US20040016650A1 - Electrocatalytic reformer for synthesis gas production - Google Patents
Electrocatalytic reformer for synthesis gas production Download PDFInfo
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- US20040016650A1 US20040016650A1 US10/206,837 US20683702A US2004016650A1 US 20040016650 A1 US20040016650 A1 US 20040016650A1 US 20683702 A US20683702 A US 20683702A US 2004016650 A1 US2004016650 A1 US 2004016650A1
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- C—CHEMISTRY; METALLURGY
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- 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
- C01B3/384—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 the catalyst being continuously externally heated
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/02—Apparatus characterised by being constructed of material selected for its chemically-resistant properties
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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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
- B01J19/2485—Monolithic reactors
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- 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
- H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00058—Temperature measurement
- B01J2219/00063—Temperature measurement of the reactants
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00132—Controlling the temperature using electric heating or cooling elements
- B01J2219/00135—Electric resistance heaters
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- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00191—Control algorithm
- B01J2219/00193—Sensing a parameter
- B01J2219/00195—Sensing a parameter of the reaction system
- B01J2219/002—Sensing a parameter of the reaction system inside the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00191—Control algorithm
- B01J2219/00211—Control algorithm comparing a sensed parameter with a pre-set value
- B01J2219/00213—Fixed parameter value
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00191—Control algorithm
- B01J2219/00222—Control algorithm taking actions
- B01J2219/00227—Control algorithm taking actions modifying the operating conditions
- B01J2219/00238—Control algorithm taking actions modifying the operating conditions of the heat exchange system
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/02—Apparatus characterised by their chemically-resistant properties
- B01J2219/025—Apparatus characterised by their chemically-resistant properties characterised by the construction materials of the reactor vessel proper
- B01J2219/0277—Metal based
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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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0215—Coating
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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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
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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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
- C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
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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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
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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
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1005—Arrangement or shape of catalyst
- C01B2203/1023—Catalysts in the form of a monolith or honeycomb
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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
- 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
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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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
Definitions
- This invention relates to a method of and an apparatus for the chemical conversion of liquid, vapor or gaseous hydrocarbons.
- This invention relates to a method of and an application for the chemical reaction of liquid, vapor, or gaseous hydrocarbons with either water or water vapor and/or either air or oxygen, into hydrogen-rich reaction gases for use in fuel cells, among other devices.
- Fuel cells are an interesting option for the provision of a decentralized energy supply and for use in vehicles.
- hydrogen is converted in an electrochemical process with a high degree of efficiency directly into electric current.
- gaseous e.g., natural gas
- liquid e.g., methanol, benzine, diesel, propane/butane mixtures
- hydrocarbons with one of: water or water vapor (steam reforming); air or oxygen (partial oxidation); or a combination of these two processes (auto thermal reforming), are turned into hydrogen-rich gases.
- a considerable disadvantage of steam reforming is its inherent bad cold start performance and its sluggish transitional properties when there are load variations, since the energy required for the reaction, e.g., using a burner, must be supplied from the exterior.
- the catalytic converter and the housing must first be brought to the required operating temperature.
- the required time, during which the reformer delivers a product gas with a composition unacceptable for the electrochemical process depends on the thermal capacity of the materials to be heated up.
- So-called cold spots are a further disadvantage, in which, because of the low temperatures present, there could be less conversion, and as a result, formation of increased quantities of carbon monoxide as well as soot formation.
- gas proof or porous silicon carbide SiC is used as a catalyst carrier.
- Its advantageous thermo mechanical and electrical properties are, among other things, described in [ 2 ], [ 3 ], and [ 4 ].
- the latter is used to always ensure optimal thermal conditions either in the reformed or on the catalytically coated surface, preferably in a honeycomb shape.
- the heat necessary for the chemical reaction can be partially or completely covered by providing Joule heat, that is, from the conversion of electrical energy into heat within the SiC matrix.
- this device will be called an electrocatalytic reformer (ECR) for short.
- ECR electrocatalytic reformer
- FIG. 1 shows schematically an electrocatalytic reformer (ECR) in accordance with the first embodiment of the present invention, in partial section;
- FIG. 2 shows a second embodiment of the present invention including a plurality of electrocatalytic reformer elements arranged in a reaction vessel;
- FIG. 3 shows a variant of the embodiment of FIG. 2, showing an alternative flow configuration
- FIG. 4 shows, schematically, a circuit, including an electrocatalytic reformer in accordance with the present invention and a fuel cell stack;
- FIG. 5 shows a further embodiment of a circuit including an electrocatalytic reformer in accordance with the present invention and a fuel cell stack.
- FIG. 1 shows one possible embodiment of an electrocatalytic reformer (ECR) element, in accordance with the present invention.
- ECR element is made of either silicon or silicon carbide and is preferably shaped like a pipe and has inner and outer pipes.
- the silicon carbide SiC is porous and has a surface catalytically coated with at least one Group VIII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt), as well as Cu and Zn and their combinations to promote the endothermal reforming reactions.
- Group VIII metals of the periodic table Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt
- the porous pipe is an inner pipe indicated at 10 and is enclosed by a non-porous outer pipe 12 , that is a gastight pipe made of metal or ceramic, which can be catalytically coated on its outer surface with the Group VIII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Ir, Pt), as well as Cu and Zn and their combinations, to promote any exothermal reactions of the anode exhaust gas with air or oxygen, which take place on the outer surface thereof, as detailed in FIG. 2.
- the Group VIII metals of the periodic table Fe, Co, Ni, Ru, Rh, Pd, Ir, Pt
- the inner and outer pipes 10 , 12 together define an annular chamber 14 .
- One end of the inner pipe 10 is closed with a contact plug 16 , secured to the inner part 10 and forming an electrical contact therewith.
- the annular chamber 14 has an inlet provided adjacent and around the contact plug 16 .
- the annular chamber 14 is closed, and the inner pipe 10 forms an outlet 18 .
- reactants e.g. hydrocarbon and water, preferably in vapor state
- the gas and vapor then flow along the annular chamber 14 , and progressively pass through the porous inner pipe 10 , to the inside of the pipe 10 .
- the catalyst on the pipe 10 promotes reaction to generate hydrogen and carbon dioxide as a synthesized gas, as detailed above. This synthesized gas then leaves through the outlet 18 .
- the coating on the inner pipe 10 is advantageously provided on the surface, which will give optimum performance.
- it can be provided uniformly over the matrix of the porous inner pipe 10 , so that the incoming hydrocarbon and water vapor contact the catalyst as they pass through the porous inner pipe 10 , and are consequently heated.
- the heat necessary for the endothermal reaction of hydrocarbon with water can be supplied in a number of ways. It can be supplied either through simple heat emission from a gaseous or liquid heat transfer medium flowing around the outside of the outer pipe 12 , together, optionally, with exothermal reactions taking place on the outer surface of the outer pipe 12 . Additionally, the contacts provided by the contact plug 16 and the outlet 18 can be used to pass an electric current through the inner pipe 12 , to generate Joule heat, released in the SiC matrix of the pipe 12 .
- FIG. 2 shows a second embodiment of the present invention, which provides a tube assembly including a number of the ECR elements of FIG. 1, the ECR elements being designated at 20 in FIG. 2.
- the ECR elements 20 are contained within a vessel 22 .
- the vessel 22 includes a plate 24 defining a first manifold 26 .
- a first port 28 is provided for reactants or reaction components, opening into the first manifold 26 .
- a second plate 30 defines a second manifold 32 , having a second port 34 for synthesized gas.
- the port 28 and manifold 26 form an inlet port and an inlet manifold
- the second manifold 32 and the second port 34 form an outlet manifold and an outlet port.
- the ECR elements 20 are mounted in the plates 24 , 30 and hence a chamber 36 is defined around the ECR elements 20 .
- An exhaust gas inlet 38 and an exhaust gas outlet 40 are provided, for forcing a mixture of exhaust gas and air through the chamber 36 .
- the individual ECR elements 20 function as described for FIG. 1.
- a mixture of hydrocarbon and water is delivered through the first or inlet port 28 and through the first or inlet manifold 26 into the annular chambers 14 of the various ECR elements 20 as shown by the arrows 42 .
- the reactants then flow through the porous inner tubes of the elements 20 and out of the elements 20 into the second or outlet manifold 32 (arrows 44 ), as synthesized gas, so the synthesized gas then exhausts from the vessel 22 through the second or outlet port 34 .
- a stream of gas comprising hydrogen containing anode exhaust gas and air, or a hot exhaust gas from a catalytic burner is delivered to the exhaust gas inlet 38 .
- This gas flows around the exterior of the ECR elements 20 and out through the exhaust gas outlet 40 .
- the outside of the ECR elements 20 can be provided with the catalytic coating mentioned above, to promote reaction of remaining hydrogen with oxygen from the air, both to consume the hydrogen and to generate additional heat to heat the ECR elements 20 .
- the gas delivered to the inlet 30 is from a catalytic burner, then any excess hydrogen will already have been consumed and heat generated, so that the gas should be at a higher temperature, suitable for heating the ECR elements 20 .
- the reactive substances can include hydrogen, carbon monoxide and hydrocarbons.
- FIG. 3 shows an apparatus similar to that of FIG. 2, and for simplicity and brevity, like components are given the same reference numeral and the description of these components is not repeated.
- the flow of the reaction substances or components is reversed.
- the second inlet 34 and second manifold 32 receive the incoming reactive substances, as indicated by the arrows 48 .
- the incoming reaction components then flow along the inside of the tubes 10 of the ECR elements 20 , through the porous SiC matrix to the outer annular chambers of the ECR elements 20 .
- the components react as before on a catalyst coated on the surface of the inner pipes 10 , to form the synthesized gas.
- the synthesized gas then exits from the annular chambers to the first manifold 26 and out through the first port 28 , as indicated by the arrows 50 .
- the first manifold 26 and the first port 28 forms an outlet manifold and an outlet port in this embodiment.
- the catalytic coating on the pipes 10 can again be located to optimize performance.
- the coating is provided uniformly over the matrix of the inner pipes 10 , so that the reaction components are heated, by passage through the SiC matrix, during which they contact the catalyst .
- exhaust gases as detailed above for FIG. 2, can be passed around the outside of the ECR elements 20 , to heat the outside of the elements 20 . This provides radiant heat that serves to heat the outside of the pipes 10 , further promoting the endothermic reaction of the reaction components.
- the invention is applicable not just to the tubular bodies described as examples but basically to any shaped bodies, for examples, plates or blocks that the reactants pass over and/or flow thorough.
- the catalytic coating may cover the entire porous surface.
- FIG. 4 shows, schematically, a circuit incorporating a fuel cell stack and an electrocatalytic reformer in accordance with the present invention.
- the circuit or arrangement is indicated generally by the reference 60 , and includes an electrocatalytic reformer 62 and a fuel cell stack 64 .
- a process control computer 66 is connected, directly or indirectly, to various components of the circuit, for control thereof, and the function of the computer 66 is detailed below.
- a water supply 68 and a methanol supply 70 are connected to a pump 72 .
- a pump 72 In known manner, appropriate valves, pumps and the like would be provided to ensure delivery of required water and methanol, or other hydrocarbon, at suitable pressures and flow rates.
- the pump 72 is controlled by a load signal indicated at 74 .
- the water and methanol mixture then pass through a flow meter 76 , to a heat exchanger 78 , in which the water and methanol are heated.
- the water and methanol flow to the electrocatalytic reformer 62 , which is indicated schematically includes a plurality of ECR elements 20 .
- the electrocatalytic reformer 62 the water and methanol are reacted to form a synthesized gas comprising mainly hydrogen and carbon dioxide.
- the synthesized gas then passes to the anode of the fuel cell stack 64 .
- an oxidant would be supplied to the cathode of the fuel cell stack 64 .
- Exhausted anode gas flows along a line 80 to a catalytic burner 82 .
- the burner 82 also has inlets 84 and 86 for air and methanol.
- air is provided for this purpose, and additional methanol can be supplied, to ensure full consumption of all residual reactive components and generation of sufficient heat.
- the heated gas is then passed to the heat exchanger 78 , for heating the incoming methanol and water, and finally, the anode gas is exhausted as indicated at 88 .
- sensors can be provided. Exemplary sensors are shown. Thus, temperature sensors are indicated at 90 , for monitoring the temperature of the incoming methanol and water mixture both upstream and downstream from the electrocatalytic reformer 62 , and also the temperature within the electrocatalytic reformer 62 .
- a pressure sensor is indicated at 92 , and a flow sensor 76 / 94 .
- a power source 96 is connected to the electrocatalytic reformer, for supplying power to the individual elements thereof, to generate heat, as described above.
- the various sensors 90 , 92 and 94 , and also the power supply 96 are connected to the process control computer 66 . It will also be understood that the computer 66 could be connected to other sensors, and other control elements, for example, the load signal 74 .
- the process control computer 66 can constantly control the temperature in the electrocatalytic reformer 62 .
- the specific electrical resistance of the reformer 62 can be measured as an indication of its temperature.
- the electrical energy supplied to the electrocatalytic reformer 62 can be adjusted such that the reaction temperature in the reformer 62 is maintained in the optimal range.
- FIG. 5 shows a variant of the system or circuit of FIG. 4. Again, for simplicity and brevity, like components are given the same reference numeral and the description of these components is not repeated.
- the system of FIG. 5 is indicated generally by the reference 100 .
- thermocatalytic reformer 102 This provides for reformation of the methanol and water mixture, to generate hydrogen and carbon dioxide by use of catalysts and heat supplied from a catalytic burner 104 .
- the anode exhaust line 80 is connected to the catalytic burner 104 , together with inlets 106 for air and 108 for methanol.
- residual hydrocarbons and the like, together with added methanol are consumed in the catalytic burner 104 , to generate carbon dioxide, water and heat.
- Resultant waste gas is exhausted at 110 and heat is transferred as indicated schematically, to the thermocatalytic reformer 102 .
- the electrocatalytic reformer 62 then acts merely as a booster reformer, to carry out any residual reformation required. Its size and dimensions can be adjusted accordingly.
- the electrocatalytic reformer 62 provides two main functions here. Firstly, it provides a security function, to assure an optimal composition of the synthesized gas flowing to the fuel cell stack, on account of the ability to adjust its reaction conditions to an optimal state. Secondly, the “booster” function of the electrocatalytic reformer 62 is in a sense that, on account of its high internal dynamics, it can respond much faster to change in demand by the fuel stack 64 as compared to the thermocatalytic reformer 102 .
- the individual ECR elements 20 are preferably made of a ceramic, more preferably silicon or silicon carbide, which preferably is in the shape of a monolithic honeycomb structure.
- the elements 20 can also be formed from wire meshes of a suitable metal, for example, an aluminum-chrome-iron alloy, these meshes can be provided in the form of a rolled up sheet.
- the elements 20 are formed from silicon or silicon carbide, it is preferred for the material to have porosity in the range of 20 to 80%, more preferably in the range of 40 to 70%, with an electrical resistance in the range 0.001 ⁇ cm to 10 M ⁇ cm.
- the ceramic is formed as a porous, lateral, flowable pipe.
- a catalyst selected from the Group VIII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt), Cu and Zn. It will be understood that the catalyst can comprise combinations of two or more of these metals, for promoting endothermal reforming reactions.
- the outer pipe 12 can also be coated with a catalyst selected from the same group of metals in the same manner. It is preferably coated on the outside, to provide a catalyst for conversion of anode exhaust gases; it is also possible to consider coating the outer pipe 12 on the inside thereof, to enhance a catalytic reformation of the incoming reactive components.
Abstract
The invention relates to a method and devices for the chemical reaction of liquid, vapor or gaseous hydrocarbons with either water or water vapor and either air or oxygen, to produce a hydrogen-rich synthesized gas for use in fuel cells. In the process, the chemical reaction of the reactants takes place on the catalytically coated surface of a material that is electrically conductive, and as a consequence of the feeding an electrical voltage, directly heatable and consequently temperature-controllable.
Description
- This invention relates to a method of and an apparatus for the chemical conversion of liquid, vapor or gaseous hydrocarbons.
- This invention relates to a method of and an application for the chemical reaction of liquid, vapor, or gaseous hydrocarbons with either water or water vapor and/or either air or oxygen, into hydrogen-rich reaction gases for use in fuel cells, among other devices.
- Fuel cells, particularly PEM fuel cells, are an interesting option for the provision of a decentralized energy supply and for use in vehicles. In fuel cells, hydrogen is converted in an electrochemical process with a high degree of efficiency directly into electric current. For various reasons, hydrogen is often not used directly when operating fuel cells, but is produced from gaseous (e.g., natural gas) or liquid (e.g., methanol, benzine, diesel, propane/butane mixtures) hydrocarbons in a chemical reaction taking place prior to the electrochemical process. In the process, the hydrocarbons, with one of: water or water vapor (steam reforming); air or oxygen (partial oxidation); or a combination of these two processes (auto thermal reforming), are turned into hydrogen-rich gases.
- In terms of the hydrogen yield, which is important for the overall efficiency of a fuel cell, steam reforming is superior to the other, abovementioned methods. For instance, methanol is, in the steam reforming process, ideally completely turned into carbon dioxide and hydrogen in the presence of a catalytic converter (nickel or platinum), in accordance with the following overall reaction.
- 2 CH3OH+2H2O→2 CO2+6 H2.
- Steam reforming is endothermic, and for methanol, takes place at approx. 300° C. [1]. If natural gas is used, the temperatures are around 700 to 800° C.
- A considerable disadvantage of steam reforming is its inherent bad cold start performance and its sluggish transitional properties when there are load variations, since the energy required for the reaction, e.g., using a burner, must be supplied from the exterior. In the process, the catalytic converter and the housing must first be brought to the required operating temperature. The required time, during which the reformer delivers a product gas with a composition unacceptable for the electrochemical process, depends on the thermal capacity of the materials to be heated up. So-called cold spots are a further disadvantage, in which, because of the low temperatures present, there could be less conversion, and as a result, formation of increased quantities of carbon monoxide as well as soot formation.
- It is therefore desirable to eliminate, to the greatest possible extent, the previously described disadvantages that may incidentally also appear in more or lesser form in the other mentioned methods of hydrogen generation.
- In the present invention, gas proof or porous silicon carbide SiC is used as a catalyst carrier. Its advantageous thermo mechanical and electrical properties are, among other things, described in [2], [3], and [4]. Its high temperature resistance (in reducing atmosphere, up to 2000° C.), paired with a good thermal and electrical conductivity, stands out, in particular. By applying an appropriate electrical voltage, the latter is used to always ensure optimal thermal conditions either in the reformed or on the catalytically coated surface, preferably in a honeycomb shape. Depending on the operating state, the heat necessary for the chemical reaction can be partially or completely covered by providing Joule heat, that is, from the conversion of electrical energy into heat within the SiC matrix. In the following, this device will be called an electrocatalytic reformer (ECR) for short.
- For a better understanding of the present invention and show more clearly how it may be carried into effect, reference will now be made, by way of example, to the accompanying drawings which show preferred embodiments of the present invention and in which:
- FIG. 1 shows schematically an electrocatalytic reformer (ECR) in accordance with the first embodiment of the present invention, in partial section;
- FIG. 2 shows a second embodiment of the present invention including a plurality of electrocatalytic reformer elements arranged in a reaction vessel;
- FIG. 3 shows a variant of the embodiment of FIG. 2, showing an alternative flow configuration;
- FIG. 4 shows, schematically, a circuit, including an electrocatalytic reformer in accordance with the present invention and a fuel cell stack; and
- FIG. 5 shows a further embodiment of a circuit including an electrocatalytic reformer in accordance with the present invention and a fuel cell stack.
- FIG. 1 shows one possible embodiment of an electrocatalytic reformer (ECR) element, in accordance with the present invention. Here, the ECR element is made of either silicon or silicon carbide and is preferably shaped like a pipe and has inner and outer pipes.
- The silicon carbide SiC is porous and has a surface catalytically coated with at least one Group VIII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt), as well as Cu and Zn and their combinations to promote the endothermal reforming reactions. In the present case, the porous pipe is an inner pipe indicated at10 and is enclosed by a non-porous
outer pipe 12, that is a gastight pipe made of metal or ceramic, which can be catalytically coated on its outer surface with the Group VIII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Ir, Pt), as well as Cu and Zn and their combinations, to promote any exothermal reactions of the anode exhaust gas with air or oxygen, which take place on the outer surface thereof, as detailed in FIG. 2. - The inner and
outer pipes annular chamber 14. One end of theinner pipe 10 is closed with acontact plug 16, secured to theinner part 10 and forming an electrical contact therewith. Theannular chamber 14 has an inlet provided adjacent and around thecontact plug 16. At the other end, theannular chamber 14 is closed, and theinner pipe 10 forms anoutlet 18. - Consequently, in use, reactants, e.g. hydrocarbon and water, preferably in vapor state, flow into the inlet of the
annular chamber 14 around theplug 16. The gas and vapor then flow along theannular chamber 14, and progressively pass through the porousinner pipe 10, to the inside of thepipe 10. The catalyst on thepipe 10 promotes reaction to generate hydrogen and carbon dioxide as a synthesized gas, as detailed above. This synthesized gas then leaves through theoutlet 18. - The coating on the
inner pipe 10 is advantageously provided on the surface, which will give optimum performance. For this purpose, it can be provided uniformly over the matrix of the porousinner pipe 10, so that the incoming hydrocarbon and water vapor contact the catalyst as they pass through the porousinner pipe 10, and are consequently heated. - The heat necessary for the endothermal reaction of hydrocarbon with water can be supplied in a number of ways. It can be supplied either through simple heat emission from a gaseous or liquid heat transfer medium flowing around the outside of the
outer pipe 12, together, optionally, with exothermal reactions taking place on the outer surface of theouter pipe 12. Additionally, the contacts provided by thecontact plug 16 and theoutlet 18 can be used to pass an electric current through theinner pipe 12, to generate Joule heat, released in the SiC matrix of thepipe 12. - Reference will now be made to FIG. 2, which shows a second embodiment of the present invention, which provides a tube assembly including a number of the ECR elements of FIG. 1, the ECR elements being designated at20 in FIG. 2.
- The
ECR elements 20 are contained within avessel 22. At one end, thevessel 22 includes aplate 24 defining afirst manifold 26. Afirst port 28 is provided for reactants or reaction components, opening into thefirst manifold 26. - Correspondingly, at the other end, a
second plate 30 defines asecond manifold 32, having asecond port 34 for synthesized gas. Here, theport 28 and manifold 26 form an inlet port and an inlet manifold, while thesecond manifold 32 and thesecond port 34 form an outlet manifold and an outlet port. - The
ECR elements 20 are mounted in theplates chamber 36 is defined around theECR elements 20. An exhaust gas inlet 38 and anexhaust gas outlet 40 are provided, for forcing a mixture of exhaust gas and air through thechamber 36. - In use, the
individual ECR elements 20 function as described for FIG. 1. Thus, a mixture of hydrocarbon and water is delivered through the first orinlet port 28 and through the first orinlet manifold 26 into theannular chambers 14 of thevarious ECR elements 20 as shown by thearrows 42. The reactants then flow through the porous inner tubes of theelements 20 and out of theelements 20 into the second or outlet manifold 32 (arrows 44), as synthesized gas, so the synthesized gas then exhausts from thevessel 22 through the second oroutlet port 34. - At the same time, to provide additional heat to the
ECR elements 20, either a stream of gas comprising hydrogen containing anode exhaust gas and air, or a hot exhaust gas from a catalytic burner, is delivered to theexhaust gas inlet 38. This gas flows around the exterior of theECR elements 20 and out through theexhaust gas outlet 40. In the case of the gas flow comprising a combination of hydrogen containing anode exhaust gas and air, the outside of theECR elements 20 can be provided with the catalytic coating mentioned above, to promote reaction of remaining hydrogen with oxygen from the air, both to consume the hydrogen and to generate additional heat to heat theECR elements 20. Where the gas delivered to theinlet 30 is from a catalytic burner, then any excess hydrogen will already have been consumed and heat generated, so that the gas should be at a higher temperature, suitable for heating theECR elements 20. Where the gas mixture of air/oxygen and reactive substances is provided, the reactive substances can include hydrogen, carbon monoxide and hydrocarbons. By causing reaction of remaining reactive substances to occur on the outside of theECR elements 20, this optimizes heat transfer of the generated heat into theECR elements 20. - It will also be understood that the necessary electrical contacts would be made to the
contact plug 16 andoutlets 18 of theECR elements 20. - Reference will now be made to FIG. 3 which shows an apparatus similar to that of FIG. 2, and for simplicity and brevity, like components are given the same reference numeral and the description of these components is not repeated.
- In FIG. 3, the flow of the reaction substances or components is reversed. Thus, here the
second inlet 34 andsecond manifold 32 receive the incoming reactive substances, as indicated by thearrows 48. The incoming reaction components then flow along the inside of thetubes 10 of theECR elements 20, through the porous SiC matrix to the outer annular chambers of theECR elements 20. The components react as before on a catalyst coated on the surface of theinner pipes 10, to form the synthesized gas. The synthesized gas then exits from the annular chambers to thefirst manifold 26 and out through thefirst port 28, as indicated by thearrows 50. Thus, thefirst manifold 26 and thefirst port 28 forms an outlet manifold and an outlet port in this embodiment. - In this embodiment, the catalytic coating on the
pipes 10 can again be located to optimize performance. For this purpose, as described above the coating is provided uniformly over the matrix of theinner pipes 10, so that the reaction components are heated, by passage through the SiC matrix, during which they contact the catalyst . Additionally, exhaust gases, as detailed above for FIG. 2, can be passed around the outside of theECR elements 20, to heat the outside of theelements 20. This provides radiant heat that serves to heat the outside of thepipes 10, further promoting the endothermic reaction of the reaction components. - It is also noted that the invention is applicable not just to the tubular bodies described as examples but basically to any shaped bodies, for examples, plates or blocks that the reactants pass over and/or flow thorough. In porous bodies, the catalytic coating may cover the entire porous surface.
- For reasons of efficiency, when using an ECR, it should be ensured that the heat needed for the chemical reaction is made available only as a small, additional portion by supplying Joule heat, i.e. from the conversion of electrical energy within the heat derived from the SiC matrix. This can be ensured through an optimized heat integration of the reformer into the entire process and the implementation of dynamic energy management.
- Reference is now being made to FIG. 4, which shows, schematically, a circuit incorporating a fuel cell stack and an electrocatalytic reformer in accordance with the present invention. The circuit or arrangement is indicated generally by the
reference 60, and includes anelectrocatalytic reformer 62 and afuel cell stack 64. Aprocess control computer 66 is connected, directly or indirectly, to various components of the circuit, for control thereof, and the function of thecomputer 66 is detailed below. - A
water supply 68 and amethanol supply 70 are connected to apump 72 . In known manner, appropriate valves, pumps and the like would be provided to ensure delivery of required water and methanol, or other hydrocarbon, at suitable pressures and flow rates. Thepump 72 is controlled by a load signal indicated at 74. The water and methanol mixture then pass through aflow meter 76, to aheat exchanger 78, in which the water and methanol are heated. - From the
heat exchanger 78, the water and methanol flow to theelectrocatalytic reformer 62, which is indicated schematically includes a plurality ofECR elements 20. As detailed above, within theelectrocatalytic reformer 62, the water and methanol are reacted to form a synthesized gas comprising mainly hydrogen and carbon dioxide. The synthesized gas then passes to the anode of thefuel cell stack 64. In known manner, an oxidant would be supplied to the cathode of thefuel cell stack 64. - Exhausted anode gas flows along a
line 80 to acatalytic burner 82. Theburner 82 also hasinlets catalytic burner 82 any residual hydrogen, hydrocarbons and other combustible materials are consumed. Air is provided for this purpose, and additional methanol can be supplied, to ensure full consumption of all residual reactive components and generation of sufficient heat. The heated gas is then passed to theheat exchanger 78, for heating the incoming methanol and water, and finally, the anode gas is exhausted as indicated at 88. - To monitor and control the system, a variety of sensors can be provided. Exemplary sensors are shown. Thus, temperature sensors are indicated at90, for monitoring the temperature of the incoming methanol and water mixture both upstream and downstream from the
electrocatalytic reformer 62, and also the temperature within theelectrocatalytic reformer 62. A pressure sensor is indicated at 92, and aflow sensor 76/94. - A
power source 96 is connected to the electrocatalytic reformer, for supplying power to the individual elements thereof, to generate heat, as described above. - The
various sensors power supply 96 are connected to theprocess control computer 66. It will also be understood that thecomputer 66 could be connected to other sensors, and other control elements, for example, theload signal 74. - Accordingly, the
process control computer 66 can constantly control the temperature in theelectrocatalytic reformer 62. In addition to the sensors shown, the specific electrical resistance of thereformer 62 can be measured as an indication of its temperature. In this way, the electrical energy supplied to theelectrocatalytic reformer 62 can be adjusted such that the reaction temperature in thereformer 62 is maintained in the optimal range. More specifically, it is preferred to use “forward-looking” power regulation, i.e. anticipating future demand and adjusting thecatalytic reformer 62 accordingly. This provides a dynamic operating characteristic, without having to accept the disadvantages with respect to the degree of conversion and the composition of the synthesized gas. In effect, this requires that, when the power demand from thefuel cell stack 64 increases, simultaneously, the heating power supplied to theelectrocatalytic reformer 62 and the flow of methanol and water from thesupplies - It will also be understood that all the heating strategies for the
electrocatalytic reformer 62, as detailed at FIGS. 1, 2 and 3 can be employed simultaneously or in various combinations. - Reference will now be made to FIG. 5, which shows a variant of the system or circuit of FIG. 4. Again, for simplicity and brevity, like components are given the same reference numeral and the description of these components is not repeated. The system of FIG. 5 is indicated generally by the
reference 100. - In FIG. 5, the
heat exchanger 78 has been replaced by athermocatalytic reformer 102. This provides for reformation of the methanol and water mixture, to generate hydrogen and carbon dioxide by use of catalysts and heat supplied from acatalytic burner 104. As for the catalytic burner of FIG. 4, theanode exhaust line 80 is connected to thecatalytic burner 104, together withinlets 106 for air and 108 for methanol. Thus, again, residual hydrocarbons and the like, together with added methanol are consumed in thecatalytic burner 104, to generate carbon dioxide, water and heat. Resultant waste gas is exhausted at 110 and heat is transferred as indicated schematically, to thethermocatalytic reformer 102. - In this embodiment, the
electrocatalytic reformer 62 then acts merely as a booster reformer, to carry out any residual reformation required. Its size and dimensions can be adjusted accordingly. Thus, theelectrocatalytic reformer 62 provides two main functions here. Firstly, it provides a security function, to assure an optimal composition of the synthesized gas flowing to the fuel cell stack, on account of the ability to adjust its reaction conditions to an optimal state. Secondly, the “booster” function of theelectrocatalytic reformer 62 is in a sense that, on account of its high internal dynamics, it can respond much faster to change in demand by thefuel stack 64 as compared to thethermocatalytic reformer 102. - The
individual ECR elements 20 are preferably made of a ceramic, more preferably silicon or silicon carbide, which preferably is in the shape of a monolithic honeycomb structure. Theelements 20 can also be formed from wire meshes of a suitable metal, for example, an aluminum-chrome-iron alloy, these meshes can be provided in the form of a rolled up sheet. - Where the
elements 20 are formed from silicon or silicon carbide, it is preferred for the material to have porosity in the range of 20 to 80%, more preferably in the range of 40 to 70%, with an electrical resistance in the range 0.001 Ωcm to 10 MΩcm. - Advantageously, the ceramic, either silicon or silicon carbide, is formed as a porous, lateral, flowable pipe. In accordance with the present invention, one or both surfaces of the pipe are coated with a catalyst selected from the Group VIII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt), Cu and Zn. It will be understood that the catalyst can comprise combinations of two or more of these metals, for promoting endothermal reforming reactions.
- Similarly, the
outer pipe 12 can also be coated with a catalyst selected from the same group of metals in the same manner. It is preferably coated on the outside, to provide a catalyst for conversion of anode exhaust gases; it is also possible to consider coating theouter pipe 12 on the inside thereof, to enhance a catalytic reformation of the incoming reactive components.
Claims (22)
1. An apparatus for the chemical conversion of a hydrocarbon with at least water, to produce a hydrogen-rich synthesized gas for use in fuel cells, the apparatus including a component formed of an electrically conductive material and having a catalytically coated surface, whereby, in use, the component can be electrically heated, to promote endothermic reactions catalyzed by the catalytically coated surface.
2. An apparatus as claimed in claim 1 , wherein the component is formed from one of silicon and silicon carbide.
3. An apparatus as claimed in claim 2 , wherein the material of the component has a monolithic honeycomb structure.
4. An apparatus as claimed in claim 1 , wherein the material of the component comprises an aluminum-chrome-iron alloy.
5. An apparatus as claimed in claim 4 wherein the aluminum-chrome-iron alloy is formed as a wire mesh formed into a roll.
6. An apparatus as claimed in claim 3 , wherein the material of the component has porosity in the range 20-80%.
7. An apparatus as claimed in claim 6 , wherein the material of the component has porosity in the range 40-70%.
8. An apparatus as claimed in claim 6 , wherein the material of the component has an electrical resistance in the range 0.001 Ωcm to 10 MΩcm.
9. An apparatus as claimed in claim 2 , wherein the material of the component is provided in the form of a porous, lateral, flowable pipe.
10. An apparatus as claimed in any one of claims 1-9, wherein the catalytically coated surface of the component includes a catalyst comprising at least one metal selected from Group VII metals of the periodic table (Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, Pt), Cu and Zn.
11. An apparatus as claimed in claim 10 , wherein the catalyst comprises a combination of two or more of said metals.
12. An apparatus as claimed in claim 1 , wherein the component comprises an elongate, inner pipe, and wherein the apparatus includes an outer pipe enclosing the inner pipe and defining an annular chamber, thereby to form an electrocatalytic reformer element.
13. An apparatus as claimed in claim 12 , wherein the outer pipe is provided with a catalytic coating for promoting exothermal reactions of anode exhaust gas with at least one of air and oxygen.
14. An apparatus as claimed in claim 13 which includes a plurality of electrocatalytic reformer elements, a vessel enclosing the elements, a first port and a first manifold providing communication to the annular chambers of the electrocatalytic reformer elements, a second port and a second manifold providing communication to the interior of the inner pipes of the electrocatalytic reformer elements, a chamber around the electrocatalytic reformer elements, and third and fourth ports providing an inlet and an outlet for anodized exhaust gases around the electrocatalytic reformer elements.
15. A method of chemically converting a hydrocarbon to generate a hydrogen-rich synthesized gas, the method comprising:
(a) Providing the hydrocarbon as one of a liquid, vapor and gas;
(b) Supplying water to at least one of the liquid and vapor state;
(c) Supplying the hydrocarbon and the water to an apparatus including at least one electrocatalytic reformer element having a component with a catalytically coated surface, whereby the hydrocarbon and the water are exposed to the catalytically coated surface;
(d) Passing electric current through the component, to heat the component and to provide heat for endothermic reaction of the hydrocarbon and the water.
16. A method as claimed in claim 15 , which includes supplying a mixture of water with one of air and oxygen.
17. A method as claimed in claim 15 , that includes measuring the resistance of at least one electrocatalytic reformer element, and determining the temperature from the measured resistance.
18. A method as claimed in claim 17 , which includes adjusting the electric current to maintain said at least one reformer element at a desired temperature, and adjusting the temperature in dependence upon anticipated changes in demand for converted hydrocarbon.
19. A method as claimed in claim 15 , which includes providing the component of the electrocatalytic reformer element as a porous component, and passing the hydrocarbon and the water through the porous component.
20. A method as claimed in claim 19 , which includes providing the component as a porous pipe, and forming the catalytically coated surface on exposed surfaces of the pipe.
21. A method as claimed in claim 20 , which includes passing the hydrocarbon and the water radially inwards from the outside to the inside of the pipe.
22. A method as claimed in claim 20 , which includes passing the hydrocarbon and the water radially outwards from the inside to the outside of the pipe.
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US10/206,837 US20040016650A1 (en) | 2002-07-29 | 2002-07-29 | Electrocatalytic reformer for synthesis gas production |
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US10/206,837 US20040016650A1 (en) | 2002-07-29 | 2002-07-29 | Electrocatalytic reformer for synthesis gas production |
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011085900A1 (en) * | 2010-01-18 | 2011-07-21 | Evonik Degussa Gmbh | Catalytic systems for continuous conversion of silicon tetrachloride to trichlorosilane |
US20110200511A1 (en) * | 2010-02-12 | 2011-08-18 | Centrotherm Sitec Gmbh | Process for the hydrogenation of chlorosilanes and converter for carrying out the process |
US11505751B2 (en) | 2018-08-31 | 2022-11-22 | Dow Global Technologies Llc | Systems and processes for improving hydrocarbon upgrading |
US11566332B2 (en) | 2012-03-06 | 2023-01-31 | Board Of Trustees Of Michigan State University | Electrocatalytic hydrogenation and hydrodeoxygenation of oxygenated and unsaturated organic compounds |
US11679367B2 (en) * | 2018-08-31 | 2023-06-20 | Dow Global Technologies Llc | Systems and processes for improving hydrocarbon upgrading |
US11905173B2 (en) | 2018-05-31 | 2024-02-20 | Haldor Topsøe A/S | Steam reforming heated by resistance heating |
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US5149508A (en) * | 1989-03-06 | 1992-09-22 | W. R. Grace & Co.-Conn. | Parallel path catalytic converter |
US6221117B1 (en) * | 1996-10-30 | 2001-04-24 | Idatech, Llc | Hydrogen producing fuel processing system |
US6585940B2 (en) * | 1998-06-29 | 2003-07-01 | Ngk Insulators, Ltd. | Reformer |
-
2002
- 2002-07-29 US US10/206,837 patent/US20040016650A1/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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US5149508A (en) * | 1989-03-06 | 1992-09-22 | W. R. Grace & Co.-Conn. | Parallel path catalytic converter |
US6221117B1 (en) * | 1996-10-30 | 2001-04-24 | Idatech, Llc | Hydrogen producing fuel processing system |
US6585940B2 (en) * | 1998-06-29 | 2003-07-01 | Ngk Insulators, Ltd. | Reformer |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011085900A1 (en) * | 2010-01-18 | 2011-07-21 | Evonik Degussa Gmbh | Catalytic systems for continuous conversion of silicon tetrachloride to trichlorosilane |
US20110200511A1 (en) * | 2010-02-12 | 2011-08-18 | Centrotherm Sitec Gmbh | Process for the hydrogenation of chlorosilanes and converter for carrying out the process |
WO2011098064A1 (en) * | 2010-02-12 | 2011-08-18 | Centrotherm Sitec Gmbh | Method for hydrogenating chlorosilanes and converter for carrying out the method |
US11566332B2 (en) | 2012-03-06 | 2023-01-31 | Board Of Trustees Of Michigan State University | Electrocatalytic hydrogenation and hydrodeoxygenation of oxygenated and unsaturated organic compounds |
US11905173B2 (en) | 2018-05-31 | 2024-02-20 | Haldor Topsøe A/S | Steam reforming heated by resistance heating |
US11505751B2 (en) | 2018-08-31 | 2022-11-22 | Dow Global Technologies Llc | Systems and processes for improving hydrocarbon upgrading |
US11679367B2 (en) * | 2018-08-31 | 2023-06-20 | Dow Global Technologies Llc | Systems and processes for improving hydrocarbon upgrading |
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Owner name: HYDROGENICS CORPORATION, CANADA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:KLUG, KARL H.;REEL/FRAME:013636/0328 Effective date: 20021119 |
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