CA2265468C - Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide - Google Patents

Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide Download PDF

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Publication number
CA2265468C
CA2265468C CA002265468A CA2265468A CA2265468C CA 2265468 C CA2265468 C CA 2265468C CA 002265468 A CA002265468 A CA 002265468A CA 2265468 A CA2265468 A CA 2265468A CA 2265468 C CA2265468 C CA 2265468C
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Prior art keywords
vessel
tube
reformer
reaction zone
oxygen
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CA002265468A
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French (fr)
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CA2265468A1 (en
Inventor
Lawrence G. Clawson
William L. Mitchell
Jeffrey M. Bentley
Johannes H.J. Thijssen
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Nuvera Fuel Cells LLC
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Nuvera Fuel Cells LLC
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    • 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
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    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
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    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1217—Alcohols
    • C01B2203/1229—Ethanol
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • C—CHEMISTRY; METALLURGY
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/141—At least two reforming, decomposition or partial oxidation steps in parallel
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • 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
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • 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
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M2250/00—Fuel cells for particular applications; Specific features of fuel cell system
    • H01M2250/20—Fuel cells in motive systems, e.g. vehicle, ship, plane
    • 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
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells
    • 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
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T90/00—Enabling technologies or technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02T90/40—Application of hydrogen technology to transportation, e.g. using fuel cells

Abstract

An apparatus and a method are disclosed for converting hydrocarbon fuel or an alcohol into hydrogen gas and carbon dioxide. The apparatus includes a first vessel (18) having a partial oxidation reaction zone (24) and a separate steam reforming reaction zone (26) that is distinct from the partial oxidation reaction zone. The first vessel has a first vessel inlet (20) at the partial oxidation reaction zone and a first vessel outlet (22) at the steam reforming zone. The reformer also includes a helical tube (32) extending about the first vessel. The helical tube has a first end connected to an oxygen-containing source (42) and a second end connected to the first vessel at the partial oxidation reaction zone. Oxygen gas from an oxygen-containing source can be directed through the helical tube to the first vessel. A second vessel (58) having a second vessel inlet (60) and second vessel outlet (22) is annularly disposed about the first vessel.
The helical tube is disposed between the first vessel and the second vessel and gases from the first vessel can be directed through second vessel.

Description

?WO 98/087711015202530CA 02265468 1999-02-24PCT/US97/14906METHOD AND APPARATUS FOR CONVERTING HYDROCARBONFUEL INTO HYDROGEN GAS AND CARBON DIOXIDEBackground of the InventionFuel cells continue to play an increasinglyimportant role in power generation for both stationaryand transportation applications. A primary advantageof fuel cells is their highly efficient operationwhich, unlike today's heat engines, are not limited byCarnot cycle efficiency. Furthermore, fuel cells farsurpass any known energy conversion device in theirpurity of operation. Fuel cells are chemical powersources in which electrical power is generated in achemical reaction between a reducer (hydrogen) and anoxidizer (oxygen) which are fed to the cells at a rateproportional to the power load. Therefore, fuel cellsneed both oxygen and a source of hydrogen to function.There are two issues which are contributing to thelimited use of hydrogen gas today. Firstly, hydrogengas (H2) has a low volumetric energy density comparedto conventional hydrocarbons, meaning that anequivalent amount of energy stored as hydrogen willtake up more volume than the same amount of energystored as a conventional hydrocarbon. Secondly, thereis presently no widespread hydrogen infrastructurewhich could support a large number of fuel cell powersystems.An attractive source of hydrogen to power fuelcells is contained in the molecular structure ofvarious hydrocarbon and alcohol fuels. A reformer is adevice that breaks down the molecules of a primary fuelto produce a hydrogen—rich gas stream capable of?WO 98/0877110152025CA 02265468 1999-02-24PCT/US97/14906-2-powering a fuel cell. Although the process forreforming hydrocarbon and alcohol fuels is established-on a large industrial basis, no known analogousdevelopment has occurred for small—scale, highlyintegrated units.Therefore, a need exists for a more compactapparatus for generating hydrogen gas from a variety ofhydrocarbon fuel sources for use in a fuel cell topower a vehicle.Summary of the InventionThe present invention relates to a reformer andmethod for converting an alcohol or hydrocarbon fuelinto hydrogen gas and carbon dioxide.The reformer includes a first vessel having apartial oxidation reaction zone and a separate steamreforming reaction zone that is distinct from thepartial oxidation reaction zone. The first vessel hasa first vessel inlet at the partial oxidation reactionzone and a first vessel outlet at the steam reformingThe reformer also includes a helical tubeThe helical tube hasa first end connected to an oxygen—containing sourceZ0118 .extending about the first vessel.and a second end connected to the first vessel at thepartial oxidation reaction zone. Oxygen gas from anoxygen—containing source can be directed through thehelical tube to the first vessel. A second vesselhaving a second vessel inlet and second vessel outletThehelical tube is disposed between the first vessel andis annularly disposed about the first vessel.?1015202530CA 02265468 1999-02-24WO 98/08771 PCT/U S97/ 14906-3-the second vessel and gases from the first vessel canbe directed through the second vessel.The method includes directing oxygen-containinggas through a helical tube which is disposed around afirst vessel. Hydrocarbon vapor and steam are directedinto the helical tube to form a mixture of oxygen gas,fuelvapor and steam are directed into the first vessel.fuel vapor and steam. The mixture of oxygen gas,The fuel vapor spontaneously partially oxidizes to forma heated reformate stream that includes carbon monoxideand hydrogen gas. The remaining fuel vapor is steamreformed in the heated reformate stream to formhydrogen gas and carbon monoxide. The heated reformatestream is directed over the exterior of the helicaltube, whereby the heated reformate stream heats themixture in the helical tube. A portion of the carbon.monoxide gas of the reformate stream is converted tocarbon dioxide and hydrogen gas by a high temperatureshift reaction. At least a portion of the remainingcarbon monoxide gas of the reformate stream isconverted to carbon dioxide and hydrogen gas by a lowtemperature shift reaction.In another embodiment of a reformer for convertinga hydrocarbon fuel into hydrogen gas and carbondioxide, the apparatus includes a first tube which hasa first tube inlet for receiving a first mixture of anoxygen—containing gas and a first fuel, which can be ahydrocarbon or an alcohol, and a first tube outlet forconducting a first reaction reformate of the firstmixture. A second tube is annularly disposed about thefirst tube, wherein the second tube has a second tube?W0 98/0877!1015202530CA 02265468 1999-02-24PCT/US97/14906-4._inlet for receiving a second mixture of a second fuel,which can be a hydrocarbon or an alcohol, and steam. ~A_second tube has a second tube outlet for conducting asecond reaction reformate of the second mixture. Acatalyst reforming zone is annularly disposed about thesecond tube. The first reaction reformate and thesecond reaction reformate can be directed through thefirst tube outlet and the second tube outlet,respectively, to the catalyst reforming zone forfurther reforming of the mixtures. In a preferreda hydrocarbon fuel fractionator is attachedThefractionator can separate a heavy portion from theembodiment,at the first tube inlet and second tube inlet.hydrocarbon fuel for subsequent direction to theA lightportion can be separated from the hydrocarbon fuel forpartial oxidation zone in the first tube.subsequent direction to the steam reforming zone in thesecond tube. HIn another embodiment of the method for convertinga hydrocarbon or alcohol fuel into hydrogen gas andcarbon dioxide, a first mixture of first hydrocarbon oralcohol fuel and oxygen—containing gas is directed intoa first tube. The hydrocarbon or alcohol fuel in thefirst mixture spontaneously partially oxidizes to forma first heated reformate stream that includes hydrogengas and carbon monoxide. A second mixture of a secondhydrocarbon or alcohol fuel and steam is directed intoa second tube annularly disposed about the first tube.The second hydrocarbon or alcohol fuel of the secondmixture partially steam reforms to form a second heatedreformate stream that includes hydrogen gas and carbon?WO 98/0877110152025CA 02265468 1999-02-24PC T/U S97/ 14906-5-monoxide. The first heated reformate stream and secondheated reformate stream aresdirected through a catalyst-reforming zone to further reform the reformate streamsto hydrogen gas and carbon dioxide. In a preferredembodiment, the hydrocarbon fuel prior to directioninto the first tube and the second tube is fractionatedinto heavy portion of the hydrocarbon fuel and a lightportion of the hydrocarbon fuel. The heavy portion issubsequently directed to the partial oxidation zone.The light portion is directed to the steam reformingzone.This invention has many advantages. The apparatuscan use a variety of hydrocarbon fuels, such asgasoline, JP-8, methanol and ethanol. The partialoxidation reaction zone allows the fuel to partiallyburn while not forming soot and while providing heat tothe steam reforming zone and the other portions of thereactor annularly disposed around the partial oxidationzone. Further, the apparatus is sufficiently compactfor use in an automobile. In some embodiments, theapparatus includes a high temperature shift catalystwhich allows the apparatus to be more compact andlighter in weight than if only a low temperature shiftcatalyst is used.Brief Description of the DrawingsFigure 1 is an orthogonal projection side view ofone embodiment of the apparatus of the presentinvention.?S1015202530CA 02265468 1999-02-24W0 98/08771 PCT/US97/14906-6-Figure 2 is an orthogonal projection side view ofa second embodiment of the apparatus of the presentinvention.Figure 3 is an orthogonal projection side view ofa third embodiment of the apparatus of the presentinvention.Detailed Description of the InventionThe features and details of the method andapparatus of the invention will now be moreparticularly described with reference to theaccompanying drawings and pointed out in the claims.The same numeral present in different figuresIt will bethe particular embodiments of the invention are shownrepresents the same item. understood thatby way of illustration and not as limitations of theinvention. The principal features of this inventioncan be employed in various embodiments withoutAllpercentages and parts are by weight unless otherwisedeparting from the scope of the invention.indicated.One embodiment of the invention is shown in FigureReformer1. Reformer 10 has reformer vessel 12.vessel 12 can be cylindrical in shape. Reformer 10 hasupper portion 14 and lower portion 16. Disposed in thecenter of reformer vessel 12 is first vessel 18 whichextends substantially the height of reformer vessel 12.First vessel 18 has first vessel inlet 20 for receivinggases into first vessel 18 and can tangentially directthe gases through the first vessel. First vessel 18has first vessel outlet 22 at upper portion 14 of?1015202530CA 02265468 1999-02-24wo 93/03771 PCT/US97/14906-7-reformer 10 for gases to exit first vessel. Perforatedplate 31 is located at first vessel outlet 22 andcovers the diameter of first vessel 18. Partialoxidation reaction zone 24 is in lower portion 16 ofifirst vessel 18.Partial oxidation zone 24 is suitable for partialoxidation of a hydrocarbon or alcohol fuel with oxygento form a mixture including carbon monoxide, steam andhydrogen gas. Steam reforming zone 26 is above partialoxidation zone 24 and includes a steam reformingcatalyst 28.Preferably, the steam reforming catalystincludes nickel with amounts of a noble metal, such ascobalt, platinum, palladium, rhodium, ruthenium,iridium, and a support such as magnesia, magnesiumalumina, silica, zirconia,aluminate, singly or incombination. Alternatively, steam reforming catalyst28 can be a single metal, such as nickel, supported ona refractory carrier like magnesia, magnesiumaluminate, alumina, silica, or zirconia, singly or incombination, promoted by an alkali metal likepotassium. Steam reforming zone 26 can autothermallyreform steam and_methane generated in partial oxidationzone 24 to hydrogen gas and carbon monoxide. Steamreforming catalyst 28, which can be granular, issupported within partial oxidation zone 24 byperforated plate 30 and perforated plate 31.Helical tube 32 extends about the length of firstFirst end 34 of helicalat inlet housing 33.vessel 18. tube 32 is locatedOxygen source 42 is connected toinlet housing 33 by conduit 35 with first end inlet 36for receiving oxygen—containing gas from oxygen gas ?1015202530CA 02265468 1999-02-24W0 98/08771 PCT/US97/ 14906-8-zone 40. Second end 44 of helical tube 32 is connectedat first vessel inlet 20. Examples of suitable oxygen-(Oz), Fuelinlet 46 is joined to helical tube 32 proximate tocontaining gas include oxygen air, etc.second end 44. Conduit 50 extends from fuel source 48to fuel inlet 46.hydrocarbons which encompass alcohols,JP-8,Steam inlet 52 is proximate to fuel inlet 46.Examples of suitable fuels includealso. Fuelsinclude gasoline, kerosene, methane, methanol andethanol.Steam can be directed from steam source 54 to steamtube 56 through first steam inlet 52 into helical tube32.directed into helical tube 32.In another embodiment, fuel and steam can beSecond vessel 58 is annularly disposed about firstvessel 18. Second vessel inlet 60 receives gaseousproducts from first vessel outlet 22. Second vesseloutlet 62 at lower portion 16 of reformer 10 allows gasto exit second vessel 58. Helical tube 32 is disposedbetween first vessel 18 and second vessel 58 and gasesfrom first vessel 18 can be directed through secondvessel 58 from second vessel inlet 60 over and aroundhelical tube 32 to second vessel outlet 62.. Flowdistribution region 63 conducts gas from second vesseloutlet 52 to high temperature shift zone 64.Additional steam or water can be directed from a steamsource into second vessel 58 through second steam inlet53 to provide added steam to provide added cooling andfurther the reformation of the fuels.High temperature shift zone 64 is annularlylocated between second vessel 58 and reformer vessel 12and includes a high temperature shift catalyst. An?1015202530CA 02265468 1999-02-24WO 98/08771 PCT/U S97/ 14906-9-example of a suitable high temperature shift catalystare those that are operable at a temperature in therange of between about 300°C and about 600°C.Preferably the high temperature shift catalyst includestransition metal oxides, such as ferric oxide (Fe?x)(Cr2O,).temperature shift catalysts include iron oxide andand chromic oxide other types of highchromium oxide promoted with copper, iron silicide,supported platinum, supported palladium, and othersupported platinum group metals, singly and incombination. High temperature shift catalyst 66 isheld in place by perforated plate 68 and perforatedplate 70. Gas can pass through high temperature shiftzone 64 through perforated plate 70 to sulfur removalzone 71.Above high temperature shift zone 64 is sulfurremoval zone 71. Sulfur removal zone 71 includes acatalyst which can reduce the amount of hydrogensulfide ?gs), which is deleterious to a lowtemperature shift catalyst, in the gas stream to aconcentration of about one part per million or less.An example of a suitable catalyst includes a zincoxide. Sulfur removal zone 71 is sized depending onIf a low sulfur fuel is used, aIf a high sulfurfuel is used, a larger sulfur removal zone isthe type of fuel used.small sulfur removal zone is needed.necessary. Gas can pass from sulfur removal zone 71through perforated plate 73 to cooling zone 72.Cooling zone 72 includes a plurality of verticalfins 74 which radiate from second vessel 58 to reformer?WO 98/0877]101S202530CA 02265468 1999-02-24PCT/US97/14906-10-vessel 12 which extends from high temperature shiftzone 64 to low temperature shift zone 76.Cooling tube 78 is helically disposed about secondvessel 58 and is attached to vertical fins 74. Coolingtube 78 has cooling tube inlet 80 for receiving asuch as water,cooling medium, through cooling tube 78to cooling tube outlet 82. In another embodiment,cooling tube 78 is wound a second series of timesaround second vessel 58. The gaseous products fromhigh temperature catalyst zone 64 can pass between the“vertical fins 74 and pass over cooling tube 78 allowinggaseous products to cool.Low temperature shift zone 76 is annularlydisposed above cooling zone 78 and between secondvessel 58 and reformer vessel 12 and includes lowtemperature shift modifying catalyst 84 for reducingcarbon monoxide to a level of less than about onepercent, by volume, or below. An example of a suitablelow temperature modifying catalyst are those that areoperable at a temperature in a range of between about150°C and about 300°C.modifying catalyst includes cupric oxide (CuO) and zinc(ZnO).catalysts include copper supported on other transitionPreferably, the low temperatureoxide Other types of low temperature shiftmetal oxides like zirconia, zinc supported ontransition metal oxides or refractory supports likesupported platinum,silica or alumina, supportedrhenium, supported palladium, supported rhodium andsupported gold. Low temperature shift zone catalyst 84is held in place by lower perforated plate 86 and upperperforated plate 88. Gaseous products from cooling?W0 98/0877]1015202530CA 02265468 1999-02-24PCT/US97/1 4906-11-zone 72 can pass through perforated plate 86 throughlow temperature shift zone 76 through upper perforatedplate 88. Exit zone 90 is above low temperature shiftzone 76 and has reformer exit 92.In the method for converting hydrocarbon fuel intohydrogen gas, an oxygen—containing gas, such as air, isdirected from oxygen source 42 through conduit 35 toinlet housing 33 to oxygen gas zone 40 into first endinlet 36 of helical tube 32.at a pressure in the range of between about 0 and 500psig.preheated to a temperature of about 450°C.Reformer 10 can operateThe oxygen—containing gas, such as air, isIn apreferred embodiment, air has a velocity of greaterthan about 40 meters per second.A suitable hydrocarbon or alcohol vapor isdirected from fuel source 48 through fuel tube 50 tofuel inlet 46. Examples of suitable hydrocarbon fuelsinclude gasoline, JP-8, methanol, ethanol, kerosene andother suitable hydrocarbons typically used insuch as methane orreformers. Gaseous hydrocarbons,propane, can also be used. Steam is directed fromsteam source 54 through steam tube 56 to first steaminlet 52.about 100 and about 150°C.hydrocarbon fuel are fed at rates sufficient to mixSteam has a temperature in the range betweenThe air, steam andwithin helical tube 32 and spontaneously partiallyoxidize as the mixture enters partial oxidation zone 24through first vessel inlet 20 to form a heatedreformate stream that includes carbon monoxide andhydrogen gas. In a preferred embodiment, oxygen-containing gas is tangentially directed around the ?WO 98/0877]1015202530CA 02265468 1999-02-24PCT/U S97/ 14906.12 7.interior of partial oxidation zone 24, which is anempty chamber. In partial oxidation zone 24, thereformate products can include methane, hydrogen gas,water and carbon monoxide. Partial oxidation zone 24has a preferred temperature in the range of betweenabout 950°C and about 1l50°C.preferentially run at the higher end of the temperatureA heavier fuel isrange while a lighter fuel is run at a lower end of thetemperature range.From partial oxidation zone 24, reformate productsare directed through perforated plate 30 to steamreforming zone 26. In steam reforming zone 26, theremaining hydrocarbon vapor in the heated reformatestream from partial oxidation zone 24 is steam reformedin the presence of steam reforming catalyst 28 intohydrogen gas and carbon monoxide. Steam reforming zone26 typically has a temperature in the range of betweenabout 700 and 900°C.provides sufficient heat to provide heat to helicalThe partial oxidation reactiontube 32 to preheat the air and other contents ofhelical tube 32 and also provide heat to the steamreforming step. The hydrocarbon fuel is burned partlyin partial oxidation zone 24 and the remainder of thefuel with the steam is mixed with the partial oxidationzone combustion products for steam reforming andhydrocarbon shifting to carbon monoxide and hydrogengas in the presence of steam reforming catalyst 28.The heated reformate stream exiting from steamreforming zone 26 has a temperature of between about700°C and about 900°C.directed between first vessel 18 and second vessel 58The heated reformate stream is? 1015202530CA 02265468 1999-02-24WO 98/08771-13-and around the exterior of helical tube 32, whereby theheated reformate stream is cooled by heating thecontents of helical tube 32 and also the first vessel18 and second vessel 56.Heated reformate stream exits second vessel outlet62 to flow distribution zone 63, where it has beencooled to a temperature of between about 300°C andabout 600°C and is directed through perforated plate 68to high temperature shift zone 64 where essentially allof the carbon monoxide is removed or reduced bycontacting the heated reformate stream with hightemperature shift catalyst 66 at a temperature in therange of between about 300°C and 600°C. High-temperature shift zone 64 operates adiabatically toreduce the carbon monoxide levels with modesttemperature rise. In one embodiment, heated reformatestream entering high temperature shift zone 64 hasabout fourteen to seventeen percent carbon monoxide, byvolume, and exits high temperature shift zone 64 withabout two to four percent carbon monoxide, by volume.The high temperature shift zone treated reformatestream is directed through sulfur removal zone 71 wherethe hydrogen sulfide content of the stream is reducedto a concentration of less than about one part permillion. From sulfur removal zone 71, the reformate isdirected to cooling zone 72 where the stream contactsthe vertical fins 74 and cooling tubes 78 to lower thetemperature of the stream to between about 150°C andabout 300°C because low temperature shift catalyst 84is temperature sensitive and could possibly sinter at atemperature of above about 300°C: Cooling zone 72PCT/US97/1 4906?W0 98/087711015202530CA 02265468 1999-02-24PCT/US97/14906-174-cools high temperature reformate gas for lowtemperature shift zone 76. Cooling zone tubes 78operate continuously flooded to allow accurate andmaximum steam side heat transfer, to reduce fouling andcorrosion to allow use of contaminated water, and toachieve a constant wall minimum temperature.Reformate stream is directed through perforatedplate 86 to low temperature shift reaction zone 76where the reformate stream contacts low temperatureshift catalyst 84 converting at least a portion of the-remaining carbon monoxide gas of the reformate streamto carbon dioxide by low temperature shift reaction toform product stream. Low temperature shift reactionzone 76 operates adiabatically to reduce the remainderof the carbon monoxide to trace levels with modestcatalyst temperature rise. The resulting gas productstream exits low temperature shift reaction zone 76through perforated plate 88 to exit gas zone 90 toreformer exit 92. The exiting product stream can havea composition of about 40% hydrogen gas and less thanone percent carbon monoxide on a wet volume basis.A second embodiment of the invention is shown inFigure 2. Second reformer 100 has reformer shell 102.Reformer shell 102 has upper portion 104 and lowerportion 106. Disposed in the center of reformer shell102 is first tube 108 which extends substantially theheight of reformer shell 102. First tube 108 has afirst tube inlet 110 at lower portion 106 for receivinggases into first tube 108. First tube 108 isconfigured for receiving a first mixture of oxygen andfirst hydrocarbon fuel. First tube outlet 112 is?WO 98/087711015202530CA 02265468 1999-02-24-1LS..configured for directing a first reaction reformate ofthe first mixture to mixing zone 114.Second tube 116 is annularly disposed about firsttube 108.for receiving second hydrocarbon fuel and steam.Second tube 116 has second tube inlet 118Second tube 116 also has second tube outlet 120 fordirecting a second reaction reformate of a secondmixture. Second tube 116 can include a steam reformingcatalyst. An example of a suitable catalyst includesnickel with amounts of a noble metal such as cobalt,platinum, palladium, rhodium, ruthenium, iridium, and asupport such as magnesia, magnesium aluminate, alumina,silica, zirconia, singly or in combination.Alternatively, steam reforming catalyst can be a singlemetal, such as nickel, supported on a refractorycarrier like magnesia, magnesium aluminate, alumina,silica, or zirconia, singly or in combination, promotedby an alkali metal like potassium. In anotherembodiment, second tube 116 can be annularly disposedwithin first tube 108,directed into the center tube and fuel and oxygen canwherein steam and fuel can bebe directed into the tube annularly disposed around thecenter tube. 'Oxygen source 122 is connected by oxygen tube 124to first tube 108. An example of a suitable oxygensource is oxygen gas or air. Steam source 126 isconnected to second tube 116 by steam tube 128. In oneembodiment, steam source 126 can provide a source ofsteam at a temperature of about 150°C and a pressure ofabout 60 psia.PCT/US97/ 14906?W0 98/087711O15202530CA 02265468 1999-02-24PCT/U S97/ 14906-16..Fuel source 130 is connected by fuel tube 132 toFuel source 130 includes a suitableJP-8,fractionator 134.fuel,kerosene, also alcohol including methanol and ethanol.such as a hydrocarbon, including gasoline,Fractionator 134 has light portion outlet 136 fordirecting light portion from fractionator 134 and heavyportion outlet 138 for directing heavy portion fromfractionator 134. Heavy portion can be directed fromheavy portion outlet 138 through heavy portion tube 140to first tube inlet 110.from light portion outlet 138 through light portionLight portion can be directedtube 142 to second tube inlet 118. In anotherembodiment, separate sources can be used for heavyportion (first hydrocarbon fuel) and light portion(second hydrocarbon fuel) without having afractionator.Catalyst reforming zone 144 is annularly disposedabout second tube 116§ First reaction reformate andsecond reaction reformate can be directed through firsttube outlet 112 and second tube outlet 120,respectively, to mixing zone 114 above catalystreforming zone 144.Catalyst reforming zone 144 includes a catalystfor further reforming of the mixtures to hydrogen gas.An example of a suitable catalyst includes nickel withamounts of a noble metal such as cobalt, platinum,palladium, rhodium, ruthenium, iridium, and a supportsuch as magnesia, magnesium aluminate, alumina, silica,zirconia, singly or in combination. Alternatively, thecatalyst can be a single metal, such as nickel,supported on a refractory carrier like magnesia,?WO 981087711015202530CA 02265468 1999-02-24PCT/U S97/ 14906-17-magnesium aluminate, alumina, silica, or zirconia,singly or in combination, promoted by an alkali metal-like potassium. Catalyst reforming zone 144 can have aheight that is substantially the length of first tube108 and second tube 116. Catalyst reforming zone 144is sufficiently porous to allow passage of gas fromexit zone 146. Catalyst 147 in catalyst reforming zone144 is held in place by lower perforated plate 148 andupper perforated plate 150. Product gases of catalystreforming zone 144 can exit second reformer 100 fromexit zone 146 through reformer shell exit 152.In the second embodiment of the invention forconverting hydrocarbon fuel into hydrogen gas anda fuel is directed from fuel source 130The fuel isseparated into a light portion and a heavy portion incarbon dioxide,to fractionator through fuel tube 132.fractionator 134. The heavy portion is directed fromheavy portion outlet 138 through heavy portion tube 140to first tube inlet 110. An oxygen—containing gas,such as air, is directed from oxygen source 122 throughoxygen tube 124 to first tube inlet 110. The oxygen-containing gas and the heavy portion of the hydrocarbonfuel form a mixture in first tube, whereby thehydrocarbon fuel of the first mixture spontaneouslypartially oxidizes to form a first heated reformatestream that includes hydrogen gas and carbon monoxide.First heated reformate stream can be heated to about1, 525°C.depending upon the type of fuel used.The ratio of fuel to oxygen is adjustedA heavier fuelThepartial oxidation of the fuel results in the fuelcan require a higher combustion temperature.?1015202530CA 02265468 1999-02-24WO 98/08771 PCT/US97/14906-18-mixture that includes carbon monoxide, water, hydrogengas and methane. Excess heat from the partialoxidation reaction allows transfer of heat from firsttube 108 to second tube 116. By burning the heavyportion at a temperature of above about l,375°C, thereis no significant formation of carbon soot or tar inthe partial oxidation zone. If necessary, ignition canbe with a hot surface igniter or a spark plug.The light portion of the fuel is directed fromlight portion outlet 136 of fractionator 134 throughlight portion tube 142 to second tube 116. Steam isdirected from steam source 126 through steam tube 128to second tube inlet 118 into second tube 116. Alsooxygen gas is directed from oxygen source 122 throughoxygen tube 124 to second tube inlet 118 into secondtube 116.directed with a light portion of hydrocarbon fuel intoIn another embodiment, only steam issecond tube. A second mixture of oxygen—containinggas, a light portion of hydrocarbon fuel and steam isformed in second tube 116 annularly disposed aboutfirst tube 108.partially reacts to form a second heated reformateHydrocarbon fuel of second mixturestream that includes hydrogen gas and carbon monoxide.In the presence of steam, second mixture partiallysteam reforms. The heat from the reaction in firsttube 108 provides energy to help cause the reaction toprogress in second tube 116.The first heated reformate stream from first tube108 and second heated reformate stream from second tube116 are directed through first tube outlet 112 andsecond tube outlet 120,respectively, into mixing zone?CA 02265468 1999-02-24WO 98/08771 PCT/US97/14906_ 1 9 _114. The separate tubes allow carbon reduced operation1015202530at high fuel to oxygen ratios of about four to one. Italso allows using distillate fuels, such as gasoline,diesel fuel, jet fuel or kerosene, whereby heavyportion type fuels are preferentially directed to firsttube 108 for high—temperature combustion necessary tobreak heavy molecules while the light portion—typevapors are directed to second tube 116 for partialsteam reforming as a result of thermal contact withcombustion chamber. First heated reformate stream andsecond heated reformate stream mix within mixing zone114. The mixture is directed from mixing zone 114through catalyst reforming zone 144 to exit zone 146.In catalyst reforming zone 144, the remainder of thecarbon monoxide is reformed to carbon dioxide to formproduct stream. The product stream exits through exitzone 146 and from second reformer 100 through reformershell exit 152.Another embodiment of the invention is shown in‘Figure 3. Third reformer 200 has reformer shell 202.Reformer shell 202 has upper portion 204 and lowerportion 206. Disposed in the center of reformer shell202 is first tube 208. First tube 208 has a first tubeinlet 210 at lower portion 206 for receiving gases intofirst tube 208. First tube 208 has first tube outlet212 at upper portion 204 for gases to exit first tube208.214 for reforming a hydrocarbon in the presence ofFirst tube 208 includes steam reforming catalyststeam. An example of a suitable steam reformingcatalyst is nickel with amounts of a noble metal suchas cobalt, platinum, palladium, rhodium, ruthenium,?1015202530CA 02265468 1999-02-24WO 98/08771 PCTIU S97/ 14906.._20 _.iridium, and a support such as magnesia, magnesiumaluminate, alumina, silica, zirconia, singly or incombination. Alternatively, steam reforming catalystcan be a single metal, such as nickel, supported on arefractory carrier like magnesia, magnesium aluminate,singly or in combination,First tubealumina, silica, or zirconia,promoted by an alkali metal like potassium.208 is configured for receiving a mixture of steam anda first hydrocarbon or alcohol fuel. First tube outlet212 is configured for directing a first reactionreformate of the first mixture to mixing zone 216.First tube 208 can be uniform in diameter, oralternatively, the tube can be tapered such as having asmaller diameter at first tube inlet 210 than thediameter at first tube outlet 212.Steam source 213 is connected to first tube 208 bysteam tube 215. Steam source 213 can provide a sourceof steam at a temperature of about 150°C and a pressureof about 60 psia. Light fuel source 217 is connectedby light fuel tube 219 to first tube 208 for directinglight fuel into first tube 208. Light fuel includes asuitable fuel such as a hydrocarbon, includingJP-8,methanol and ethanol.gasoline, kerosene, also alcohol includingSecond tube 218 is annularly disposed about firsttube 208 .for receiving a mixture of oxygen and heavy hydrocarbonfuel.for directing a second reaction reformate of a secondSecond tube 218 has second tube inlet 220Second tube 218 also has second tube outlet 222mixture. Second tube 218 can have a uniform diameterlength of second tube 218, or alternatively second tube?WO 98/0877]1015202530CA 02265468 1999-02-24PCTIUS97/ 14906.. 218 can be tapered, such as having a larger diameter atlower portion 206 and narrower diameter at upperportion 204. Second tube outlet 222 is configured fordirecting a second reaction reformate of the secondmixture to mixing zone 216.Annularly disposed about second tube is third tube224. Third tube 224 has third tube inlet 226 proximateto mixing zone 216 for receiving a mixture of firstreaction reformate of the first mixture and secondThird tube224 has third tube outlet 228 for directing mixture ofreaction reformate of the second mixture.first reaction reformate and second reaction reformatefrom third tube 224. Third tube 224 can include steamreforming catalyst 225 for further reforming thehydrocarbon present in the mixture. An example of asuitable steam reforming catalyst includes the samecatalyst described for steam reforming catalyst 214.Helical tube 232 extends about the length of thirdtube 224. First end 234 of helical tube 232 is locatedat inlet housing 233. Oxygen source 242 is connectedto inlet housing 233 by conduit 235 with first endinlet 236 for receiving oxygen—containing gas fromSecond end 247 of helical tube232 has helical tube outlet 244 for directing oxygen-oxygen gas zone 240.containing gas into second tube 218. Examples ofsuitable oxygen—containing gas include oxygen (d?,air, etc.Heavy fuel source 241 is connected by heavy fueltube 243 to heavy fuel inlet 246. Heavy fuel inlet 246is joined to helical tube 232 proximate to second end247. Examples of suitable heavy fuels include?WO 981087711015202530CA 02265468 1999-02-24PCT/US97/14906-22-gasoline, kerosene, JP-8, methanol and ethanol. Inanother embodiment, the same sources of fuel can beused for heavy fuelfuelfractionator,(first hydrocarbon fuel) and light(second hydrocarbon fuel). Alternatively, aas described in Figure 2, can be used tosupply a heavy fuel and a light fuel. In anotherembodiment, the light fuel and heavy fuel can be thesame and can come from the same source.Vessel 252 is annularly disposed about third tube224.from third tube outlet 228 into vessel 252.Vessel inlet 254 can direct reformate productsHelicaltube 232 is disposed between vessel 252 and third tube224 and gases from third tube 224 can be directedthrough vessel 252 from vessel inlet 254 over andaround helical tube 232 to vessel outlet 256. Flowdistribution region 258 conducts gas from vessel outlet256 to catalyst reforming zone 260. Additional steamcan be added through second steam inlet 257 to provideadded cooling and water for reforming.Catalyst reforming zone 260 is annularly disposedabout vessel 252. Catalyst reforming zone 260 includescatalyst 262 for further shifting the reformate toAn example of a suitable catalyst(Fe,O,)Other types of high temperature shift catalysts includehydrogen gas.includes ferric oxide and chromic oxide (crgx).iron oxide and chromium oxide promoted with copper,iron silicide, supported platinum, supported palladium,and other supported platinum group metals, singly andin combination. The catalyst can be in powdered formand have a height substantially the height of vessel252. Catalyst reforming zone 260 is sufficiently?1015202530WO 98/08771CA 02265468 1999-02-24PCT/US97/14906-23-porous to allow passage of gas from flow distributionregion 258 to exit zone 268. Catalyst 262 in catalystreforming zone 260 is held in place by lower perforatedplate 264 and upper perforated plate 266. Productgases of catalyst reforming zone 260 can exit thirdreformer 200 from exit zone 268 through reformer shellexit 270 .In a third embodiment of the invention forconverting hydrocarbon or alcohol fuel into hydrogengas and carbon dioxide, a fuel is directed from lightfuel source 217 through light fuel tube 219 to firsttube inlet 210.213 through steam tube 215 to tube inlet 210 into tube208.form a first heated reformate stream that includesFirst heatedreformate stream is directed from first tube 208Steam is directed from steam sourceLight fuel partially reacts with the steam tohydrogen gas and carbon monoxide.through first tube outlet 212 to mixing zone 216.An oxygen containing gas, such as air, is directedfrom oxygen source 242 through conduit 235 to inlethousing 233 to oxygen gas zone 240 into first end inlet236 of helical tube 232.such as air,450°C.velocity of greater than about 40 meters per second.The oxygen containing gas,is preheated to a temperature of aboutIn a preferred embodiment, the air has aAs oxygen containing gas is directed through helicaltube 232,heavy fuel source 241 through heavy fuel tube 243.a suitable heavy fuel vapor is directed fromExamples of suitable heavy fuels include JP—8, keroseneand other hydrocarbon fuels typically used insuch as methane andreformers. Gaseous hydrocarbons,?CA 02265468 1999-02-24wo 93/03771 PCT/US97ll4906_ 2 4 _propane, can also be used. The oxygen—containing gas1015202530and heavy fuel are fed at rates sufficient to mixwithin helical tube 232 and spontaneously partiallyoxidize as the mixture enters second tube 218 throughsecond tube inlet 220 to form a heated second reformatestream that includes steam, carbon monoxide and oxygengas. In a preferred embodiment, oxygen—containing gasis tangentially directed around the interior of secondtube 218. A hydrocarbon fuel of second mixturepartially reacts to form a second heated reformatestream that includes hydrogen gas and carbon monoxide.The heat in second tube 218 provides energy to causethe reaction to progress in first tube 208.The fuel that is fed into first tube 208 andsecond tube 218 may or may not be about equal inSecond tube 218,chamber, is operated at a ratio of about two to one,amount. the partial oxidationfuel to oxygen gas, for example, with a temperature ofl375°C.tube 208 can cause partial steam reforming inabout Heat transfer from second tube 218 tofirsttube 208 while the temperature is maintained at925°C.kerosene, the lighter fuel ends are prevaporizedfirstabout For liquid fuels, such as gasoline andlightfor delivery to first tube 208. Heavy fuels are burnedin the partial oxidation zone where high temperature(about 1375°C)carbonization.can break down fuel with minimalThe first heated reformate stream from first tube208 and second heated reformate stream from second tube218 are directed to first tube outlet 212 and secondrespectively,tube outlet 222, into mixing zone 216.?1015202530CA 02265468 1999-02-24W0 98/03771 PCT/US97ll4906-25-The separate tubes allow carbon reduced operation athigh fuel to oxygen ratios of about four or five toIt allows usingone, thereby reducing soot formation.distillate fuels, wherebysuch as gasoline or kerosene,heavy portion type fuels are preferentially directed tosecond tube 218 for high temperature combustionnecessary to break heavy molecules while a lightportion—type vapors are directed to first tube 208 forpartial steam reforming as a result of thermal contactwith the heated combustion from second tube 218. Firstheated reformate stream and second heated reformatestream mix within mixing zone 216. The mixture isdirected from mixing zone 216 through third tube inlet226 into third tube 224.In third tube 224, a further portion of the fuelis reformed to hydrogen and carbon monoxide to formThird tube reformateThird tubereformate products are directed through vessel inletthird tube reformate stream.stream exits through third tube outlet 228.254 into vessel 252 where the reformate stream passesover and around helical tube 232 to vessel outlet 256.Additional steam can be added to-vessel 252 throughsteam inlet 253 to provide additional cooling andfurther reform the hydrocarbon and carbon monoxidepresent in the reformate stream. The reformate streamis directed from flow distribution region 258 throughcatalyst reforming zone 260 where reformate stream isdirected through catalyst reforming zone for furtherreforming the carbon monoxide into hydrogen gas andcarbon dioxide to form product stream having acarbonconcentration of about 0.5 percent, by volume,?CA 02265468 1999-02-24W0 98/08771 PCT/US97/14906=2e~monoxide. The product stream exits through exit zone268 through shell exit 270.EguivalentsThose skilled in the art will recognize or be ableto ascertain using no more than routineexperimentation, many equivalents to the specificembodiments of the invention described specificallyherein. Such equivalents are intended to beencompassed in the scope of the claims.

Claims (41)

1. A reformer for converting a hydrocarbon fuel into hydrogen gas and carbon dioxide comprising:
a first vessel (18) having a first portion defining a partial oxidation reaction zone (24) and a first vessel inlet (20) adapted to direct reactants including oxygen-containing gas and unburned fuel tangentially into the first portion of the first vessel (18);
and, a first vessel outlet (22) disposed downstream of the partial oxidation reaction zone (24).
2. The reformer of claim 1 wherein the partial oxidation reaction zone (24) is adapted to permit reactants to flow therethrough in a substantially helical manner in response to tangentially delivered unburned fuel.
3. The reformer of claim 1 wherein the first vessel (18) includes means to ignite the reactants.
4. The reformer of claim 1 wherein the partial oxidation reaction zone (24) contains an open interior space without any catalyst.
5. The reformer of claim 1 further comprising:
a helical tube (32) disposed about the first vessel (18) and having a first end (34) for connection to an oxygen source (42) and a second end (44) for connection to the first vessel inlet (20), the helical tube (32) adapted to conduct the oxygen-containing gas from the oxygen source (42) to the first vessel (18); and, a second vessel (58) having a second vessel inlet (60) and a second vessel outlet (62), the second vessel (58) annularly disposed about the first vessel (18) and adapted to direct product gases from the first vessel (18) through the second vessel (58), wherein the helical tube (32) is interposed between the first vessel (18) and the second vessel (58).
6. The reformer of claim 1 wherein the first vessel (18) has a second portion disposed downstream of the first portion and defining a steam reforming reaction zone (26), and the first vessel outlet (22) communicates with the steam reforming reaction zone (26).
7. The reformer of claim 6 wherein the first vessel (18) includes a perforated barrier (30) interposed between the first and second portions.
8. The reformer of claim 6 further comprising:
a helical tube (32) disposed about the first vessel (18) and having a first end (34) for connection to an oxygen source (42) and a second end (44) for connection to the first vessel inlet (20), the helical tube (32) adapted to conduct the oxygen-containing gas from the oxygen source (42) to the first vessel (18); and, a second vessel (58) having a second vessel inlet (60) and a second vessel outlet (62), the second vessel (58) annularly disposed about the first vessel (18) and adapted to direct product gases from the first vessel (18) through the second vessel (58).
wherein the helical tube (32) is interposed between the first vessel (18) and the second vessel (58).
9. The reformer of claim 8 wherein the oxygen source (42) is adapted to supply air.
10. The reformer of claim 8 further comprising a conduit (53) communicating with a water source and the second vessel (58) and adapted to direct a supply of water to the second vessel (58).
11. The reformer of claim 8 wherein the helical tube (32) is connected to a fuel source (48) and is adapted to permit fuel from the fuel source (48) to mix with the oxygen-containing gas within the helical tube (32).
12. The reformer of claim 11 wherein the helical tube (32) is connected to a steam source (54) and is adapted to permit steam from the steam source (54) to mix with the fuel and the oxygen-containing gas within the helical tube (32).
13. The reformer of claim 6 wherein the steam reforming reaction zone (26) contains a first catalyst (28).
14. The reformer of claim 13 wherein the first catalyst (28) includes nickel.
15. The reformer of claim 6 further comprising a third vessel annularly disposed about the second vessel (58), the third vessel having a third vessel inlet (63) and a third vessel outlet (90) for directing product gases from the second vessel (58) through the third vessel.
16. The reformer of claim 15 wherein the third vessel has a high-temperature shift reaction zone (64) containing a second catalyst (66).
17. The reformer of claim 16 wherein the second catalyst (66) includes iron oxide.
18. The reformer of claim 18 wherein the third vessel includes a cooling zone (72).
19. The reformer of claim 18 wherein the cooling zone (72) contains a cooling tube (78) having a cooling tube inlet (80) adapted for communication with a cooling medium source and a cooling tube outlet (82).
20. The reformer of claim 19 wherein the cooling medium source is adapted to direct a liquid-phase cooling medium into the cooling tube (78) and maintain a two-phase mixture throughout substantially an entire length of the cooling tube (78) within the cooling zone (72).
21. The reformer of claim 19 wherein the cooling tube (78) is helically disposed within the cooling zone (72).
22. The reformer of claim 18 wherein the third vessel has a low-temperature shift reaction zone (76) including a third catalyst (84) and is disposed downstream of the cooling zone (72).
23. The reformer of claim 22 wherein the third catalyst (84) includes copper.
24. The reformer of claim 22 wherein the third vessel has a high-temperature shift reaction zone (64) disposed upstream of the low-temperature shift reaction zone (76) and the cooling zone (72) is interposed between the high-temperature and low-temperature shift reaction zones (64, 76).
25. A method for converting hydrocarbon fuel into hydrogen gas and carbon dioxide within a reformer comprising the steps of:
a. directing a stream including an oxygen-containing gas adjacent to a first vessel (18) to pre-heat the oxygen-containing gas by heat transfer from the first vessel (18);
b. introducing a stream including unburned fuel into the oxygen-containing gas stream to form a mixture including oxygen-containing gas and fuel:
c. directing the mixture of oxygen-containing gas and fuel tangentially into a partial oxidation reaction zone (24) within the first vessel (18); and, d. directing the mixture of oxygen-containing gas and fuel through the partial oxidation reaction zone (24) to produce a heated reformate stream including hydrogen gas and carbon monoxide.
26. The method of claim 25 further comprising the step of directing the mixture of oxygen-containing gas and fuel through the partial oxidation reaction zone (24) in a substantially helical manner.
27. The method of claim 25 further comprising the steps of introducing steam into the first vessel (18) and directing the reformate stream from the partial oxidation reaction zone (24) to a steam reforming reaction zone (26) including a first catalyst to produce additional hydrogen gas in the reformate stream.
28. The method of claim 27 further including the steps of:
directing the stream including the oxygen-containing gas from an oxygen source (42), through a helical tube (32) interposed between the first vessel (18) and a second vessel (58), and into the first vessel (18);
directing the reformate stream from the steam reforming reaction zone (26) through the second vessel (58), wherein heat energy is transferred from the reformate stream in the second vessel (58) to the stream including oxygen-containing gas in the helical tube (32).
29. The method of claim 28 further including the step of introducing water into the second vessel (58) from a water source external to the reformer.
30. The method of claim 28 further including the step of introducing the fuel stream and steam into the helical tube (32).
31. The method of claim 27 further including the step of providing a first catalyst (28) including nickel in the steam reforming reaction zone (26).
32. The method of claim 28 further comprising the step of directing the reformate stream from the second vessel (58) to a third vessel.
33. The method of claim 32 further comprising the step of directing the reformate stream through a high-temperature shift reaction zone (64) to convert a portion of the carbon monoxide of the reformate stream into carbon dioxide, wherein the high-temperature shift reaction zone (64) includes a second catalyst (66) and is disposed within the third vessel.
34. The method of claim 33 further providing the step of providing a second catalyst (66) including iron oxide in the high-temperature shift reaction zone (64).
35. The method of claim 32 further comprising the step of directing the reformate stream through a cooling zone (72) disposed in the third vessel.
36. The method of claim 35 further comprising the steps of radially extending a plurality of fins (74) between an inner wall and outer wall of the third vessel, and directing a cooling medium through a cooling tube (78) disposed within the third vessel to transfer heat from the reformate stream to the fins (74) and to the cooling medium within the cooling tube (78).
37. The method of claim 36 further comprising the step of maintaining a two-phase mixture of the cooling medium throughout substantially an entire length of the cooling tube (78) within the cooling zone (72).
38. The method of claim 36 wherein the cooling tube (78) is disposed in a helical manner within the cooling zone (72).
39. The method of claim 35 further comprising the step of directing the reformate stream from the cooling zone (72) to a low-temperature shift reaction zone (76) including a third catalyst (84) and disposed within the third vessel.
40. The method of claim 39 further comprising the step of providing a third catalyst (84) including copper within the low-temperature shift reaction zone (76).
41. The method of claim 35 further comprising the step of directing the reformate stream through a high-temperature shift reaction zone (64) disposed upstream of the cooling zone (72).
CA002265468A 1996-08-26 1997-08-25 Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide Expired - Fee Related CA2265468C (en)

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US6207122B1 (en) 2001-03-27
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US6123913A (en) 2000-09-26
US6083425A (en) 2000-07-04

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