WO2009064169A2 - Système compact d'adsorption modulée en pression pour l'épuration d'hydrogène - Google Patents

Système compact d'adsorption modulée en pression pour l'épuration d'hydrogène Download PDF

Info

Publication number
WO2009064169A2
WO2009064169A2 PCT/MY2009/000005 MY2009000005W WO2009064169A2 WO 2009064169 A2 WO2009064169 A2 WO 2009064169A2 MY 2009000005 W MY2009000005 W MY 2009000005W WO 2009064169 A2 WO2009064169 A2 WO 2009064169A2
Authority
WO
WIPO (PCT)
Prior art keywords
gas
cell
adsorption
hydrogen
cells
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
PCT/MY2009/000005
Other languages
English (en)
Other versions
WO2009064169A3 (fr
Inventor
Wan Ramli Wan Daud
Abdul Wahab Mohammad
Edy Herianto Majlan
Abu Baker Mohammad
Abdul Amir Hassan Khadum
Mohd Sobri Takriff
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.)
National University of Malaysia
Original Assignee
National University of Malaysia
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 National University of Malaysia filed Critical National University of Malaysia
Publication of WO2009064169A2 publication Critical patent/WO2009064169A2/fr
Publication of WO2009064169A3 publication Critical patent/WO2009064169A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • B01D2253/102—Carbon
    • 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
    • B01D2253/106—Silica or silicates
    • 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
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • 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
    • B01D2256/16—Hydrogen
    • 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
    • B01D2257/502—Carbon monoxide
    • 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
    • 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
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/40062—Four
    • 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
    • B01D2259/404—Further details for adsorption processes and devices using four beds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a compact pressure swing adsorption (CPSA) system for gas separation and purification.
  • CPSA compact pressure swing adsorption
  • the present invention relates to a CPSA system for hydrogen purification which is operated in four cells of adsorption chambers together independently and a process of CPSA thereof for obtaining a highly purified hydrogen gas to be used as fuel in the polymer electrolyte membrane fuel cell (PEMFC).
  • PEMFC polymer electrolyte membrane fuel cell
  • Fuel cells are electrochemical devices that convert chemical energy of a reaction into electrical energy.
  • PEMFC is the most likely alternative to the internal combustion engine as the power generating system for the 21 st century.
  • Hydrogen gas which is usually produced by steam reforming of fossil fuels has become the fuel of choice for PEMFC.
  • Carbon monoxide which is a by-product of the steam reforming of hydrogen production will affect the performance of PEMFC since carbon monoxide in a concentration of higher than lOppm poisons the platinum catalyst in the membrane- electrode-assembly (MEA).
  • MEA membrane- electrode-assembly
  • Hydrogen gas is widely produced for chemical and industrial purposes by hydrogenation, saturation and methanol in a reforming process to produce a synthesis gas.
  • Pressure swing adsorption is known to be one of the most economic processes for gas separation and purification.
  • the hydrogen gas stream is passed to a separation zone comprising a PSA system to produce a high purity hydrogen stream and a separation waste stream comprising carbon monoxide.
  • the PSA system can be designed to achieve up to 99.9999% of hydrogen purity and 55% to 95% of hydrogen recovery.
  • Conventional PSA system employs two adsorption column that are used and regenerated alternatively.
  • the capacity of the PSA is limited by the switching time between the two columns.
  • PSA has a high turndown ratio and can maintain both recovery and product purity by automatically adjusting cycle times.
  • This invention provides a system to purify hydrogen by using a hydride compressor and catalytic converters combined with a process controller.
  • the invention includes a step of converting carbon monoxide contained within the impure hydrogen to methane.
  • a series of check valves and solenoid valves are activated which allows venting the contaminants contained within the hydrogen stream.
  • Some of the prior arts also relates to a PSA system or process.
  • a PSA for fuel cell application described in the U. S. Patent No. US2005098034.
  • This invention discloses a system that includes a series of nine vessels housing an adsorbent or combination of adsorbents that adsorb carbon monoxide, carbon dioxide, nitrogen, water and methane in the feed gas such as a reformate gas.
  • This invention utilizes a wide range of materials as adsorbent beds.
  • this invention provides a much less stringent purity requirement of the hydrogen output.
  • Another U. S. Patent No. US2004179998 also discloses a fuel processor module for hydrogen production and purification using PSA system.
  • the system comprises a primary reactor that generates hydrogen from a hydrocarbon fuel to obtain a reformate gas containing hydrogen and other by-product; and an adsorber device for receiving the reformate gas from the primary reactor to generate a nearly pure hydrogen.
  • this invention requires heat to combust and vaporize during the reforming process.
  • PSA is a hydrogen production system which can produce a highly pure hydrogen stream and a separation waste stream comprising carbon monoxide
  • the primary object of the present invention is to design a CPSA system for hydrogen gas purification which incorporates a plurality of adsorption cells hashed in a cylindrical adsorption chamber of CPSA.
  • Another object of the present invention is to provide a CPSA system for hydrogen purification whereby the series of pressurization, adsorption, depressurization and purging step of a CPSA is run independently in the adsorption chamber.
  • Still another object of the present invention is to design a CPSA system which is capable of reducing the carbon monoxide concentration in hydrogen stream from 4000ppm to below lOppm.
  • Further object of the present invention is to design a flexible CPSA system wherein the valves and the process cycles can be controlled manually or automatically.
  • one of the preceding objects is met, in whole or in part, by the present invention, in which one of the embodiments of the present invention describes a CPSA system for gas separation and purification, comprising an absorption chamber, means for pressurizing the adsorption chamber with a gas stream (60) fed by an inputting means; means for adsorbing impurity gas (58) from the gas stream (60) and conveying purified gas (56) to an outputting means; means for depressurizing the adsorption chamber to regenerate absorbed impurity gas (58); and means for purging any remaining adsorbed impurity gas (58) by a purge gas (55); wherein the adsorption chamber comprises a plurality of separate cells, each cell having adsorbent bed (51, 52, 53, 54), and the inputting and outputting means are connected to each cell with means for switching between the cells so that only one cell at a time is connected to the inputting means and another cell is connected to the outputting means, by a network of pipes and valve
  • Another preferred embodiment of the present invention is a CPSA system for gas separation and purification further comprising a computer programed to regulate, manipulate and record keeping the system.
  • the invention discloses a process of CPSA for gas separation and purification comprising: a) pressurizing a cell of an adsorption chamber with a gas stream (60) fed by an inputting means; b) adsorbing impurity gas (58) from the gas stream (60) into an adsorbent bed (51, 52, 53, 54) of the cell to give purified gas (56) at an outputting means; c) depressurizing the cell to regenerate adsorbed impurity gas (58); and d) purging any remaining adsorbed impurity gas (58) by a purge gas (55) to cleanse the absorbent bed (51); wherein the series of pressurizing, adsorbing, depressurizing and purging steps is run independently in any cells of the adsorption chamber which comprises a plurality of similar cells that are operated simultaneously.
  • the process of CPSA for gas separation and purification is run in a double adsorption approach whereby the gas (56) obtained from the outputting means from a first cell serves as the gas stream (60) for a second cell to be doubly purified therein.
  • Figure 1 is a schematic diagrame for a CPSA system with four cells in an absorption chamber.
  • the present invention relates to a compact pressure swing adsorption (CPSA) system for gas separation and purification.
  • CPSA compact pressure swing adsorption
  • the present invention relates to a CPSA system for hydrogen purification which is operated in four cells of adsorption chambers together independently and a process of CPSA thereof for obtaining a highly purified hydrogen gas to be used as fuel in the polymer electrolyte membrane fuel cell (PEMFC).
  • PEMFC polymer electrolyte membrane fuel cell
  • the present invention discloses a compact pressure swing adsorption system for gas separation and purification, comprising an absorption chamber, means for pressurizing the adsorption chamber with a gas stream (60) fed by an inputting means; means for adsorbing impurity gas (58) from the gas stream (60) and conveying purified gas (56) to an outputting means; means for depressurizing the adsorption chamber to regenerate absorbed impurity gas (58); and means for purging any remaining adsorbed impurity gas (58) by a purge gas (55); wherein the adsorption chamber comprises a plurality of separate cells, each cell having adsorbent bed (51, 52, 53, 54), and the inputting and outputting means are connected to each cell with means for switching between the cells so that only one cell at a time is connected to the inputting means and another cell is connected to the outputting means, by a network of pipes and valves (57).
  • the CPSA invented is identified as the most economic system for hydrogen gas separation and purification which is capable of obtaining a hydrogen stream with a purity of up to 99.9999%, and the hydrogen recovery of 50% to 95%.
  • This CPSA system is especially designed for the purification of hydrogen produced from autothermal steam reforming of fossil fuels, such as methanol.
  • the CPSA system comprises an inputting means which is a feed manifold for inputting a gas stream (60).
  • the gas stream (60) is usually a mixture of a gas to be purified which is contaminated with other impurity gases (58).
  • this gas stream (60) is a hydrogen-rich reformate which is an effluent gas mixture obtained from the autothermal steam reforming process.
  • This effluent gas mixture can be a gas mixture of hydrogen and carbon monoxide, a gas mixture of hydrogen and carbon dioxide, or a gas mixture of hydrogen, carbon monoxide and carbon dioxide.
  • the cylindrical absorption chamber of the preferred embodiment the cylindrical absorption chamber of the preferred embodiment
  • CPSA is divided into four separate cells each having an adsorbent bed (51, 52, 53,
  • each of the four adsorption cells can be means for pressurizing a cell of the adsorption chamber with a gas stream (60) fed by an inputting means; means for adsorbing impurity gas (58) from the gas stream (60) and conveying purified gas (56) to an outputting means; means for depressurizing the cell to regenerate absorbed impurity gas (58); and means for purging any remaining adsorbed impurity gas (58) by a purge gas (55).
  • all four steps of a PSA cycle process can be run independently in these cells and all cells can be operated simultaneously whereas those steps are run intermittently on alternate adsorbers in a conventional PSA.
  • CPSA Since the design of CPSA is based on the velocity effects, regeneration purge, adsorbent bed size and the choice of the adsorbent, these four factors are important in determining the efficiency of the CPSA.
  • the gas stream flows through tortuous interstitial passages between the granules in adsorbent bed (51, 52, 53, 54) resulting in viscous and kinetic energy losses that create pressure gradient within the bed.
  • the gas separation by CPSA process depends on retaining both the mass-transfer and heat- transfer fronts within the adsorbent bed (51, 52, 53, 54), therefore, the bed length is determined by the retention of the mass-transfer front if the impurity gas (58) or contaminants are noncondensables.
  • the adsorbent bed (51, 52, 53, 54) that will be used shall possess high selectivity for carbon monoxide so that it can be adsorbed from the hydrogen stream efficiently.
  • a lot of materials can be used as the absorbent bed (51, 52, 53, 54) for adsorbing impurity gas (58) in the adsorption chambers since the selectivity for most impurity gas (58) is higher than that for hydrogen.
  • the impurity gas (58) are contaminants in the gas stream (60), which includes carbon monoxide, carbon dioxide, nitrogen or a combination of any two or more thereof.
  • the adsorbent bed is a porous medium having a certain size.
  • suitable materials to be used as the adsorbent bed (51, 52, 53, 54) include activated carbon, zeolite, silica gel or a composite containing any two or more thereof.
  • the adsorbent bed (51, 52, 53, 54) used is activated carbon.
  • Activated carbon with a surface area of 695.07 m2/g has a carbon monoxide absorption capacity of 0.548mmol/g and carbon dioxide absorption capacity of 2.045mmol/g at standard temperature and pressure (STP).
  • the purified gas (56) can be obtained from an outputting means which is the product manifold. According to the preferred embodiment of the present invention, this purified gas (56) is a gas stream of pure hydrogen up to 99.9999% purity. It is suitable to be used as fuel for most applications especially for the use in the PEMFC. Concentration of carbon monoxide in the purified hydrogen stream will be reduced from 4000ppm to less than lOppm. In accordance with the preferred embodiment, the concentration of carbon monoxide in the purified gas (56) of the present invention is usually as low as lppm.
  • a purge gas (55) is also used in the CPSA system of the present invention.
  • this purge gas (55) is preferably hydrogen gas.
  • the hydrogen used as purge gas (55) is a part of the purified gas (56) from the cells of adsorption chamber.
  • the purge generation is controlled by purge flow. Purge flow conveys the heat of adsorption into contaminant region of the adsorbent bed (51, 52, 53, 54) and sweeps away the adsorbed contaminants or impurity gases out of the CPSA system during the regeneration process.
  • a CPSA system for gas separation and purification further comprises a pressure transducer, a thermocouple, a pressure indicator and a flowmeter associated with the cells of adsorption chamber.
  • the pressure transducer is capable of measuring the pressure of the system.
  • 5 pressure transducers are equiped in the CPSA system.
  • the pressure in each cell is indicated by the 4 pressure indicators, respectively.
  • the thermocouple is used as a temperature sensor for the CPSA system of the present invention.
  • the CPSA system is supplied with 16 thermocouples, 4 at each adsorbent bed, respectively.
  • the thermocouples are located equidistant from each other on each bed. There are 3 flowmeters showing flow rate of the feed gas stream, flow rate of the product and flow rate of purge gas, respectively.
  • Another preferred embodiment of the present invention is a CPSA system for gas separation and purification further comprising a computer programed to regulate, manipulate and record keeping the system. Therefore, this system can be operated manually or automatically.
  • the invention discloses a a process of compact pressure swing adsorption for gas separation and purification comprising: a) pressurizing a cell of an adsorption chamber with a gas stream (60) fed by an inputting means; b) adsorbing impurity gas (58) from the gas stream (60) into an adsorbent bed (51, 52, 53, 54) of the cell to give purified gas (56) at an outputting means; c) depressurizing the cell to regenerate adsorbed impurity gas (58); and d) purging any remaining adsorbed impurity gas (58) by a purge gas (55) to cleanse the absorbent bed (51); wherein the series of pressurizing, adsorbing, depressurizing and purging steps is run independently in any cells of the adsorption chamber which comprises a plurality of similar cells that are operated simultaneously.
  • the CPSA system can be run in a single adsorption approach or a double adsorption approach.
  • the adsorption cells are used one by another.
  • the adsorption process is performed by only one adsorbent bed at a time whereas the rest of the adsorbent beds are in other steps of the CPSA cycle.
  • Adsorption will occur in the second adsorption cell merely after the saturation of the first adsorption chamber.
  • the CPSA cycle is initiated by feeding an adsorption chamber with a gas stream (60).
  • the gas stream (60) is preferably a hydrogen- rich reformate obtained from the autothermal steam reforming process of fossil fuels.
  • the pressurization of the adsorption cell is achieved by the feeding of gas stream (60) via the inputting means.
  • the bottom valve for the first adsorption cell is opened while closing its top valve to pressurize the first adsorption cell.
  • the adsorbent bed (51) can be any porous medium with a high selectivity for impurity gases, such as carbon monoxide and carbon dioxide.
  • the most preferred type of material to be used as adsorbent bed (51, 52, 53, 54) in the present invention is activated carbon which has high affinity for carbon monoxide and carbon dioxide. According to the preferred embodiment of the present invention, the adsorption process is ceased in the first cell when the adsorbent bed
  • the saturation stage can be identified by the concentration of the adsorbed impurity gas (58) which reaches a certain threshold.
  • a depressurizing step is performed by opening the top valve of the first absorption cell while closing its bottom valve. Due to the difference between the internal and external pressure of the absorption cell, gas flows out from the cell immediately. During the depressurization process, the absorbed impurity gas (58), such as carbon monoxide and carbon dioxide, will flow out together with the effluent.
  • the absorbed impurity gas (58) such as carbon monoxide and carbon dioxide
  • a purge gas (55) is employed so as to remove any remaining adsorbed impurity gas from the adsorbent bed.
  • the purge gas is channeled into the adsorption cell countercurrently, whereby it flows into the adsorption cell from the top valve and carries the remaining absorbed impurity gas (58) out of the adsorption chamber at the bottom valve.
  • the purge gas (55) is preferably hydrogen gas which is a part of the purified gas (56) from the absorption cells.
  • the four adsorption cells as embodied by the present invention are operated simultaneously with the four steps of CPSA cycle run independently in each cell.
  • the purified hydrogen gas usually contains merely lppm of carbon monoxide.
  • the process of CPSA for gas separation and purification is run in a double adsorption approach whereby the gas (56) obtained from the outputting means of the first absorption cell serves as the gas stream (60) for a second absorption cell to be doubly purified therein.
  • the gas stream to be purified will enter 2 adsorption chambers in series before exiting the CPSA system as a doubly purified product.
  • the gas stream (60) is first channeled into the first absorption cell.
  • the impurity gas (58) is absorbed from the gas stream (60) in this absorption cell and a stream of purified gas (56) will be produced.
  • This purified gas (56) is then channeled into the second absorption cell from its inputting means as a gas stream (60) for the second adsorption cell. Therefore, the purified gas (56) flows out from the second adsorption cell will be a product of the double adsorption approach.
  • the pressurization process is performed in the third absorption chamber. All the CPSA processes are run independently in these four absorption cells and all cells can be run simultaneously.
  • the CPSA system invented by the present invention is preferably to be used for hydrogen purification. Besides, it is also applicable for volatile organic compounds removal, air purification, nitrogen or oxygen separation from air, landfill gas separation, gas drying and others.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un système compact d'adsorption modulée en pression pour la séparation et l'épuration de gaz, comportant une chambre d'adsorption, un moyen de mise sous pression de la chambre d'adsorption avec un flux gazeux (60) alimenté par un moyen d'admission ; un moyen pour adsorber d'impuretés gazeuses (58) depuis le flux gazeux (60) et pour transporter le gaz purifié (56) vers un moyen d'évacuation; un moyen de dépressurisation de la chambre d'adsorption pour régénérer les impuretés gazeuses adsorbées (58) ; et un moyen pour purger toute impureté gazeuse adsorbée restante (58) par un gaz de purge (55). La chambre d'adsorption comporte une pluralité de cellules séparées, chaque cellule comprenant un lit adsorbant (51, 52, 53, 54), et les moyens d'entrée et d'évacuation sont reliés à chaque cellule avec des moyens pour une commutation entre les cellules de sorte qu'une seule cellule soit reliée au moyen d'admission et une autre cellule soit reliée au moyen d'évacuation à la fois, par un réseau de conduites et de soupapes.
PCT/MY2009/000005 2007-11-16 2009-01-02 Système compact d'adsorption modulée en pression pour l'épuration d'hydrogène Ceased WO2009064169A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
MYPI20072029 2007-11-16
MYPI20072029A MY171684A (en) 2007-11-16 2007-11-16 Compact pressure swing adsorption system for hydrogen purification

Publications (2)

Publication Number Publication Date
WO2009064169A2 true WO2009064169A2 (fr) 2009-05-22
WO2009064169A3 WO2009064169A3 (fr) 2009-10-22

Family

ID=40639343

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/MY2009/000005 Ceased WO2009064169A2 (fr) 2007-11-16 2009-01-02 Système compact d'adsorption modulée en pression pour l'épuration d'hydrogène

Country Status (2)

Country Link
MY (1) MY171684A (fr)
WO (1) WO2009064169A2 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012010292A1 (de) * 2012-05-21 2013-11-21 promakon gmbh Druckluft-Zerlegungseinrichtung zur Herstellung eines Verbrauchergases mittels Adsorbtion für industrielle, gewerbliche oder private Anwendungen und Verfahren zum Zerlegen von Druckluft in ein Verbrauchergas durch Adsorbtion ebenfalls für die genannten An
WO2014182376A1 (fr) * 2013-05-08 2014-11-13 Linde Aktiengesellschaft Procédé de production d'hydrogène avec récupération de dioxyde de carbone
CN115608080A (zh) * 2022-10-31 2023-01-17 中科富海(中山)低温装备制造有限公司 一种提高氢气浓度分级除杂的氢气纯化装置

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3346032A1 (de) * 1983-12-20 1985-06-20 Linde Ag, 6200 Wiesbaden Druckwechseladsorptionsverfahren
US4761165A (en) * 1987-09-01 1988-08-02 Union Carbide Corporation Pressure swing adsorption control method and apparatus
US5827358A (en) * 1996-11-08 1998-10-27 Impact Mst, Incorporation Rapid cycle pressure swing adsorption oxygen concentration method and apparatus
US6454838B1 (en) * 2000-06-21 2002-09-24 Air Products And Chemicals, Inc. Six bed pressure swing adsorption process with four steps of pressure equalization
CA2320551C (fr) * 2000-09-25 2005-12-13 Questair Technologies Inc. Petit appareil d'adsorption modulee en pression

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012010292A1 (de) * 2012-05-21 2013-11-21 promakon gmbh Druckluft-Zerlegungseinrichtung zur Herstellung eines Verbrauchergases mittels Adsorbtion für industrielle, gewerbliche oder private Anwendungen und Verfahren zum Zerlegen von Druckluft in ein Verbrauchergas durch Adsorbtion ebenfalls für die genannten An
WO2014182376A1 (fr) * 2013-05-08 2014-11-13 Linde Aktiengesellschaft Procédé de production d'hydrogène avec récupération de dioxyde de carbone
CN115608080A (zh) * 2022-10-31 2023-01-17 中科富海(中山)低温装备制造有限公司 一种提高氢气浓度分级除杂的氢气纯化装置

Also Published As

Publication number Publication date
WO2009064169A3 (fr) 2009-10-22
MY171684A (en) 2019-10-23

Similar Documents

Publication Publication Date Title
US20240382896A1 (en) Ammonia Cracking for Green Hydrogen
US7763086B2 (en) Hydrogen purification process and system
US7892328B2 (en) PSA apparatus for producing high-purity hydrogen gas
US6770390B2 (en) Carbon monoxide/water removal from fuel cell feed gas
US20050098034A1 (en) Hydrogen purification process using pressure swing adsorption for fuel cell applications
JP2004512650A5 (fr)
Harale et al. Experimental studies of a hybrid adsorbent-membrane reactor (HAMR) system for hydrogen production
US7276095B2 (en) Fuel processor module for hydrogen production for a fuel cell engine using pressure swing adsorption
JP5743215B2 (ja) ヘリウムガスの精製方法および精製装置
US20080299424A1 (en) Carbon monoxide clean-up in a pem fuel cell system
CN101582514B (zh) 用于燃料电池供氢的一步变压吸附纯化氢的装置
JP5748272B2 (ja) ヘリウムガスの精製方法および精製装置
WO2009064169A2 (fr) Système compact d'adsorption modulée en pression pour l'épuration d'hydrogène
JP4357756B2 (ja) メンブレンリフォーマによる高純度水素製造システム
AU2016201267B2 (en) A plant and process for simutaneous recovering multiple gas products from petrochemical offgas
JP2004075439A (ja) 水素製造装置
JP2017222557A (ja) 水素ガス製造方法及び水素ガス製造装置
JP4041085B2 (ja) 燃料ガス製造システム及びその停止方法
JP3867082B2 (ja) 家庭用燃料ガス製造装置の停止方法
JP2018150209A (ja) 水素供給システム
JP4139338B2 (ja) 燃料ガス製造装置
CN102807199B (zh) 氩气的提纯方法及提纯装置
JP5270215B2 (ja) 燃料電池システム
JP4357979B2 (ja) 燃料ガス製造装置の始動方法
JP2007254229A (ja) 水素製造方法および水素製造装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09700034

Country of ref document: EP

Kind code of ref document: A2

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 09700034

Country of ref document: EP

Kind code of ref document: A2