317B1 (en) * 1997-08-14 1999-09-10 Air Liquide PROCESS FOR CONVERTING A FLOW CONTAINING HYDROCARBONS BY PARTIAL OXIDATION

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5511381A (en) * 1994-03-16 1996-04-30 The Boc Group Plc Air separation
US5685173A (en) * 1995-09-29 1997-11-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and plant for the production of a gas under pressure by cryogenic distillation

Also Published As

Publication number Publication date
MY143107A (en) 2011-03-15
CN101096269A (en) 2008-01-02
AU2007202735B2 (en) 2010-09-16
AU2007202735A1 (en) 2008-01-17
CN101096269B (en) 2011-05-04

Similar Documents

Publication Publication Date Title
EP1043558B1 (en) Integrated apparatus for generating power and/or oxygen enriched fluid, and process thereof
US6202442B1 (en) Integrated apparatus for generating power and/or oxygen enriched fluid and process for the operation thereof
US8695377B2 (en) Process and apparatus for the separation of air by cryogenic distillation
KR100421071B1 (en) Method and device for the production of variable amounts of a pressurized gaseous product
US5941098A (en) Method and plant for supplying a variable flow rate of a gas from air
EP1972875A1 (en) Process and apparatus for the separation of air by cryogenic distillation
US20090007595A1 (en) Low Temperature Air Separation Process for Producing Pressurized Gaseous Product
EP1767884A1 (en) Process and apparatus for the separation of air by cryogenic distillation
JP2692700B2 (en) Method and apparatus for cryogenic separation of compressed feed air to produce high pressure oxygen and nitrogen products
US6666048B1 (en) Variable capacity fluid mixture separation apparatus and process
KR970062629A (en) Method and apparatus for producing high pressure oxygen
US6568207B1 (en) Integrated process and installation for the separation of air fed by compressed air from several compressors
US20020121106A1 (en) Three-column system for the low-temperature fractionation of air
MXPA02007813A (en) Multiple process plant product lines from a common set of engineered components.
AU2007202735B2 (en) Process for the production of pressurised oxygen and nitrogen by cryogenic distillation of air
CN102985776B (en) For the method and apparatus by separating air by cryogenic distillation
EP3196574B1 (en) Process and apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air
RU2354902C2 (en) Method and installation for high purity oxygen provision by means of cryogenic distillation of air
US20040244416A1 (en) Method for separating air by cryogenic distillation and installation therefor
AU2005225027A1 (en) Process and apparatus for the separation of air by cryogenic distillation
EP2562502A1 (en) Process and installation for supplying gaseous carbon monoxide by cryogenic distillation
JP3479277B2 (en) Variable oxygen flow delivery method and low temperature air separation device using the same
EP4357708A2 (en) Process and apparatus for improved recovery of argon
Singla et al. Strategizing practical implementation of additional condenser-reboilers (CR) to reduce power consumption of a dual purity cryogenic single column gaseous oxygen plant
US20240125550A1 (en) Process and Apparatus for Improved Recovery of Argon

Legal Events

Date Code Title Description
FGA Letters patent sealed or granted (standard patent)
TH Corrigenda

Free format text: IN VOL 24, NO 37, PAGE(S) 4345 UNDER THE HEADING APPLICATIONS ACCEPTED - NAME INDEX UNDER THE NAME L AIR LIQUIDE, SOCIETE ANONYME POUR L ETUDE ET L EXPLOITATION DES PROCEDES GEORGES CLAUDE, APPLICATION NO. 2007202735, UNDER INID (72) CORRECT THE CO-INVENTOR TO LE BIHAN, HERVE

MK14 Patent ceased section 143(a) (annual fees not paid) or expired