CA2081170C - Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen - Google Patents
Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen Download PDFInfo
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- CA2081170C CA2081170C CA002081170A CA2081170A CA2081170C CA 2081170 C CA2081170 C CA 2081170C CA 002081170 A CA002081170 A CA 002081170A CA 2081170 A CA2081170 A CA 2081170A CA 2081170 C CA2081170 C CA 2081170C
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
- B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2475—Membrane reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
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- 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
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/42—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles
- C01B3/44—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles using the fluidised bed technique
-
- 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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00123—Fingers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00292—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant solids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00628—Controlling the composition of the reactive mixture
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- 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
- C01B2203/0405—Purification by membrane separation
- C01B2203/041—In-situ membrane purification during hydrogen production
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- 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
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- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
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- 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
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S48/00—Gas: heating and illuminating
- Y10S48/05—Diffusion membrane for gas reaction or separation
Abstract
Hydrogen gas is generated in a fluidized bed reactor by reacting gases namely steam and a hydrocarbon gas such as methane or natural gas in a fluidized bed of particulate catalytic material. The catalytic material is fluidized by injecting the mixture of the reacting gases at the bottom of the bed.
Hydrogen generated within the bed is removed via a selectively permeable membrane that extends through the bed and through a freeboard area above the bed. The reaction is endothermic and therefore heat to maintain the bed at the desired temperature is added as required. preferably a separator separates particulate catalytic material entrained in the gases in the freeboard area and delivers the particulate material separated from the gas back into the bed.
Hydrogen generated within the bed is removed via a selectively permeable membrane that extends through the bed and through a freeboard area above the bed. The reaction is endothermic and therefore heat to maintain the bed at the desired temperature is added as required. preferably a separator separates particulate catalytic material entrained in the gases in the freeboard area and delivers the particulate material separated from the gas back into the bed.
Description
Fluidized Bed Reaction System for Steam/Hydmcarbon Gas Refomung to P~bduce Hydrogen Field of the Invention The present invention relates to an improved hydrogen forming reaction 5 system using a fluidized bed reactor.
Description of the Pvior An The production of hydrogen ming reaction systems employing steam and hydrocarbon gases such r~s methane or natural gas or the like are well known in the art. These reactions are generally catalytic and are limited by intra particle 10 diffusion and thermodynamic equilibrium Reactors employ;d for this purpose are normally fixed bed type reactors as opposed to fluidized bed reactors although lluidiLed bed reactors have been proposed for use in production of hydrogen in US Patent 3,524,819 issued Aug.
18 1970 to Guerneri and US patents 4,877,550 and 4,888,131 issued October 31 15 1989 and December 18 1989 respectively to Goeisch and . (See also U.S.
Patent 4,938,946 issued July 3, 199t> to Gibsoa, of al. which teaches fluidir~ng Regolith in particulate form 1.'or producing hydrogen gas at elevated temperature.) The addition of hwt to reformers 1z41s also been taught, for example, in US
Patent 3,524,819 to Guerrieri andlor Deutches Patent 3,331,:202 issued 1984 to 20 Reichel. Us patent 4,474,23t? issued Oci. 2 1984 to MeCallister teaches the use ofheat pipes to introduce heat into fluidized bed reactors.
The Goetsch patent 4,877,550 also teaches rapid cooling to overcome the negative effect of the catalyst fuzes entraiizrrrent which reduces the reaction conversion in the Ii~eeboard zone and subsequent process lines.
25 Generally in such steact~hydrocarlxm reaction systems, it is required that the hydrogen be separated using relatively complicated processes for increasing the purity of the hydrogen to that required for subsequent uses. It has also been proposed by Minet et al irr U.S Patent no. 4,981,676 issued January 1 1991 to use a diffusion process for steam relbrming of hydrocarbons in the production of 30 hydrogen, carbon monoxide and carbon dioxide by employing a generally tubular, porous, ceramic membrane and providing a heirted rm.ction ;cone in a container into which the membrane is received. The membrane carries the catalyst and the hydrocarbon gas and steam contact one side of ttze membrrne t.o produce the ~o~~~~o hydrogen, carbon monoxide and carbon dioxide gases. The hydrogen formed selectively diffuses through the membrane and is carried off in an entraining gas.
U.S. Patent 4,810,485 issued March 7, 1989 to Marianowski teaches the formation of hydrogen gas in a reaction zone containing a hydrogen ion porous metallic foil which conducts hydrogen ions therethrough to remove the hydrogen ions from the packed bed as they are' formed and thereby permit a reduction in the operating temperature of the bed and producing a relatively pure hydrogen that is conducted away through the tubular metallic foils to a manifold.
Brief Description ~f the Present Ynvention It is an object of the present invention to provide an improved reaction system employing a fluidized bed to react steam and hydrocarbon gas to produce hydrogen and to separate the hydrogen upon formation thereby to improve the reaction yield.
Broadly the present invention relates to a method and apparatus for producing hydrogen gas comprising forming a fluidized bed of a suitable particulate catalyst by introducing reacting gases comprising a mixture of steam and hydrocarbon gas into the bottom of said fluidized bed to fluidize said particles and form said fluidized bed, said fluidized 'bed occupying a portion of a vessel and forming a reaction zone; a freeboard zone in said vessel above said fluidized bed, reacting said reacting gases 'within said bed to produce hydrogen gas, separating said hydrogen gas as it is formed in said bed as molecular or atomic hydrogen through a perm selective membrane means that extends through said bed' in the direction of flow of said reaction gases and permits transfer of hydrogen therethrough while preventing the transmission of other gases present in said reaction zone therethrough, said hydrogen gas after permeation through the membrane providing a source of relatively pure hydrogen gas.
Preferably said membrane means will also extend through said freeboard zone and separate hydrogen froni said other gases in said freeboard zone.
In some embodiments said perm selective membrane means will comprise a plurality of tubes of perm selective membrane material arranged about said bed with the longitudinal axes of said tubes substantially parallel and extending in said direction of flow of said reaction gases.
2~~~.~~0 Preferably adjacent said perm selective tubes will be spaced at least sufficient to permit fluidizing of said catalyst particles therebetween yet sufficiently small to provide the desired surface area exposed to said reaction zone to permit the transfer of hydrogen generated in said reaction zone.
Preferably said perm selective membrane means will comprise a plurality of modules, each said modules being formed by a plurality of perm selective membrane tubes enclosed in a protective sheath of material that permits hydrogen and other gases to pass therethrough and into contact with said perm selective membrane tubes while prohibiting the passage of said particulate catalyst.
Preferably a pressure significantly lower than that in the reaction zone will be maintained in said perm selective membrane means to improve the permeation rate of hydrogen through. said perm selective meriibrane means.
Preferably, a heating means will be provided to supply heat needed in the reaction zone to maintain said fluidized bed at the desired.reaction temperature.
Preferably, said, other gases leaving said freeboard will be separated from particulate material and said particulate material will be redirected back into said fluidized bed.
Preferably, said separation will comprise centrifugally separating said particulate from said gases in centrifugal cleaner having a conical section having a particulate outlet at 'the small diameter end, said particulate outlet being submerged in said bed and a gas outlet from said base section at the major diameter end of said conical section for removal of cleaned gas from the system and a tangential gas inlet to said centrifugal cleaner adjacent to said gas outlet.
In soma cases it may be desirable to recycle selected amount of other gas evolving from said freeboard and introduce said other gas from said freeboard into said reaction zone with said reacting gasps to control fluidization of said fluidized bed.
l6rief Description of the lDrawings Further features, objects and advantages will be evident from the following detailed description of the preferred embodiments of the present invention taken in conjunction with the accompanying drawings in which:
Figure 1 is a schematic illustration of a fluidized bed reactor system ~t constructed in accordance with the presern invention.
Figure 2 is a section along the line 2 - 2 o f Figure 1.
Figure 3 is an enlarged cross section of a perm selective membrane module.
Figure 4 is a section on the line 4 - 4 of Figure 1 with parts omitted showing a modified arrangement of the perm selective membrane tubes within the fluidized bed reaction zone.
Figure 5 is an e,nla~~ged cross section showing the spacing between adjacent perm selective membrane tubes.
Description of the Pmfe~md Embodiments The reactor vessel 1t7 schematically illustrated in Figm-e 1 has two main sections; A fluidized bed section l2 ibrming a reaction -none 12 and a freeboard section or zone 14. A distributor plate 16 forms the bottom of the fluidized bed section 12 and connects the bottom of the fluidized bed 12 with the wind or blow box 18 which in turn is connected via gas inlet 20 to the sources of reacting gases such as methane and steam as indicated by the lines 22 and 24 respectively.
Preferably a preheater 23 will preheat the reacting gases before they enter the wind box 18.
The fluidized bed section 12 is filled to the desired level with particles 26 of catalyst used for the reaction to be performed and these particles are fluidized by introducing the reacting gases entering inlet 20 into the wind box 18 and then passing up through the perforated distributor plate lti to fluidize the particles 26 and form the fluidirxd bed 12.
A plurality of separation tubes 28 extend through the fluidized bed 12 and freeboard 14 with their longitudinal axes substantially parallel to the direction of flow of the gases tluough the bed 12 so as not t~~ interfere si,~mificantly with the formation of the lluidized bed 12 and to mininvze ,abrasion. These separation tubes 28 separate hydrogen formed in the bed (and the freeboard 14) from the other gases in the bed and are formed of material that permits the transmission of hydrogen in molecular or <atomic form into the tubes while inhibiting the transmission of the other gases that are also present in the fluidized bed and in the freeboard 14 so that the gas within the separation tubes 28 is relatively pure hydrogen.
The output from the separation tubes 28 may be connected by a pump 29 to an outlet line 31. 'x he pump 29 may be in the form. of a vacuum pump to apply a negative pressure to the. inside of the tubes 28 and improve the transmission of hydrogen through the membranes.
S The separation tubes 28 extend vertically inside the bed 12 (i.e parallel to the flow direction of the reaction gases) and the freeboard 14 i.e. from the wind box 28 to the top of the freeboard 14.
1n the embodiment illustrated in Figures 1 to 3 inclusive each of the separation tubes 28 is in the form of a membrane module 30 which is composed 1D of an outer protective sheath or tube 32 and inner perm selective membrane tubes 34 which in the illustrated arrangement are shown in a spaced symmetrical arrangement. The periphery of these tubes 34 need not be separated, but must provide the area required to transmit or transfer the desired amount of hydrogen therethrough. The required spacing' for the modules 30 in the bed 12 will be 15 described herein below.
The outer sheath 32 will normally be formed of an abrasion resistant material having a pore size to transmit hydrogen as welt as at least most of the other gases present in the bed 12 and/or freeboard 14 but sufficiently small to prevent the passage of particulate maferial from the bed. This sheath or shielding 20 tube 32 may be made for example of porous ceramic material or porous metallic . material.
The perm selective membrane tubes 34 may be made of any suitable material that will, as above described, result in the partially or perfectly selective transmission of the particular material, in this case hydrogen, while tending to 25 prevent the transmissioxa of any of the other gases or chemicals present in the case of the present invention the reaction mixture gases present within the reactor 10. Membranes maybe substantially perfectly selective to hydrogen (e.g.tubes of dense phase membranes, Ni, Nb, Pd, metal coatings an porous structures enveloped by shielding have been found satisfactory, etc.), i.e. systems wherein the 30 . mechanism of transfer is adsorption, molecule disassociation, atomic diffusion, atoms combination and then molecular desorption; or the membranes that may be partially selective to hydrogen, for example alumina base or silica base porous membranes which operate on the principal of Knudson diffusion or molecular 2~~~~.'~~
sieving wherein selectivity depends on the pore size and relative molecular sizes of the different gases involved in the gas mixture e.g to transfer the smaller molecular size gas while preventing the transmission of the larger molecules.
The choice of which membrane to use in any particular application will S depend on the application including the downstream process requirements and the conditions within the reactor.
If desired the separation tubes may be directly exposed within the bed 12 as shoryn in Figure 4. This arrangement may permit a higher packing of the perm selective membrane tubes within the bed 12 and freeboard 14, but obviously subjects the perm selective nnembrane tubes 34 directly to the fluidized action of the catalyst bed 12 which will likely significantly shorten their life span and thereby increase the operating cost of the system.
The spacing of the separation tubes 28 (which may be discreet tubes 34 or modules 30) will preferably be related to the particle size of the particles 26 of , catalyst to ensure there is ample space for the free movement of the particles 26 to form the fluidized bed 12. Thus the smallest distance eg Sl, SZ or S3 illustrated in Figure 5 will be sufficient to prevent blockages or bridging of the fluidized bed 12 but not significantly larger so that the maximum number of tubes 28 may be provided in the reaction zone 12.
The presence of these tubes 28, aids in limiting the growth of bubbles eg.
tends to prevent bubble coalescing thereby to facilitate maximizing heat and mass transfex i.e. the presence of these tubes 28 influences bubble formation and thus the size of 'bubbles within the bed and optimizing the number, size (diameter) and spacing of such tubes may be used to~ increase the effectiveness of the bed.
The particular catalyst chosen will depend on the reaction intended. For example, a nickel catalyst supported over an alpha-alumina (nickel loading of 4%
to 22%) having a mean particle size range of about 60 to 300 microns, has been found satisfactory for the reforming reaction and formation of the fluidized bed by natural gas, steam mixture maintained at a temperature of 650 to 950 °C under a pressure of 1.5 to 4.5 MPa.
The mixture in the above example will have a steam to carbon ratio preferably in the range of 1.2 to 6.
It will be apparent that the reaction in the fluidized bed 110 is an 20~~1°~p endothermic reaction and thus it is important that the temperature within the xeaction zone of ~luidized bed 12 be maintained. Suitable heat pipes or heat exchangers 36 have been shown schematically as embedded within the bed 12 and serviced by circulating a thermal fluid as indicated by the numeral 38 i.e.
the tube 36 will form at least 1 loop for circulation of a thermal or heating fluid in and out of this fluidized bed 12. This will permit maintaining the temperature in the required range for the particular reaction described above or at any other selected temperature for any particular application to which the present invention may be applied.
While the embedding of a heat exchanger within the bed 12 is the preferred mode of heat transfer to the bed 12, other conventional means for supplying heat to the bed 12 may be used. For example, particles 26 may be withdrawn from the bed 12, heated and then returned to the bed 12 (see the Guerrieri i1S patent 3,524,819 referred to above).
1S In the illustrated arrangement, the gases not absoxbed by the separation tubes 28 move into the freeboard ~ area 14 and tangentially into a cyclone schematically indicated at 40 in Figure 1. These gases enter the cyclone 40 in the a right cylindrical body section 42 which tapers into a conical section 44 joining body 42 to an extension 46 which extends downwardly into the bed 12. The outlet end 48 of the extension 46 is buried well vvithin the bed 12 so that particles separated in the separator 40 are reintroduced into the bed 12. The gas separated from the entrained particulate in tl~e cyclone 40 pass as indicated by a .
line 50 to the further stage in its processing.
- If desired some of the gas separated in the separator 40 and leaving the system may be redirected as indicated by line ~2 under control of the valve 54 back into the system with the re~.ction gases in the blow box 18 and be used to adjust the desired degree of fluidization of the bed 12.
' Generally; when the present invention is employed to produce hydrogen gas by a steam ~ hydrocarbon gas reaction such as the reaction between methane and steam, the reactions will be as follows:
CH4 + 2H20 = C02 -~ 4H2 (1) CH4 + HZO ~ CO + 3H2 (2) as the main reactions. These two reversible reactions will be further promoted ~0~11~0 by removal of hydrogen due to the shift in the chemical equilibrium provided the temperature within the fluidized bed is maintained.
A possible side reaction if CO 'is formed in the fluidized bed comprises:
CO + H20 = COZ + H2, (3) 'Obviously, the removal of hydrogen will favour this reversible reaction as well.
It is important that as much hydrogen as possible be stripped from the product gases before the product gases are exhausted from the system. For this reason, the membrane tubes 28 exteind not just through the fluidized bed 12 but through the freeboard zone 14 as well.
1 The separation tubes 28 within the freeboard 14 aid in further displacing the reaction mixture from the equilibrium compositions to avoid the reduction o~
methane conversion caused by the reverse reaction (methanation) which is :favouzed by the lower temperature in the freeboard 14 and in the lines 50 and 52, It will be apparent that with the present system, the hydxogen gas leaving via line 31 is relatively pure hydrogen gas depending on the perm selective membrane material being used.
It will also be apparent that the gas passing into the freeboard and exiting wia the cleaner 40 and line SO is lean in hydrogen gas due to the separation tubes 28 and to tl~e extension of the separation tubes 28 through the freeboard 14 and therefore is unlikely to undergo methanation over the entrained catalyst. The likelihood of the methanation reaction occurring after the particles of catalyst have been separated in the cleaner 40 is reduced even further.
It will also be apparent that tha reactor and reacting system of the present invention permit the formation of relatively puxe hydrogen gas in a single unit 2S without the need for a purification process. The product gas composition may be controlled by adjusting recycle ratio is the amount of gas recycled via line 52 and the setting of the vacuum pump 29 from a steam hydrocarbon gas reactor, such as a steam, methane or natural gas reactor.
Having described the invention, modifications will be evident to those skilled in the art without departing from the spirit of the invention as defined in the appended claims.
Description of the Pvior An The production of hydrogen ming reaction systems employing steam and hydrocarbon gases such r~s methane or natural gas or the like are well known in the art. These reactions are generally catalytic and are limited by intra particle 10 diffusion and thermodynamic equilibrium Reactors employ;d for this purpose are normally fixed bed type reactors as opposed to fluidized bed reactors although lluidiLed bed reactors have been proposed for use in production of hydrogen in US Patent 3,524,819 issued Aug.
18 1970 to Guerneri and US patents 4,877,550 and 4,888,131 issued October 31 15 1989 and December 18 1989 respectively to Goeisch and . (See also U.S.
Patent 4,938,946 issued July 3, 199t> to Gibsoa, of al. which teaches fluidir~ng Regolith in particulate form 1.'or producing hydrogen gas at elevated temperature.) The addition of hwt to reformers 1z41s also been taught, for example, in US
Patent 3,524,819 to Guerrieri andlor Deutches Patent 3,331,:202 issued 1984 to 20 Reichel. Us patent 4,474,23t? issued Oci. 2 1984 to MeCallister teaches the use ofheat pipes to introduce heat into fluidized bed reactors.
The Goetsch patent 4,877,550 also teaches rapid cooling to overcome the negative effect of the catalyst fuzes entraiizrrrent which reduces the reaction conversion in the Ii~eeboard zone and subsequent process lines.
25 Generally in such steact~hydrocarlxm reaction systems, it is required that the hydrogen be separated using relatively complicated processes for increasing the purity of the hydrogen to that required for subsequent uses. It has also been proposed by Minet et al irr U.S Patent no. 4,981,676 issued January 1 1991 to use a diffusion process for steam relbrming of hydrocarbons in the production of 30 hydrogen, carbon monoxide and carbon dioxide by employing a generally tubular, porous, ceramic membrane and providing a heirted rm.ction ;cone in a container into which the membrane is received. The membrane carries the catalyst and the hydrocarbon gas and steam contact one side of ttze membrrne t.o produce the ~o~~~~o hydrogen, carbon monoxide and carbon dioxide gases. The hydrogen formed selectively diffuses through the membrane and is carried off in an entraining gas.
U.S. Patent 4,810,485 issued March 7, 1989 to Marianowski teaches the formation of hydrogen gas in a reaction zone containing a hydrogen ion porous metallic foil which conducts hydrogen ions therethrough to remove the hydrogen ions from the packed bed as they are' formed and thereby permit a reduction in the operating temperature of the bed and producing a relatively pure hydrogen that is conducted away through the tubular metallic foils to a manifold.
Brief Description ~f the Present Ynvention It is an object of the present invention to provide an improved reaction system employing a fluidized bed to react steam and hydrocarbon gas to produce hydrogen and to separate the hydrogen upon formation thereby to improve the reaction yield.
Broadly the present invention relates to a method and apparatus for producing hydrogen gas comprising forming a fluidized bed of a suitable particulate catalyst by introducing reacting gases comprising a mixture of steam and hydrocarbon gas into the bottom of said fluidized bed to fluidize said particles and form said fluidized bed, said fluidized 'bed occupying a portion of a vessel and forming a reaction zone; a freeboard zone in said vessel above said fluidized bed, reacting said reacting gases 'within said bed to produce hydrogen gas, separating said hydrogen gas as it is formed in said bed as molecular or atomic hydrogen through a perm selective membrane means that extends through said bed' in the direction of flow of said reaction gases and permits transfer of hydrogen therethrough while preventing the transmission of other gases present in said reaction zone therethrough, said hydrogen gas after permeation through the membrane providing a source of relatively pure hydrogen gas.
Preferably said membrane means will also extend through said freeboard zone and separate hydrogen froni said other gases in said freeboard zone.
In some embodiments said perm selective membrane means will comprise a plurality of tubes of perm selective membrane material arranged about said bed with the longitudinal axes of said tubes substantially parallel and extending in said direction of flow of said reaction gases.
2~~~.~~0 Preferably adjacent said perm selective tubes will be spaced at least sufficient to permit fluidizing of said catalyst particles therebetween yet sufficiently small to provide the desired surface area exposed to said reaction zone to permit the transfer of hydrogen generated in said reaction zone.
Preferably said perm selective membrane means will comprise a plurality of modules, each said modules being formed by a plurality of perm selective membrane tubes enclosed in a protective sheath of material that permits hydrogen and other gases to pass therethrough and into contact with said perm selective membrane tubes while prohibiting the passage of said particulate catalyst.
Preferably a pressure significantly lower than that in the reaction zone will be maintained in said perm selective membrane means to improve the permeation rate of hydrogen through. said perm selective meriibrane means.
Preferably, a heating means will be provided to supply heat needed in the reaction zone to maintain said fluidized bed at the desired.reaction temperature.
Preferably, said, other gases leaving said freeboard will be separated from particulate material and said particulate material will be redirected back into said fluidized bed.
Preferably, said separation will comprise centrifugally separating said particulate from said gases in centrifugal cleaner having a conical section having a particulate outlet at 'the small diameter end, said particulate outlet being submerged in said bed and a gas outlet from said base section at the major diameter end of said conical section for removal of cleaned gas from the system and a tangential gas inlet to said centrifugal cleaner adjacent to said gas outlet.
In soma cases it may be desirable to recycle selected amount of other gas evolving from said freeboard and introduce said other gas from said freeboard into said reaction zone with said reacting gasps to control fluidization of said fluidized bed.
l6rief Description of the lDrawings Further features, objects and advantages will be evident from the following detailed description of the preferred embodiments of the present invention taken in conjunction with the accompanying drawings in which:
Figure 1 is a schematic illustration of a fluidized bed reactor system ~t constructed in accordance with the presern invention.
Figure 2 is a section along the line 2 - 2 o f Figure 1.
Figure 3 is an enlarged cross section of a perm selective membrane module.
Figure 4 is a section on the line 4 - 4 of Figure 1 with parts omitted showing a modified arrangement of the perm selective membrane tubes within the fluidized bed reaction zone.
Figure 5 is an e,nla~~ged cross section showing the spacing between adjacent perm selective membrane tubes.
Description of the Pmfe~md Embodiments The reactor vessel 1t7 schematically illustrated in Figm-e 1 has two main sections; A fluidized bed section l2 ibrming a reaction -none 12 and a freeboard section or zone 14. A distributor plate 16 forms the bottom of the fluidized bed section 12 and connects the bottom of the fluidized bed 12 with the wind or blow box 18 which in turn is connected via gas inlet 20 to the sources of reacting gases such as methane and steam as indicated by the lines 22 and 24 respectively.
Preferably a preheater 23 will preheat the reacting gases before they enter the wind box 18.
The fluidized bed section 12 is filled to the desired level with particles 26 of catalyst used for the reaction to be performed and these particles are fluidized by introducing the reacting gases entering inlet 20 into the wind box 18 and then passing up through the perforated distributor plate lti to fluidize the particles 26 and form the fluidirxd bed 12.
A plurality of separation tubes 28 extend through the fluidized bed 12 and freeboard 14 with their longitudinal axes substantially parallel to the direction of flow of the gases tluough the bed 12 so as not t~~ interfere si,~mificantly with the formation of the lluidized bed 12 and to mininvze ,abrasion. These separation tubes 28 separate hydrogen formed in the bed (and the freeboard 14) from the other gases in the bed and are formed of material that permits the transmission of hydrogen in molecular or <atomic form into the tubes while inhibiting the transmission of the other gases that are also present in the fluidized bed and in the freeboard 14 so that the gas within the separation tubes 28 is relatively pure hydrogen.
The output from the separation tubes 28 may be connected by a pump 29 to an outlet line 31. 'x he pump 29 may be in the form. of a vacuum pump to apply a negative pressure to the. inside of the tubes 28 and improve the transmission of hydrogen through the membranes.
S The separation tubes 28 extend vertically inside the bed 12 (i.e parallel to the flow direction of the reaction gases) and the freeboard 14 i.e. from the wind box 28 to the top of the freeboard 14.
1n the embodiment illustrated in Figures 1 to 3 inclusive each of the separation tubes 28 is in the form of a membrane module 30 which is composed 1D of an outer protective sheath or tube 32 and inner perm selective membrane tubes 34 which in the illustrated arrangement are shown in a spaced symmetrical arrangement. The periphery of these tubes 34 need not be separated, but must provide the area required to transmit or transfer the desired amount of hydrogen therethrough. The required spacing' for the modules 30 in the bed 12 will be 15 described herein below.
The outer sheath 32 will normally be formed of an abrasion resistant material having a pore size to transmit hydrogen as welt as at least most of the other gases present in the bed 12 and/or freeboard 14 but sufficiently small to prevent the passage of particulate maferial from the bed. This sheath or shielding 20 tube 32 may be made for example of porous ceramic material or porous metallic . material.
The perm selective membrane tubes 34 may be made of any suitable material that will, as above described, result in the partially or perfectly selective transmission of the particular material, in this case hydrogen, while tending to 25 prevent the transmissioxa of any of the other gases or chemicals present in the case of the present invention the reaction mixture gases present within the reactor 10. Membranes maybe substantially perfectly selective to hydrogen (e.g.tubes of dense phase membranes, Ni, Nb, Pd, metal coatings an porous structures enveloped by shielding have been found satisfactory, etc.), i.e. systems wherein the 30 . mechanism of transfer is adsorption, molecule disassociation, atomic diffusion, atoms combination and then molecular desorption; or the membranes that may be partially selective to hydrogen, for example alumina base or silica base porous membranes which operate on the principal of Knudson diffusion or molecular 2~~~~.'~~
sieving wherein selectivity depends on the pore size and relative molecular sizes of the different gases involved in the gas mixture e.g to transfer the smaller molecular size gas while preventing the transmission of the larger molecules.
The choice of which membrane to use in any particular application will S depend on the application including the downstream process requirements and the conditions within the reactor.
If desired the separation tubes may be directly exposed within the bed 12 as shoryn in Figure 4. This arrangement may permit a higher packing of the perm selective membrane tubes within the bed 12 and freeboard 14, but obviously subjects the perm selective nnembrane tubes 34 directly to the fluidized action of the catalyst bed 12 which will likely significantly shorten their life span and thereby increase the operating cost of the system.
The spacing of the separation tubes 28 (which may be discreet tubes 34 or modules 30) will preferably be related to the particle size of the particles 26 of , catalyst to ensure there is ample space for the free movement of the particles 26 to form the fluidized bed 12. Thus the smallest distance eg Sl, SZ or S3 illustrated in Figure 5 will be sufficient to prevent blockages or bridging of the fluidized bed 12 but not significantly larger so that the maximum number of tubes 28 may be provided in the reaction zone 12.
The presence of these tubes 28, aids in limiting the growth of bubbles eg.
tends to prevent bubble coalescing thereby to facilitate maximizing heat and mass transfex i.e. the presence of these tubes 28 influences bubble formation and thus the size of 'bubbles within the bed and optimizing the number, size (diameter) and spacing of such tubes may be used to~ increase the effectiveness of the bed.
The particular catalyst chosen will depend on the reaction intended. For example, a nickel catalyst supported over an alpha-alumina (nickel loading of 4%
to 22%) having a mean particle size range of about 60 to 300 microns, has been found satisfactory for the reforming reaction and formation of the fluidized bed by natural gas, steam mixture maintained at a temperature of 650 to 950 °C under a pressure of 1.5 to 4.5 MPa.
The mixture in the above example will have a steam to carbon ratio preferably in the range of 1.2 to 6.
It will be apparent that the reaction in the fluidized bed 110 is an 20~~1°~p endothermic reaction and thus it is important that the temperature within the xeaction zone of ~luidized bed 12 be maintained. Suitable heat pipes or heat exchangers 36 have been shown schematically as embedded within the bed 12 and serviced by circulating a thermal fluid as indicated by the numeral 38 i.e.
the tube 36 will form at least 1 loop for circulation of a thermal or heating fluid in and out of this fluidized bed 12. This will permit maintaining the temperature in the required range for the particular reaction described above or at any other selected temperature for any particular application to which the present invention may be applied.
While the embedding of a heat exchanger within the bed 12 is the preferred mode of heat transfer to the bed 12, other conventional means for supplying heat to the bed 12 may be used. For example, particles 26 may be withdrawn from the bed 12, heated and then returned to the bed 12 (see the Guerrieri i1S patent 3,524,819 referred to above).
1S In the illustrated arrangement, the gases not absoxbed by the separation tubes 28 move into the freeboard ~ area 14 and tangentially into a cyclone schematically indicated at 40 in Figure 1. These gases enter the cyclone 40 in the a right cylindrical body section 42 which tapers into a conical section 44 joining body 42 to an extension 46 which extends downwardly into the bed 12. The outlet end 48 of the extension 46 is buried well vvithin the bed 12 so that particles separated in the separator 40 are reintroduced into the bed 12. The gas separated from the entrained particulate in tl~e cyclone 40 pass as indicated by a .
line 50 to the further stage in its processing.
- If desired some of the gas separated in the separator 40 and leaving the system may be redirected as indicated by line ~2 under control of the valve 54 back into the system with the re~.ction gases in the blow box 18 and be used to adjust the desired degree of fluidization of the bed 12.
' Generally; when the present invention is employed to produce hydrogen gas by a steam ~ hydrocarbon gas reaction such as the reaction between methane and steam, the reactions will be as follows:
CH4 + 2H20 = C02 -~ 4H2 (1) CH4 + HZO ~ CO + 3H2 (2) as the main reactions. These two reversible reactions will be further promoted ~0~11~0 by removal of hydrogen due to the shift in the chemical equilibrium provided the temperature within the fluidized bed is maintained.
A possible side reaction if CO 'is formed in the fluidized bed comprises:
CO + H20 = COZ + H2, (3) 'Obviously, the removal of hydrogen will favour this reversible reaction as well.
It is important that as much hydrogen as possible be stripped from the product gases before the product gases are exhausted from the system. For this reason, the membrane tubes 28 exteind not just through the fluidized bed 12 but through the freeboard zone 14 as well.
1 The separation tubes 28 within the freeboard 14 aid in further displacing the reaction mixture from the equilibrium compositions to avoid the reduction o~
methane conversion caused by the reverse reaction (methanation) which is :favouzed by the lower temperature in the freeboard 14 and in the lines 50 and 52, It will be apparent that with the present system, the hydxogen gas leaving via line 31 is relatively pure hydrogen gas depending on the perm selective membrane material being used.
It will also be apparent that the gas passing into the freeboard and exiting wia the cleaner 40 and line SO is lean in hydrogen gas due to the separation tubes 28 and to tl~e extension of the separation tubes 28 through the freeboard 14 and therefore is unlikely to undergo methanation over the entrained catalyst. The likelihood of the methanation reaction occurring after the particles of catalyst have been separated in the cleaner 40 is reduced even further.
It will also be apparent that tha reactor and reacting system of the present invention permit the formation of relatively puxe hydrogen gas in a single unit 2S without the need for a purification process. The product gas composition may be controlled by adjusting recycle ratio is the amount of gas recycled via line 52 and the setting of the vacuum pump 29 from a steam hydrocarbon gas reactor, such as a steam, methane or natural gas reactor.
Having described the invention, modifications will be evident to those skilled in the art without departing from the spirit of the invention as defined in the appended claims.
Claims (20)
1. An apparatus for producing hydrogen gas comprising a reaction vessel having a reaction vane, a suitable particulate catalyst contained within said vessel, means for introducing reacting gases comprising a mixture of steam and hydrocarbon gas into a bottom end of said reaction zone to fluidize said particulate catalyst and form said reaction zone into a fluidized bed, said fluidized bed reaction zone occupying a portion of said vessel, means forming a freeboard zone in said vessel above said fluidized bed, separating means for separating hydrogen gas produced in said reaction vessel from other gases in said reaction vessel, a first portion of said separating means in said fluidized bed reaction zone for separating said hydrogen gas in said fluidized bed reaction zone, a second portion of said separating means in said freeboard zone to separate further of said hydrogen gas formed in said vessel, said separating means including perm selective membrane tubes having walls formed by perm selective membrane material that selectively permit said hydrogen to pass therethrough as molecular or atomic hydrogen while preventing the transmission of other gases present in said reaction zone therethrough, the spacing between adjacent said separating means being at least sufficient for fluidizing of said particulate catalyst therebetween, but sufficiently small to provide the surface area of said separation means exposed to said reacting gases in said fluidized bed reaction zone required for effective transfer of hydrogen generated in said reaction zone from said reaction zone, and means for withdrawing said hydrogen gas from inside said perm selective membrane tubes in a stream containing substantially all of said hydrogen gas as hydrogen gas, whereby said hydrogen gas after permeation through said membrane material provides a source of relatively pure hydrogen gas.
2. ~An apparatus as defined in claim 1 wherein said first portion of said separating means extends through said fluidized bed reaction zone in a direction substantially parallel to the direction of flow of said reacting gases through said fluidized bed reaction zone toward said freeboard zone.
3. ~An apparatus as defined in claim 1 wherein at least said first portion of said separating means comprises a plurality of perm selective modules, each of said perm selective modules including a protective sheath and a selected number of said membrane tubes of said perm selective membrane material, said protective sheath formed from material that permits said hydrogen and said other gases to pass therethrough and into contact with said perm selective membrane tubes while preventing the passage of said particulate catalyst therethrough.
4. ~An apparatus as defined in Claim 1 wherein at least said first portion of said separating means comprises a plurality of perm selective modules, each of said perm selective modules being formed by a plurality of perm selective membrane tubes enclosed in a protective sheath, said protective sheath formed from material that permits said hydrogen and said other gases to pass therethrough and into contact with said perm selective membrane tubes while preventing the passage of said particulate catalyst therethrough.
5. ~An apparatus as defined in Claim 3 further comprising means for withdrawing hydrogen gas from the inside of said perm selective membrane tubes.
6. ~An apparatus as defined in Claim 1 further comprising separator means for separating entrained said particulate catalyst from said other gas after said other gas leaves said fluidized bed reaction zone, said separator means having an outlet for separated particulate catalyst submerged in said fluidized bed to return said separated particulate catalyst to said fluidized bed.
7.~An apparatus as defined in Claim 1 further comprising means to recycle selected amount of other gas evolving from said freeboard zone and introduce said other gas from said freeboard zone into said reaction zone with said reacting gases to control fluidization characteristics of said fluidized bed.
8. ~An apparatus as defined in Claim 2 wherein at least said first portion of said separating means comprises a plurality of perm selective modules, each of said perm selective modules including a protective sheath and a selected number of said membrane tubes of said perm selective membrane material, said protective sheath formed from material that permits said hydrogen and said other gases to pass therethrough and into contact with said perm selective membrane tubes while preventing the passage of said particulate catalyst therethrough.
9. ~An apparatus as defined in Claim 2 wherein at least said first portion of said separating means comprises a plurality of perm selective modules, each of said perm selective modules being formed by a plurality of perm selective membrane tubes enclosed in a protective sheath, said protective sheath formed from material that permits said hydrogen and said other gases to pass therethrough and into contact with said perm selective membrane tubes while preventing the passage of said particulate catalyst therethrough.
10. ~A method for producing hydrogen gas comprising forming a fluidized bed of a suitable particulate catalyst by introducing reacting gases comprising a mixture of steam and hydrocarbon gas into the bottom of said fluidized bed to fluidize said particulate catalyst and form said fluidized bed, said fluidized bed occupying a portion of a vessel and forming a reaction zone, forming a freeboard zone in said vessel above said fluidized bed reaction zone, reacting said reacting gases within said fluidized bed reaction zone to produce hydrogen gas, separating said hydrogen gas from other gases in said fluidized bed reaction zone as molecular or atomic hydrogen through a perm selective membrane means that permits transfer of hydrogen therethrough while preventing the transmission of said other gases present in said reaction zone therethrough, separating further hydrogen gas from said other gases through said perm selective membrane means in said freeboard zone, said hydrogen gas after permeation through said perm selective membrane means
11 providing a source of relatively pure hydrogen gas and withdrawing said relatively pure hydrogen gas.
11. A method as defined in claim 10 wherein said separating comprises first separating said hydrogen and said other gases from said particulate catalyst through a protective sheath and then separating said hydrogen from said other gases through said perm selective membrane means.
11. A method as defined in claim 10 wherein said separating comprises first separating said hydrogen and said other gases from said particulate catalyst through a protective sheath and then separating said hydrogen from said other gases through said perm selective membrane means.
12. A method as defined in claim 10 further comprising withdrawing hydrogen gas from the side of said perm selective membrane means separated from said fluidized bed and to which said hydrogen passes to improve the permeation rate of said hydrogen through said perm selective membrane means.
13. A method as defined in claim 10 further comprising supplying heat to said reaction zone to maintain said fluidized bed reaction zone at a selected reaction temperature.
14. A method as defined in claim 10 further comprising separating said particulate catalyst from said other gases after leaving said fluidized bed reaction zone and recirculating said separated particulate catalyst back into said fluidized bed.
15. A method as defined in claim 10 further comprising recycling a selected amount of said other gas evolving from said reaction zone back into said reaction zone with said reacting gases to control fluidization of said fluidized bed.
16. A method as defined in claim 10 wherein said separating comprises first separating said hydrogen and said other gases from said particulate catalyst through a protective sheath and then separating said hydrogen from said other gases through said perm selective membrane means.
17. A method as defined in claim 17 further comprising withdrawing hydrogen gas from the side of said perm selective membrane means separated from said fluidized bed to which said hydrogen passes to improve the permeation rate of said hydrogen through said perm selective membrane means.
18. A method as defined in claim 17 further comprising supplying heat to said reaction zone to maintain said fluidized bed reaction zone at a selected reaction temperature.
19. A method as defined in claim l6 further comprising recycling a selected amount of said other gas evolving from said reaction zone back into said reaction zone with said reacting gases to control fluidization of said fluidized bed.
20. A method as defined in claim 14 further comprising recycling a selected amount of said other gas evolving from said reaction zone back into said reaction zone with said reacting gases to control fluidization of said fluidized bed.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002081170A CA2081170C (en) | 1992-10-22 | 1992-10-22 | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
| US07/965,011 US5326550A (en) | 1992-10-22 | 1992-10-23 | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
| PCT/CA1993/000423 WO1994008890A1 (en) | 1992-10-22 | 1993-10-12 | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA002081170A CA2081170C (en) | 1992-10-22 | 1992-10-22 | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
| US07/965,011 US5326550A (en) | 1992-10-22 | 1992-10-23 | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2081170A1 CA2081170A1 (en) | 1994-04-23 |
| CA2081170C true CA2081170C (en) | 2002-12-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002081170A Expired - Lifetime CA2081170C (en) | 1992-10-22 | 1992-10-22 | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
Country Status (3)
| Country | Link |
|---|---|
| US (1) | US5326550A (en) |
| CA (1) | CA2081170C (en) |
| WO (1) | WO1994008890A1 (en) |
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| US11535514B2 (en) * | 2020-02-26 | 2022-12-27 | Gas Technology Institute | System and method for recycling pressure swing absorber off-gas |
| US11712655B2 (en) | 2020-11-30 | 2023-08-01 | H2 Powertech, Llc | Membrane-based hydrogen purifiers |
| US20230024915A1 (en) * | 2021-07-16 | 2023-01-26 | Battelle Memorial Institute | Porous Polybenzimidazole Membrane Supports for Composite Membranes |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2516974A (en) * | 1946-12-04 | 1950-08-01 | Texace Dev Corp | Method and apparatus for gasifying carbonaceous material |
| US3524819A (en) * | 1967-03-03 | 1970-08-18 | Lummus Co | Steam reforming of hydrocarbons |
| US4474230A (en) * | 1982-08-31 | 1984-10-02 | Foster Wheeler Energy Corporation | Fluidized bed reactor system |
| DE3424208A1 (en) * | 1984-06-30 | 1986-01-16 | Kernforschungsanlage Jülich GmbH, 5170 Jülich | METHOD AND DEVICE FOR INCREASING THE SALES OF GAS REACTIONS PROCESSING WITH HYDROGEN PRODUCTION |
| US4810485A (en) * | 1986-08-25 | 1989-03-07 | Institute Of Gas Technology | Hydrogen forming reaction process |
| US4877550A (en) * | 1988-03-28 | 1989-10-31 | Exxon Research And Engineering Company | Synthesis gas preparation and catalyst therefor |
| US4888131A (en) * | 1988-03-28 | 1989-12-19 | Exxon Research And Engineering Company | Synthesis gas preparation and catalyst therefor |
| CA1333008C (en) * | 1988-03-28 | 1994-11-15 | Duane Arlen Goetsch | Synthesis gas preparation and catalyst therefor |
| US4938946A (en) * | 1988-04-13 | 1990-07-03 | Carbotek, Inc. | Lunar hydrogen recovery process |
| FR2636858B1 (en) * | 1988-09-08 | 1990-11-02 | Air Liquide | METHOD AND INSTALLATION FOR SEPARATING A COMPONENT WITH INTERMEDIATE PERMEABILITY OF A GASEOUS MIXTURE |
| US4981676A (en) * | 1989-11-13 | 1991-01-01 | Minet Ronald G | Catalytic ceramic membrane steam/hydrocarbon reformer |
| US5073356A (en) * | 1990-09-20 | 1991-12-17 | Air Products And Chemicals, Inc. | Integrated processes for the production of carbon monoxide |
-
1992
- 1992-10-22 CA CA002081170A patent/CA2081170C/en not_active Expired - Lifetime
- 1992-10-23 US US07/965,011 patent/US5326550A/en not_active Expired - Lifetime
-
1993
- 1993-10-12 WO PCT/CA1993/000423 patent/WO1994008890A1/en active Application Filing
Also Published As
| Publication number | Publication date |
|---|---|
| WO1994008890A1 (en) | 1994-04-28 |
| US5326550A (en) | 1994-07-05 |
| CA2081170A1 (en) | 1994-04-23 |
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