GB1586961A - Separation of gaseous mixtures - Google Patents

Separation of gaseous mixtures Download PDF

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Publication number
GB1586961A
GB1586961A GB35176/76A GB3517676A GB1586961A GB 1586961 A GB1586961 A GB 1586961A GB 35176/76 A GB35176/76 A GB 35176/76A GB 3517676 A GB3517676 A GB 3517676A GB 1586961 A GB1586961 A GB 1586961A
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Prior art keywords
bed
gas
air
stream
adsorbent
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GB35176/76A
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BOC Ltd
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BOC Ltd
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Publication date
Application filed by BOC Ltd filed Critical BOC Ltd
Priority to GB35176/76A priority Critical patent/GB1586961A/en
Priority to ZA00774932A priority patent/ZA774932B/en
Priority to BR7705591A priority patent/BR7705591A/en
Priority to ES461831A priority patent/ES461831A1/en
Priority to JP10100577A priority patent/JPS5342182A/en
Priority to FR7725845A priority patent/FR2363069A1/en
Priority to AU28177/77A priority patent/AU509650B2/en
Publication of GB1586961A publication Critical patent/GB1586961A/en
Expired legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/12—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/102—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B01D2257/7022—Aliphatic hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/401—Further details for adsorption processes and devices using a single bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F25J2205/72—Pressurising or depressurising the adsorption vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

(54) SEPARATION OF GASEOUS MIXTURES (71) We, BOC LIMITED, of Hammersmith House, London, W6 9DX, England an English company, do hereby declare the invention, for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement: This invention relates to the separation of gaseous mixtures and is particularly, although not exclusively, suitable for air separation.
Large scale cryogenic air separation plants, for example plants capable of producing as much as a thousand tons per day of oxygen, are now well known. Such plants often employ extremely large reversing heat exchangers in which water and carbon dioxide in a feed air stream are condensed as the air is cooled by heat exchange with streams of waste nitrogen and product oxygen. The streams of inlet air and waste nitrogen are from time to time switched so that the waste nitrogen cleans away water and carbon dioxide condensed in passages through which feed air has been passed immediately beforehand.
However in order to effect satisfactory cleaning it is normally necessary for the volume of the waste nitrogen stream to constitute 45% or so of the volume of air fed to the system for separation. Furthermore the heat exchanger only removes products such as water and carbon dioxide from the inlet air and other possible contaminants, for example acetylene, pass through the heat exchanger to the rectification column.
According to the invention there is provided a process for separating a gaseous mixture comprising the steps of feeding the mixture through an adsorbent bed to remove by adsorption one or more components of the mixture. cooling and rectifying the unadsorbed gas to produce a product relatively rich in a desired component of the gaseous mixture and a waste gas relatively lean in the desired component, and regenerating the adsorbent bed by purging it with a stream of the waste gas, the steps of adsorption and regeneration being performed at substantially the same temperature.
The invention also provides gas separation plant for performing the process comprising an adsorbent bed adapted to remove by adsorption one or more components of a gaseous mixture fed therethrough, means for cooling and rectifying the unadsorbed gas to produce a product relatively rich in a desired component of the gaseous mixture and a waste gas relatively lean in the desired component and means for regenerating the adsorbent bed by purging the bed with a stream of the waste gas, there being no means for substantially varying the temperature of the bed.
The invention is particularly suitable for obtaining high purity oxygen from air. The adsorbent bed preferably contains an adsorbent which preferentially adsorbs water and carbon dioxide from the air stream, for example alumina. There may also be provided further adsorbents in the bed, or further beds, which preferentially adsorb other constituents of the air stream, for example acetylene.
When air is separated by a process according to the invention it is the waste nitrogen stream which is used to purge the adsorbent bed. The waste nitrogen stream is usually at a lower pressure than that of the feed stream so that the pressure difference between adsorption and purging of the bed assists in the regeneration of the bed.
A plurality of adsorbent beds are preferably employed and the feeding and regenerating steps for each bed sequenced so that a substantially continuous supply of enriched gas is obtained from the beds.
Preferably a reservoir is provided to receive an initial portion of the effluent gas from a bed being purged, the gas in such reservoir being used to repressurise the absorbent bed(s) after regeneration thereof.
In the case of air separation, traces of oxygen and nitrogen will remain in the interstitial volume of an adsorbent bed after a feed of air therethrough so that the initial effluent obtained from the bed during purging will be rich in such gases. This initial effluent may be stored and used for repressurising the bed(s) after regeneration to bring them up to pressure for another feed step.
The unadsorbed gas is preferably cooled prior to rectification by heat exchange with the stream of waste gas and/or a stream or streams of product gas obtained from the rectification step. Such heat exchange may conveniently take place in an ordinary (non-reversing) matrix heat exchanger.
Cooling and rectification can be more effective in a cryogenic system if the stream of unadsorbed gas is at an elevated pressure before it is fed to the rectification column.
The inlet air fed to the adsorbent bed(s) is therefore preferably compressed so that the enriched stream of gas leaving the adsorption unit will be at an elevated pressure.
A preferred embodiment of an air separation plant according to the invention will now be more particularly described by way of example and with reference to the accompanying diagrammatic drawing of such a plant.
Referring to the drawing a compressor 10 draws in air through line 11 and delivers compressed air through line 12 to an adsorption unit 13. The adsorption unit comprises two beds 14 and 15 containing adsorbents which preferentially adsorb water and carbon dioxide from the air and possibly further adsorbents which preferentially adsorb e.g. acetylene. The air is fed into one or other of the beds 14 or 15. The unadsorbed gas from the bed 14 or 15 is delivered into an outlet line 18 through valved line 19 or 20. This unadsorbed gas (from which carbon dioxide, water and possibly other constituents, such as acetylene, have been removed) is then passed via a pipeline 18 through a matrix heat exchanger 24 in which it is cooled by a stream of waste nitrogen in line 25 and a stream of product oxygen in line 26. The cooled air stream is then fed into rectification column 27 from the bottom of which product oxygen is taken and from the top of which waste nitrogen is taken.
The stream of waste nitrogen in line 25 is fed to either bed 14 or 15, which at the time being is closed to the air inlet feed, to regenerate the adsorbent in that bed. The pressure of the air stream fed through beds 14 and 15 is of the order of 6 atmospheres whereas the pressure of the waste nitrogen stream is of the order of 1.1 atmospheres so that regeneration is a combination of a pressure swing and purging action. Adsorp tion and regeneration take place at substantially the same pressure, there being no means to vary by a substantial amount the temperature of the adsorbent beds. An initial portion of the effluent gas obtained from bed 14 or 15 being purged is fed through valved line 28 to a collection tank 29. The remainder of the effluent during purging is fed to waste through valved line 30. At the end of a purging operation the bed which has just been purged is repressurised with gas passed from tank 29 through valved line 32 or 31. The bed is then ready for a further feeding (adsorption) step.
It is believed that the quantity of waste nitrogen required for purging is of the order of 25% of the volume of the feed air and is therefore considerably less than that required to clean a reversing heat exchanger so that the amount of product quality gas is that much greater. Furthermore greater flexibility is given by adopting a process and apparatus in accordance with the invention particularly in the balance of heat exchange rates along the length of the heat exchanger 24 in comparison with the requirements of a reversing heat exchanger where various expedients such as splitting the feed air into two streams and feeding back a portion to an intermediate location in the height of the heat exchanger are often required in order to achieve heat exchange rates throughout the height of the heat exchanger which enable the required condensation of the water and carbon dioxide in the heat exchanger to be achieved.
WHAT WE CLAIM IS: 1. A process for separating a gaseous mixture comprising the steps of feeding the mixture through an adsorbent bed to remove by adsorption one or more components of the mixture, cooling and rectifying the unadsorbed gas to produce a product relatively rich in a desired component of the gaseous mixture and a waste gas relatively lean in the desired component and regenerating the adsorbent bed by purging it with a stream of the waste gas, the steps of adsorption and regeneration being performed at substantialy the same temperature.
2. A process according to claim 1 wherein the gaseous mixture is air.
3. A process according to claim 2 wherein the adsorbent bed is adapted to remove water and carbon dioxide from the air.
4. A process according to claim 3 wherein said adsorbent bed or a further adsorbent bed is adapted to remove acetylene from the air.
5. A process according to any one of
**WARNING** end of DESC field may overlap start of CLMS **.

Claims (18)

**WARNING** start of CLMS field may overlap end of DESC **. receive an initial portion of the effluent gas from a bed being purged, the gas in such reservoir being used to repressurise the absorbent bed(s) after regeneration thereof. In the case of air separation, traces of oxygen and nitrogen will remain in the interstitial volume of an adsorbent bed after a feed of air therethrough so that the initial effluent obtained from the bed during purging will be rich in such gases. This initial effluent may be stored and used for repressurising the bed(s) after regeneration to bring them up to pressure for another feed step. The unadsorbed gas is preferably cooled prior to rectification by heat exchange with the stream of waste gas and/or a stream or streams of product gas obtained from the rectification step. Such heat exchange may conveniently take place in an ordinary (non-reversing) matrix heat exchanger. Cooling and rectification can be more effective in a cryogenic system if the stream of unadsorbed gas is at an elevated pressure before it is fed to the rectification column. The inlet air fed to the adsorbent bed(s) is therefore preferably compressed so that the enriched stream of gas leaving the adsorption unit will be at an elevated pressure. A preferred embodiment of an air separation plant according to the invention will now be more particularly described by way of example and with reference to the accompanying diagrammatic drawing of such a plant. Referring to the drawing a compressor 10 draws in air through line 11 and delivers compressed air through line 12 to an adsorption unit 13. The adsorption unit comprises two beds 14 and 15 containing adsorbents which preferentially adsorb water and carbon dioxide from the air and possibly further adsorbents which preferentially adsorb e.g. acetylene. The air is fed into one or other of the beds 14 or 15. The unadsorbed gas from the bed 14 or 15 is delivered into an outlet line 18 through valved line 19 or 20. This unadsorbed gas (from which carbon dioxide, water and possibly other constituents, such as acetylene, have been removed) is then passed via a pipeline 18 through a matrix heat exchanger 24 in which it is cooled by a stream of waste nitrogen in line 25 and a stream of product oxygen in line 26. The cooled air stream is then fed into rectification column 27 from the bottom of which product oxygen is taken and from the top of which waste nitrogen is taken. The stream of waste nitrogen in line 25 is fed to either bed 14 or 15, which at the time being is closed to the air inlet feed, to regenerate the adsorbent in that bed. The pressure of the air stream fed through beds 14 and 15 is of the order of 6 atmospheres whereas the pressure of the waste nitrogen stream is of the order of 1.1 atmospheres so that regeneration is a combination of a pressure swing and purging action. Adsorp tion and regeneration take place at substantially the same pressure, there being no means to vary by a substantial amount the temperature of the adsorbent beds. An initial portion of the effluent gas obtained from bed 14 or 15 being purged is fed through valved line 28 to a collection tank 29. The remainder of the effluent during purging is fed to waste through valved line 30. At the end of a purging operation the bed which has just been purged is repressurised with gas passed from tank 29 through valved line 32 or 31. The bed is then ready for a further feeding (adsorption) step. It is believed that the quantity of waste nitrogen required for purging is of the order of 25% of the volume of the feed air and is therefore considerably less than that required to clean a reversing heat exchanger so that the amount of product quality gas is that much greater. Furthermore greater flexibility is given by adopting a process and apparatus in accordance with the invention particularly in the balance of heat exchange rates along the length of the heat exchanger 24 in comparison with the requirements of a reversing heat exchanger where various expedients such as splitting the feed air into two streams and feeding back a portion to an intermediate location in the height of the heat exchanger are often required in order to achieve heat exchange rates throughout the height of the heat exchanger which enable the required condensation of the water and carbon dioxide in the heat exchanger to be achieved. WHAT WE CLAIM IS:
1. A process for separating a gaseous mixture comprising the steps of feeding the mixture through an adsorbent bed to remove by adsorption one or more components of the mixture, cooling and rectifying the unadsorbed gas to produce a product relatively rich in a desired component of the gaseous mixture and a waste gas relatively lean in the desired component and regenerating the adsorbent bed by purging it with a stream of the waste gas, the steps of adsorption and regeneration being performed at substantialy the same temperature.
2. A process according to claim 1 wherein the gaseous mixture is air.
3. A process according to claim 2 wherein the adsorbent bed is adapted to remove water and carbon dioxide from the air.
4. A process according to claim 3 wherein said adsorbent bed or a further adsorbent bed is adapted to remove acetylene from the air.
5. A process according to any one of
claims 2 to 4 wherein said waste gas is nitrogen.
6. A process according to any preceding claim wherein an initial portion of the effluent gas obtained from said adsorbent bed during the regeneration thereof is supplied to a reservoir and wherein gas from said reservoir is used to repressurise the bed after regeneration thereof.
7. A process according to any preceding claim wherein the unadsorbed gas is cooled prior to rectification by heat exchange with a stream of gas obtained from the rectification of a preceding portion of the enriched mixture.
8. A process according to any preceding claim wherein the gaseous mixture is compressed prior to being fed through said adsorbent bed.
9. A process according to any preceding claim wherein a plurality of said adsorbent beds are employed and wherein said steps of feeding and regenerating for each bed are sequenced such that a substantially continuous supply of said enriched mixture is obtained from the beds.
10. A process for separating a gaseous mixture substantially as hereinbefore described with respect to the accompanying drawing.
11.A gas separation plant for performing the process of claim 1 comprising an adsorbent bed adapted to remove by adsorption ole or more components of a gaseous mixture fed therethrough, means for cooling and rectifying the unadsorbed gas to produce a product relatively rich in a desired component of the gaseous mixture and a waste gas relatively lean in the desired component and means for regenerating the adsorbent bed by purging the bed with a stream of the waste gas, there being no means substantially for varying the temperature of the bed.
12. A plant according to claim 11 for the separation of air wherein the adsorbent bed contains an adsorbent which preferentially adsorbs water and carbon dioxide from air.
13. A plant according to claim 12 wherein said adsorbent bed or a further adsorbent bed contains an adsorbent which preferentially adsorbs acetylene from air.
14. A plant according to any one of claims 11 to 13 comprising a reservoir, means for supplying to said reservoir an initial portion of the effluent gas obtained from said adsorbent bed during the regeneration thereof, and means for supplying gas from said reservoir to said adsorbent bed to repressurise the bed after regeneration thereof.
15. .A plant according to any one of claims 11 to 14 comprising a heat exchanger, means for directing the unadsorbed gas through said heat exchanger, and means for directing a stream of gas obtained from the rectification of a preceding portion of the unadsorbed gas through said heat exchanger, whereby the unadsorbed gas can be cooled prior to rectification by heat exchange with said stream.
16. Plant according to any one of claims 11 to 15 comprising means for compressing the gaseous mixture prior to being fed through said adsorbent bed.
17. Plant according to anyone of claims 11 to 16 comprising a plurality of said adsorbent beds and means whereby said steps of feeding and regenerating for each bed can be sequenced such that a substantially continuous supply of said enriched mixture is obtained from the beds.
18. A gas separation plant substantially as hereinbefore described with reference to the accompanying drawing.
GB35176/76A 1976-08-24 1976-08-24 Separation of gaseous mixtures Expired GB1586961A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
GB35176/76A GB1586961A (en) 1976-08-24 1976-08-24 Separation of gaseous mixtures
ZA00774932A ZA774932B (en) 1976-08-24 1977-08-15 Separation of gaseous mixtures
BR7705591A BR7705591A (en) 1976-08-24 1977-08-22 PROCESS TO SEPARATE A GAS MIXTURE AND INSTALLATION FOR GAS SEPARATION
ES461831A ES461831A1 (en) 1976-08-24 1977-08-23 Separation of gaseous mixtures
JP10100577A JPS5342182A (en) 1976-08-24 1977-08-23 Method of separating gas mixture
FR7725845A FR2363069A1 (en) 1976-08-24 1977-08-24 PROCESS AND INSTALLATION FOR SEPARATING THE COMPONENTS OF A GAS MIXTURE
AU28177/77A AU509650B2 (en) 1976-08-24 1977-10-24 Separation of gaseous mixtures

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB35176/76A GB1586961A (en) 1976-08-24 1976-08-24 Separation of gaseous mixtures

Publications (1)

Publication Number Publication Date
GB1586961A true GB1586961A (en) 1981-03-25

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GB35176/76A Expired GB1586961A (en) 1976-08-24 1976-08-24 Separation of gaseous mixtures

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JP (1) JPS5342182A (en)
AU (1) AU509650B2 (en)
BR (1) BR7705591A (en)
ES (1) ES461831A1 (en)
FR (1) FR2363069A1 (en)
GB (1) GB1586961A (en)
ZA (1) ZA774932B (en)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5090973A (en) * 1990-10-23 1992-02-25 The Boc Group, Inc. Psa employing high purity purging
US5137548A (en) * 1990-05-09 1992-08-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for purifying air to be distilled by adsorption
US5666828A (en) * 1996-06-26 1997-09-16 Praxair Technology, Inc. Cryogenic hybrid system for producing low purity oxygen and high purity oxygen
US5779767A (en) * 1997-03-07 1998-07-14 Air Products And Chemicals, Inc. Use of zeolites and alumina in adsorption processes
US5919286A (en) * 1997-03-06 1999-07-06 Air Products And Chemicals, Inc. PSA process for removel of nitrogen oxides from gas
US6391092B1 (en) 1999-10-12 2002-05-21 The Boc Group, Inc. Thermal swing adsorption process for the removal of dinitrogen oxide, hydrocarbons and other trace impurities from air

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5527034A (en) * 1978-08-16 1980-02-26 Hitachi Ltd Pressure swing adsorption system used with heat regeneration method
US4264340A (en) * 1979-02-28 1981-04-28 Air Products And Chemicals, Inc. Vacuum swing adsorption for air fractionation
US4340398A (en) * 1981-05-20 1982-07-20 Union Carbide Corporation Pressure swing adsorption recovery
JPS5880485A (en) * 1981-11-06 1983-05-14 株式会社日立製作所 Preparatory pressing method for cushion tank
JPS5983906A (en) * 1982-11-02 1984-05-15 Kawasaki Heavy Ind Ltd Method for purifying hydrogen gas using metallic hydride
JPS59186627A (en) * 1984-03-30 1984-10-23 Hitachi Ltd Pretreating device of low temperature air separator
FR2690633A1 (en) * 1992-04-30 1993-11-05 Air Liquide High pressure air distillation installation - allowing the recovery of a substantial part of the air usually lost during regeneration of the adsorbent
FR2970184B1 (en) 2011-01-07 2013-08-02 Air Liquide ZEOLITIC COMPOSITION SUITABLE FOR AIR CLEANING

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5137548A (en) * 1990-05-09 1992-08-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for purifying air to be distilled by adsorption
AU643007B2 (en) * 1990-05-09 1993-11-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for purifying air to be distilled by absorption
US5090973A (en) * 1990-10-23 1992-02-25 The Boc Group, Inc. Psa employing high purity purging
EP0482863A1 (en) * 1990-10-23 1992-04-29 The Boc Group, Inc. PSA Employing high purity purging
AU654677B2 (en) * 1990-10-23 1994-11-17 Boc Group, Inc., The PSA employing high purity purging
US5666828A (en) * 1996-06-26 1997-09-16 Praxair Technology, Inc. Cryogenic hybrid system for producing low purity oxygen and high purity oxygen
US5919286A (en) * 1997-03-06 1999-07-06 Air Products And Chemicals, Inc. PSA process for removel of nitrogen oxides from gas
US5779767A (en) * 1997-03-07 1998-07-14 Air Products And Chemicals, Inc. Use of zeolites and alumina in adsorption processes
US6391092B1 (en) 1999-10-12 2002-05-21 The Boc Group, Inc. Thermal swing adsorption process for the removal of dinitrogen oxide, hydrocarbons and other trace impurities from air

Also Published As

Publication number Publication date
FR2363069B3 (en) 1980-06-06
AU509650B2 (en) 1980-05-22
BR7705591A (en) 1978-06-06
ZA774932B (en) 1978-06-28
ES461831A1 (en) 1978-05-16
FR2363069A1 (en) 1978-03-24
JPS5342182A (en) 1978-04-17
AU2817777A (en) 1979-03-01

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