US20020090334A1 - Method for reducing the carbon monoxide content of a hydrogen rich gas - Google Patents

Method for reducing the carbon monoxide content of a hydrogen rich gas Download PDF

Info

Publication number
US20020090334A1
US20020090334A1 US10/006,876 US687601A US2002090334A1 US 20020090334 A1 US20020090334 A1 US 20020090334A1 US 687601 A US687601 A US 687601A US 2002090334 A1 US2002090334 A1 US 2002090334A1
Authority
US
United States
Prior art keywords
catalyst bed
reactor
operating temperature
carbon monoxide
desired range
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US10/006,876
Inventor
James Stevens
Curtis Krause
Doug Naae
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Texaco Inc
Original Assignee
Texaco Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Texaco Inc filed Critical Texaco Inc
Priority to US10/006,876 priority Critical patent/US20020090334A1/en
Assigned to TEXACO, INC. reassignment TEXACO, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KRAUSE, CURTIS, NAAE, DOUG, STEVENS, JAMES
Publication of US20020090334A1 publication Critical patent/US20020090334A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
    • B01J8/0488—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being placed in separate reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2475—Membrane reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
    • B01J8/0423—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
    • B01J8/048—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being superimposed one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—Catalytic partial combustion
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—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 followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04037—Electrical heating
    • 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
    • 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
    • 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
    • H01M8/0625—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 in a modular combined reactor/fuel cell structure
    • H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
    • 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
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0668—Removal of carbon monoxide or carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00141—Coils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00194—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00203—Coils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00407—Controlling the temperature using electric heating or cooling elements outside the reactor bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00415—Controlling the temperature using electric heating or cooling elements electric resistance heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00716—Means for reactor start-up
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00805—Details of the particulate material
    • B01J2208/00814—Details of the particulate material the particulate material being provides in prefilled containers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material
    • B01J2208/025—Two or more types of catalyst
    • 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
    • B01J2219/00002—Chemical plants
    • B01J2219/00018—Construction aspects
    • B01J2219/0002—Plants assembled from modules joined together
    • 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
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00083—Coils
    • 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
    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements
    • B01J2219/00135—Electric resistance heaters
    • 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
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
    • 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
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical
    • 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
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1944—Details relating to the geometry of the reactor round circular or disk-shaped spiral
    • 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
    • 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
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • 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
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/044—Selective oxidation of carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0455—Purification by non-catalytic desulfurisation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water
    • 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
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • 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
    • 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
    • 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
    • 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
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • 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
    • C01B2203/0872—Methods of cooling
    • C01B2203/0877—Methods of cooling by direct injection of fluid
    • 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
    • C01B2203/0872—Methods of cooling
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • C01B2203/0894—Generation of steam
    • 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
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • 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
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • C01B2203/1017—Packed bed of catalytic structures, e.g. particles, packing elements characterised by the form of the structure
    • 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
    • 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
    • C01B2203/1035—Catalyst coated on equipment surfaces, e.g. reactor walls
    • 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
    • C01B2203/1041—Composition of the catalyst
    • 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
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1082—Composition of support materials
    • 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
    • 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
    • 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
    • C01B2203/142—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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • C01B2203/147—Three or more purification 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
    • C01B2203/16—Controlling the process
    • C01B2203/1604—Starting up the process
    • 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
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
    • H01M8/04022—Heating by combustion
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04059—Evaporative processes for the cooling of a fuel cell
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • Fuel cells provide electricity from chemical oxidation-reduction reactions and possess significant advantages over other forms of power generation in terms of cleanliness and efficiency.
  • fuel cells employ hydrogen as the fuel and oxygen as the oxidizing agent.
  • the power generation is proportional to the consumption rate of the reactants.
  • a significant disadvantage which inhibits the wider use of fuel cells is the lack of a widespread hydrogen infrastructure. Hydrogen has a relatively low volumetric energy density and is more difficult to store and transport than the hydrocarbon fuels currently used in most power generation systems. One way to overcome this difficulty is the use of reformers to convert the hydrocarbons to a hydrogen rich gas stream which can be used as a feed for fuel cells.
  • Hydrocarbon-based fuels such as natural gas, LPG, gasoline, and diesel
  • conversion processes to be used as fuel sources for most fuel cells.
  • Current art uses multistep processes combining an initial conversion process with several clean-up processes. The initial process is most often steam reforming (SR), autothermal reforming (ATR), catalytic partial oxidation (CPOX), or non-catalytic partial oxidation (POX).
  • SR steam reforming
  • ATR autothermal reforming
  • CPOX catalytic partial oxidation
  • POX non-catalytic partial oxidation
  • the hydrogen rich gas also contains other chemical species such as nitrogen, hydrogen sulfide, carbon monoxide, carbon dioxide, and carbonyl sulfide.
  • carbon monoxide levels must be reduced greatly.
  • Catalyst enhanced water-gas shift reaction steps are generally used to reduce the carbon monoxide level to 0.1 to 0.5 mole %.
  • a common practice is to oxidize the carbon monoxide to carbon dioxide by the addition of air to the hydrogen rich product gas in the presence of catalysts that promote the oxidation of carbon monoxide over the oxidation of hydrogen to water.
  • the present invention utilizes a porous distribution tube to add air for carbon monoxide oxidation throughout the length of a catalyst bed. By distributing the air injection, hot and cold areas in the catalyst bed can be avoided, thereby improving the selectivity of the reactor to carbon monoxide oxidation.
  • One illustrative embodiment of the present invention includes a method and apparatus for reducing the carbon monoxide content of a hydrogen rich gas having a catalyst bed containing an oxidation catalyst, a porous tube positioned substantially within the catalyst bed for distributing an oxygen-containing stream throughout the catalyst bed, and a cooling jacket for maintaining the reactor operating temperature in a desired range.
  • the porous tube can be constructed as a sintered stainless steel tube or as an alumina tube or as any equivalent porous tube that is known to those of skill in the art to perform the objectives of this method and apparatus.
  • the porous tube is positioned along the catalyst bed length, or may be aligned in any orientation that one of skill in the art would appreciate to result in optimal dispersion of the oxygen-containing stream throughout the catalyst bed.
  • the reactor operating temperature is controlled by the cooling jacket from about 90° C. to about 180° C., more preferably from about 90° C. to about 150° C.
  • the cooling jacket should contain a circulating coolant that can be water, steam, or air, or, in one illustrative embodiment, the hydrocarbon fuel feed to the fuel processor for energy efficiency.
  • FIG. 1 depicts a simple process flow diagram for a fuel processor.
  • FIG. 2 illustrates an improved apparatus and method for selectively oxidizing carbon monoxide in accordance with the present invention
  • the present invention is generally directed to an improved method for reducing the carbon monoxide content of a hydrogen rich gas stream.
  • the present invention uses a porous distribution tube to add an oxygen-containing stream for the carbon monoxide oxidation throughout the length of a catalyst bed instead of one or two fixed injection points as is currently practiced. By distributing the air injection hot and cold areas in the catalyst bed can be avoided, thereby improving the selectivity of the reactor to carbon monoxide oxidation.
  • the apparatus and methods described relate to improved reduction of the carbon monoxide content of a hydrogen rich gas stream in a compact fuel processor for feeding a fuel cell.
  • Hydrogen rich gas produced from such compact fuel processors will have increasing importance in the development of fuel cells, including fuel cells used to power automotive vehicles. Accordingly, while the invention is described herein as being used in conjunction with compact fuel processors and fuel cells, the scope of the invention is not limited to such use.
  • the hydrocarbon fuel feed to a fuel processor may be liquid or gas at ambient conditions as long as it can be vaporized.
  • hydrocarbon includes organic compounds having C—H bonds that are capable of producing hydrogen from a partial oxidation or steam reforming reaction. The presence of atoms other than carbon and hydrogen in the molecular structure of the compound is not excluded.
  • suitable fuels for use in the method and apparatus disclosed herein include, but are not limited to hydrocarbon fuels such as natural gas, methane, ethane, propane, butane, naphtha, gasoline, and diesel fuel, and alcohols such as methanol, ethanol, propanol, and the like.
  • the fuel processor feeds include hydrocarbon fuel, oxygen, and water.
  • the oxygen can be in the form of air, enriched air, or substantially pure oxygen.
  • the water can be introduced as a liquid or vapor. The composition percentages of the feed components are determined by the desired operating conditions, as discussed below.
  • the fuel processor effluent stream includes hydrogen and carbon dioxide and can also include some water, unconverted hydrocarbons, carbon monoxide, impurities (e.g. hydrogen sulfide and ammonia) and inert components (e.g., nitrogen and argon, especially if air was a component of the feed stream).
  • impurities e.g. hydrogen sulfide and ammonia
  • inert components e.g., nitrogen and argon, especially if air was a component of the feed stream.
  • FIG. 1 depicts a general process flow diagram for a fuel processor.
  • One of skill in the art should appreciate that a certain amount of progressive order is needed in the flow of the reactants through the reactors disclosed herein.
  • Process step A is an autothermal reforming process in which two reactions, partial oxidation (formula I, below) and optionally also steam reforming (formula II, below), are combined to convert the feed stream F into a synthesis gas containing hydrogen and carbon monoxide.
  • Formulas I and II are exemplary reaction formulas wherein methane is considered as the hydrocarbon:
  • the partial oxidation reaction occurs very quickly to the complete conversion of oxygen added and produces heat.
  • the steam reforming reaction occurs slower and consumes heat.
  • a higher concentration of oxygen in the feed stream favors partial oxidation whereas a higher concentration of water vapor favors steam reforming. Therefore, the ratios of oxygen to hydrocarbon and water to hydrocarbon become characterizing parameters. These ratios affect the operating temperature and hydrogen yield.
  • the operating temperature of the autothermal reforming step can range from about 550° C. to about 900° C., depending on the feed conditions and the catalyst.
  • the invention uses a catalyst bed of a partial oxidation catalyst with or without a steam reforming catalyst.
  • the catalyst may be in any form including pellets, spheres, extrudate, monoliths, and the like.
  • Partial oxidation catalysts should be well known to those with skill in the art and are often comprised of noble metals such as platinum, palladium, rhodium, and/or ruthenium on an alumina washcoat on a monolith, extrudate, pellet or other support. Non-noble metals such as nickel or cobalt have been used.
  • washcoats such as titania, zirconia, silica, and magnesia have been cited in the literature.
  • additional materials such as lanthanum, cerium, and potassium have been cited in the literature as “promoters” that improve the performance of the partial oxidation catalyst.
  • Steam reforming catalysts should be known to those with skill in the art and can include nickel with amounts of cobalt or a noble metal such as platinum, palladium, rhodium, ruthenium, and/or iridium.
  • the catalyst can be supported, for example, on magnesia, alumina, silica, zirconia, or magnesium aluminate, singly or in combination.
  • the steam reforming catalyst can include nickel, preferably supported on magnesia, alumina, silica, zirconia, or magnesium aluminate, singly or in combination, promoted by an alkali metal such as potassium.
  • Process step B is a cooling step for cooling the synthesis gas stream from process step A to a temperature of from about 200° C. to about 600° C., preferably from about 300° C. to about 500° C., and more preferably from about 375° C. to about 425° C., to optimize the temperature of the synthesis gas effluent for the next step.
  • This cooling may be achieved with heat sinks, heat pipes or heat exchangers depending upon the design specifications and the need to recover/recycle the heat content of the gas stream.
  • One illustrative embodiment for step B is the use of a heat exchanger utilizing feed stream F as the coolant circulated through the heat exchanger.
  • the heat exchanger can be of any suitable construction known to those with skill in the art including shell and tube, plate, spiral, etc.
  • cooling step B may be accomplished by injecting additional feed components such as fuel, air or water. Water is preferred because of its ability to absorb a large amount of heat as it is vaporized to steam. The amounts of added components depend upon the degree of cooling desired and are readily determined by those with skill in the art.
  • Process step C is a purifying step.
  • One of the main impurities of the hydrocarbon stream is sulfur, which is converted by the autothermal reforming step A to hydrogen sulfide.
  • the processing core used in process step C preferably includes zinc oxide and/or other material capable of absorbing and converting hydrogen sulfide, and may include a support (e.g., monolith, extrudate, pellet etc.). Desulfirization is accomplished by converting the hydrogen sulfide to water in accordance with the following reaction formula III:
  • the reaction is preferably carried out at a temperature of from about 300° C. to about 500° C., and more preferably from about 375° C. to about 425° C.
  • Zinc oxide is an effective hydrogen sulfide absorbent over a wide range of temperatures from about 25° C. to about 700° C. and affords great flexibility for optimizing the sequence of processing steps by appropriate selection of operating temperature.
  • the effluent stream may then be sent to a mixing step D in which water is optionally added to the gas stream.
  • the addition of water lowers the temperature of the reactant stream as it vaporizes and supplies more water for the water gas shift reaction of process step E (discussed below).
  • the water vapor and other effluent stream components are mixed by being passed through a processing core of inert materials such as ceramic beads or other similar materials that effectively mix and/or assist in the vaporization of the water.
  • any additional water can be introduced with feed, and the mixing step can be repositioned to provide better mixing of the oxidant gas in the CO oxidation step G disclosed below.
  • Process step E is a water gas shift reaction that converts carbon monoxide to carbon dioxide in accordance with formula IV:
  • concentration of carbon monoxide should preferably be lowered to a level that can be tolerated by fuel cells, typically below 50 ppm.
  • the water gas shift reaction can take place at temperatures of from 150° C. to 600° C. depending on the catalyst used. Under such conditions, most of the carbon monoxide in the gas stream is converted in this step.
  • Low temperature shift catalysts operate at a range of from about 150° C. to about 300° C. and include for example, copper oxide, or copper supported on other transition metal oxides such as zirconia, zinc supported on transition metal oxides or refractory supports such as silica, alumina, zirconia, etc., or a noble metal such as platinum, rhenium, palladium, rhodium or gold on a suitable support such as silica, alumina, zirconia, and the like.
  • High temperature shift catalysts are preferably operated at temperatures ranging from about 300° to about 600° C. and can include transition metal oxides such as ferric oxide or chromic oxide, and optionally including a promoter such as copper or iron silicide. Also included, as high temperature shift catalysts are supported noble metals such as supported platinum, palladium and/or other platinum group members.
  • the processing core utilized to carry out this step can include a packed bed of high temperature or low temperature shift catalyst such as described above, or a combination of both high temperature and low temperature shift catalysts.
  • the process should be operated at any temperature suitable for the water gas shift reaction, preferably at a temperature of from 150° C. to about 400° C. depending on the type of catalyst used.
  • a cooling element such as a cooling coil may be disposed in the processing core of the shift reactor to lower the reaction temperature within the packed bed of catalyst. Lower temperatures favor the conversion of carbon monoxide to carbon dioxide.
  • a purification processing step C can be performed between high and low shift conversions by providing separate steps for high temperature and low temperature shift with a desulfurization module between the high and low temperature shift steps.
  • Process step F is a cooling step performed In one illustrative embodiment by a heat exchanger.
  • the heat exchanger can be of any suitable construction including shell and tube, plate, spiral, etc. Alternatively a heat pipe or other form of heat sink may be utilized.
  • the goal of the heat exchanger is to reduce the temperature of the gas stream to produce an effluent having a temperature preferably in the range of from about 90° C. to about 150° C.
  • Oxygen is added to the process in step F.
  • the oxygen is consumed by the reactions of process step G described below.
  • the oxygen can be in the form of air, enriched air, or substantially pure oxygen.
  • the heat exchanger may by design provide mixing of the air with the hydrogen rich gas.
  • the embodiment of process step D may be used to perform the mixing.
  • Process step G is an oxidation step wherein almost all of the remaining carbon monoxide in the effluent stream is converted to carbon dioxide.
  • the processing is carried out in the presence of a catalyst for the oxidation of carbon monoxide and may be in any suitable form, such as pellets, spheres, monolith, etc.
  • Oxidation catalysts for carbon monoxide are known and typically include noble metals (e.g., platinum, palladium) and/or transition metals (e.g., iron, chromium, manganese), and/or compounds of noble or transition metals, particularly oxides.
  • a preferred oxidation catalyst is platinum on an alumina washcoat. The washcoat may be applied to a monolith, extrudate, pellet or other support.
  • cerium or lanthanum may be added to improve performance.
  • Many other formulations have been cited in the literature with some practitioners claiming superior performance from rhodium or alumina catalysts. Ruthenium, palladium, gold, and other materials have been cited in the literature as being active for this use.
  • Process step G preferably reduces the carbon monoxide level to less than 50 ppm, which is a suitable level for use in fuel cells, but one of skill in the art should appreciate that the present invention can be adapted to produce a hydrogen rich product with higher and lower levels of carbon monoxide.
  • the effluent exiting the fuel processor is a hydrogen rich gas containing carbon dioxide and other constituents which may be present such as water, inert components (e.g., nitrogen, argon), residual hydrocarbon, etc.
  • Product gas may be used as the feed for a fuel cell or for other applications where a hydrogen rich feed stream is desired.
  • product gas may be sent on to further processing, for example, to remove the carbon dioxide, water or other components.
  • a compact fuel processor is of modular construction with individual modular units, which are separable, rearrangeable, and individually replaceable.
  • the present invention is an improvement to process step G described above, and utilizes a porous distribution tube to add air for the carbon monoxide oxidation throughout the catalyst bed length instead of one or two fixed injection points. By distributing the air injection hot and cold areas in the catalyst bed can be avoided.
  • air A is injected through a porous tube 210 , such as a sintered stainless steel tube manufactured by the Mott Corporation or an alumina tube as manufactured by the NGK corporation of Japan.
  • a porous tube 210 such as a sintered stainless steel tube manufactured by the Mott Corporation or an alumina tube as manufactured by the NGK corporation of Japan.
  • supply air A will enter the chamber containing a carbon monoxide selective oxidation catalyst 220 , such as that manufactured by the Engelhard Corporation.
  • the oxygen in the air will oxidize carbon monoxide and hydrogen (according to equations V and VI, above) causing the catalyst 220 and reactor 200 to warm.
  • reactor 200 can be maintained in the desired operating temperature range of from about 90° C. to about 180° C.
  • This oxidation step preferably reduces the carbon monoxide level to less than 50 ppm, which is a suitable level for use in fuel cells, but one of skill in the art should appreciate that the present invention can be adapted to produce a hydrogen rich product P with higher and lower levels of carbon monoxide.
  • one illustrative embodiment of the present invention includes a method and apparatus for reducing the carbon monoxide content of a hydrogen rich gas.
  • Such an illustrative embodiment includes a catalyst bed containing an oxidation catalyst, a porous tube positioned substantially within the catalyst bed for distributing an oxygen-containing stream throughout the catalyst bed, and a cooling jacket for maintaining the reactor operating temperature in a desired range.
  • the porous tube can be constructed as a sintered stainless steel tube or as an alumina tube or as any equivalent porous tube that is known to those of skill in the art to perform the objectives of this method and apparatus.
  • the porous tube is positioned along the catalyst bed length, or may be aligned in any orientation that one of skill in the art would appreciate to result in optimal dispersion of the oxygen-containing stream throughout the catalyst bed.
  • the reactor operating temperature is controlled by the cooling jacket from about 90° C. to about 180° C., more preferably from about 90° C. to about 150° C.
  • the cooling jacket should contain a circulating coolant that can be water, air, or the hydrocarbon fuel to the fuel processor for energy efficiency improvements.
  • the present invention is intended not only for general oxidation reactors, but is also a preferred technology selection for the carbon monoxide oxidation reactors of fuel processors. Because of the direct feed to a fuel cell, there is a great need to ensure continuous on-specification hydrogen rich gas produced from compact fuel processors.

Abstract

A method and apparatus for reducing the carbon monoxide content of a hydrogen rich gas including a catalyst bed containing an oxidation catalyst, a porous tube positioned substantially within the catalyst bed for distributing an oxygen-containing stream throughout the catalyst bed, and a cooling jacket for maintaining the reactor operating temperature in a desired range. The porous tube can be constructed as a sintered stainless steel tube or as an alumina tube or as any equivalent porous tube that is known to those of skill in the art to perform the objectives of this method and apparatus. The porous tube is generally positioned along the length of the catalyst bed in manner that optimizes dispersion of the oxygen-containing stream throughout the catalyst bed. The reactor operating temperature is controlled by a cooling jacket to from about 90° C. to about 180° C., more preferably from about 90° C. to about 150° C. The cooling jacket should contain a circulating coolant that can be water, steam, air, or the hydrocarbon fuel to the fuel processor.

Description

    BACKGROUND OF THE INVENTION
  • Fuel cells provide electricity from chemical oxidation-reduction reactions and possess significant advantages over other forms of power generation in terms of cleanliness and efficiency. Typically, fuel cells employ hydrogen as the fuel and oxygen as the oxidizing agent. The power generation is proportional to the consumption rate of the reactants. [0001]
  • A significant disadvantage which inhibits the wider use of fuel cells is the lack of a widespread hydrogen infrastructure. Hydrogen has a relatively low volumetric energy density and is more difficult to store and transport than the hydrocarbon fuels currently used in most power generation systems. One way to overcome this difficulty is the use of reformers to convert the hydrocarbons to a hydrogen rich gas stream which can be used as a feed for fuel cells. [0002]
  • Hydrocarbon-based fuels, such as natural gas, LPG, gasoline, and diesel, require conversion processes to be used as fuel sources for most fuel cells. Current art uses multistep processes combining an initial conversion process with several clean-up processes. The initial process is most often steam reforming (SR), autothermal reforming (ATR), catalytic partial oxidation (CPOX), or non-catalytic partial oxidation (POX). [0003]
  • As a practical matter, the hydrogen rich gas also contains other chemical species such as nitrogen, hydrogen sulfide, carbon monoxide, carbon dioxide, and carbonyl sulfide. For many uses, such as fuel for fuel cells or as feed to an ammonia plant, carbon monoxide levels must be reduced greatly. Catalyst enhanced water-gas shift reaction steps are generally used to reduce the carbon monoxide level to 0.1 to 0.5 mole %. For uses that require lower concentrations of carbon monoxide, a common practice is to oxidize the carbon monoxide to carbon dioxide by the addition of air to the hydrogen rich product gas in the presence of catalysts that promote the oxidation of carbon monoxide over the oxidation of hydrogen to water. As commonly practiced this method of removing carbon monoxide can result in large losses of hydrogen if the heat produced by the exothermic oxidation process is not removed since the catalysts used tend to become less specific for carbon monoxide oxidation as the temperature increases. In addition, if the temperature is too low, the carbon monoxide can deactivate the catalyst. [0004]
  • Despite the above work, there remains a need for a simple unit for use with a fuel cell—one that can produce hydrogen rich gas with minimal carbon monoxide impurity. [0005]
    • SUMMARY OF THE INVENTION
  • The present invention utilizes a porous distribution tube to add air for carbon monoxide oxidation throughout the length of a catalyst bed. By distributing the air injection, hot and cold areas in the catalyst bed can be avoided, thereby improving the selectivity of the reactor to carbon monoxide oxidation. [0006]
  • One illustrative embodiment of the present invention includes a method and apparatus for reducing the carbon monoxide content of a hydrogen rich gas having a catalyst bed containing an oxidation catalyst, a porous tube positioned substantially within the catalyst bed for distributing an oxygen-containing stream throughout the catalyst bed, and a cooling jacket for maintaining the reactor operating temperature in a desired range. The porous tube can be constructed as a sintered stainless steel tube or as an alumina tube or as any equivalent porous tube that is known to those of skill in the art to perform the objectives of this method and apparatus. The porous tube is positioned along the catalyst bed length, or may be aligned in any orientation that one of skill in the art would appreciate to result in optimal dispersion of the oxygen-containing stream throughout the catalyst bed. In one illustrative embodiment of the present invention is for the reactor operating temperature to be controlled by the cooling jacket from about 90° C. to about 180° C., more preferably from about 90° C. to about 150° C. The cooling jacket should contain a circulating coolant that can be water, steam, or air, or, in one illustrative embodiment, the hydrocarbon fuel feed to the fuel processor for energy efficiency.[0007]
    • BRIEF DESCRIPTION OF THE DRAWINGS
  • The description is presented with reference to the accompanying drawings in which: [0008]
  • FIG. 1 depicts a simple process flow diagram for a fuel processor. [0009]
  • FIG. 2 illustrates an improved apparatus and method for selectively oxidizing carbon monoxide in accordance with the present invention [0010]
    • DESCRIPTION OF ILLUSTRATIVE EMBODIMENTS
  • The present invention is generally directed to an improved method for reducing the carbon monoxide content of a hydrogen rich gas stream. In one illustrative embodiment, the present invention uses a porous distribution tube to add an oxygen-containing stream for the carbon monoxide oxidation throughout the length of a catalyst bed instead of one or two fixed injection points as is currently practiced. By distributing the air injection hot and cold areas in the catalyst bed can be avoided, thereby improving the selectivity of the reactor to carbon monoxide oxidation. In one illustrative embodiment of the present invention, the apparatus and methods described relate to improved reduction of the carbon monoxide content of a hydrogen rich gas stream in a compact fuel processor for feeding a fuel cell. Hydrogen rich gas produced from such compact fuel processors will have increasing importance in the development of fuel cells, including fuel cells used to power automotive vehicles. Accordingly, while the invention is described herein as being used in conjunction with compact fuel processors and fuel cells, the scope of the invention is not limited to such use. [0011]
  • The hydrocarbon fuel feed to a fuel processor may be liquid or gas at ambient conditions as long as it can be vaporized. As used herein the term “hydrocarbon” includes organic compounds having C—H bonds that are capable of producing hydrogen from a partial oxidation or steam reforming reaction. The presence of atoms other than carbon and hydrogen in the molecular structure of the compound is not excluded. Thus, suitable fuels for use in the method and apparatus disclosed herein include, but are not limited to hydrocarbon fuels such as natural gas, methane, ethane, propane, butane, naphtha, gasoline, and diesel fuel, and alcohols such as methanol, ethanol, propanol, and the like. [0012]
  • The fuel processor feeds include hydrocarbon fuel, oxygen, and water. The oxygen can be in the form of air, enriched air, or substantially pure oxygen. The water can be introduced as a liquid or vapor. The composition percentages of the feed components are determined by the desired operating conditions, as discussed below. [0013]
  • The fuel processor effluent stream includes hydrogen and carbon dioxide and can also include some water, unconverted hydrocarbons, carbon monoxide, impurities (e.g. hydrogen sulfide and ammonia) and inert components (e.g., nitrogen and argon, especially if air was a component of the feed stream). [0014]
  • FIG. 1 depicts a general process flow diagram for a fuel processor. One of skill in the art should appreciate that a certain amount of progressive order is needed in the flow of the reactants through the reactors disclosed herein. [0015]
  • Process step A is an autothermal reforming process in which two reactions, partial oxidation (formula I, below) and optionally also steam reforming (formula II, below), are combined to convert the feed stream F into a synthesis gas containing hydrogen and carbon monoxide. Formulas I and II are exemplary reaction formulas wherein methane is considered as the hydrocarbon: [0016]
  • CH4+½O2→2H2+CO  (I)
  • CH4+H2O→3H2+CO  (II)
  • The partial oxidation reaction occurs very quickly to the complete conversion of oxygen added and produces heat. The steam reforming reaction occurs slower and consumes heat. A higher concentration of oxygen in the feed stream favors partial oxidation whereas a higher concentration of water vapor favors steam reforming. Therefore, the ratios of oxygen to hydrocarbon and water to hydrocarbon become characterizing parameters. These ratios affect the operating temperature and hydrogen yield. [0017]
  • The operating temperature of the autothermal reforming step can range from about 550° C. to about 900° C., depending on the feed conditions and the catalyst. The invention uses a catalyst bed of a partial oxidation catalyst with or without a steam reforming catalyst. The catalyst may be in any form including pellets, spheres, extrudate, monoliths, and the like. Partial oxidation catalysts should be well known to those with skill in the art and are often comprised of noble metals such as platinum, palladium, rhodium, and/or ruthenium on an alumina washcoat on a monolith, extrudate, pellet or other support. Non-noble metals such as nickel or cobalt have been used. Other washcoats such as titania, zirconia, silica, and magnesia have been cited in the literature. Many additional materials such as lanthanum, cerium, and potassium have been cited in the literature as “promoters” that improve the performance of the partial oxidation catalyst. [0018]
  • Steam reforming catalysts should be known to those with skill in the art and can include nickel with amounts of cobalt or a noble metal such as platinum, palladium, rhodium, ruthenium, and/or iridium. The catalyst can be supported, for example, on magnesia, alumina, silica, zirconia, or magnesium aluminate, singly or in combination. Alternatively, the steam reforming catalyst can include nickel, preferably supported on magnesia, alumina, silica, zirconia, or magnesium aluminate, singly or in combination, promoted by an alkali metal such as potassium. [0019]
  • Process step B is a cooling step for cooling the synthesis gas stream from process step A to a temperature of from about 200° C. to about 600° C., preferably from about 300° C. to about 500° C., and more preferably from about 375° C. to about 425° C., to optimize the temperature of the synthesis gas effluent for the next step. This cooling may be achieved with heat sinks, heat pipes or heat exchangers depending upon the design specifications and the need to recover/recycle the heat content of the gas stream. One illustrative embodiment for step B is the use of a heat exchanger utilizing feed stream F as the coolant circulated through the heat exchanger. The heat exchanger can be of any suitable construction known to those with skill in the art including shell and tube, plate, spiral, etc. Alternatively, or in addition thereto, cooling step B may be accomplished by injecting additional feed components such as fuel, air or water. Water is preferred because of its ability to absorb a large amount of heat as it is vaporized to steam. The amounts of added components depend upon the degree of cooling desired and are readily determined by those with skill in the art. [0020]
  • Process step C is a purifying step. One of the main impurities of the hydrocarbon stream is sulfur, which is converted by the autothermal reforming step A to hydrogen sulfide. The processing core used in process step C preferably includes zinc oxide and/or other material capable of absorbing and converting hydrogen sulfide, and may include a support (e.g., monolith, extrudate, pellet etc.). Desulfirization is accomplished by converting the hydrogen sulfide to water in accordance with the following reaction formula III: [0021]
  • H2S+ZnO→H2O+ZnS  (III)
  • Other impurities such as chlorides can also be removed. The reaction is preferably carried out at a temperature of from about 300° C. to about 500° C., and more preferably from about 375° C. to about 425° C. Zinc oxide is an effective hydrogen sulfide absorbent over a wide range of temperatures from about 25° C. to about 700° C. and affords great flexibility for optimizing the sequence of processing steps by appropriate selection of operating temperature. [0022]
  • The effluent stream may then be sent to a mixing step D in which water is optionally added to the gas stream. The addition of water lowers the temperature of the reactant stream as it vaporizes and supplies more water for the water gas shift reaction of process step E (discussed below). The water vapor and other effluent stream components are mixed by being passed through a processing core of inert materials such as ceramic beads or other similar materials that effectively mix and/or assist in the vaporization of the water. Alternatively, any additional water can be introduced with feed, and the mixing step can be repositioned to provide better mixing of the oxidant gas in the CO oxidation step G disclosed below. [0023]
  • Process step E is a water gas shift reaction that converts carbon monoxide to carbon dioxide in accordance with formula IV: [0024]
  • H2O+CO→H2+C0 2  (IV)
  • This is an important step because carbon monoxide, in addition to being highly toxic to humans, is a poison to fuel cells. The concentration of carbon monoxide should preferably be lowered to a level that can be tolerated by fuel cells, typically below 50 ppm. Generally, the water gas shift reaction can take place at temperatures of from 150° C. to 600° C. depending on the catalyst used. Under such conditions, most of the carbon monoxide in the gas stream is converted in this step. [0025]
  • Low temperature shift catalysts operate at a range of from about 150° C. to about 300° C. and include for example, copper oxide, or copper supported on other transition metal oxides such as zirconia, zinc supported on transition metal oxides or refractory supports such as silica, alumina, zirconia, etc., or a noble metal such as platinum, rhenium, palladium, rhodium or gold on a suitable support such as silica, alumina, zirconia, and the like. [0026]
  • High temperature shift catalysts are preferably operated at temperatures ranging from about 300° to about 600° C. and can include transition metal oxides such as ferric oxide or chromic oxide, and optionally including a promoter such as copper or iron silicide. Also included, as high temperature shift catalysts are supported noble metals such as supported platinum, palladium and/or other platinum group members. [0027]
  • The processing core utilized to carry out this step can include a packed bed of high temperature or low temperature shift catalyst such as described above, or a combination of both high temperature and low temperature shift catalysts. The process should be operated at any temperature suitable for the water gas shift reaction, preferably at a temperature of from 150° C. to about 400° C. depending on the type of catalyst used. Optionally, a cooling element such as a cooling coil may be disposed in the processing core of the shift reactor to lower the reaction temperature within the packed bed of catalyst. Lower temperatures favor the conversion of carbon monoxide to carbon dioxide. Also, a purification processing step C can be performed between high and low shift conversions by providing separate steps for high temperature and low temperature shift with a desulfurization module between the high and low temperature shift steps. [0028]
  • Process step F is a cooling step performed In one illustrative embodiment by a heat exchanger. The heat exchanger can be of any suitable construction including shell and tube, plate, spiral, etc. Alternatively a heat pipe or other form of heat sink may be utilized. The goal of the heat exchanger is to reduce the temperature of the gas stream to produce an effluent having a temperature preferably in the range of from about 90° C. to about 150° C. [0029]
  • Oxygen is added to the process in step F. The oxygen is consumed by the reactions of process step G described below. The oxygen can be in the form of air, enriched air, or substantially pure oxygen. The heat exchanger may by design provide mixing of the air with the hydrogen rich gas. Alternatively, the embodiment of process step D may be used to perform the mixing. [0030]
  • Process step G is an oxidation step wherein almost all of the remaining carbon monoxide in the effluent stream is converted to carbon dioxide. The processing is carried out in the presence of a catalyst for the oxidation of carbon monoxide and may be in any suitable form, such as pellets, spheres, monolith, etc. Oxidation catalysts for carbon monoxide are known and typically include noble metals (e.g., platinum, palladium) and/or transition metals (e.g., iron, chromium, manganese), and/or compounds of noble or transition metals, particularly oxides. A preferred oxidation catalyst is platinum on an alumina washcoat. The washcoat may be applied to a monolith, extrudate, pellet or other support. Additional materials such as cerium or lanthanum may be added to improve performance. Many other formulations have been cited in the literature with some practitioners claiming superior performance from rhodium or alumina catalysts. Ruthenium, palladium, gold, and other materials have been cited in the literature as being active for this use. [0031]
  • Two reactions occur in process step G: the desired oxidation of carbon monoxide (formula V) and the undesired oxidation of hydrogen (formula VI) as follows: [0032]
  • CO+½O2→CO2  (V)
  • H2+½O2→H2O  (VI)
  • The preferential oxidation of carbon monoxide is favored by low temperatures. Since both reactions produce heat it may be advantageous to optionally include a cooling element such as a cooling coil disposed within the process. The operating temperature of process is preferably kept in the range of from about 90° C. to about 150° C. Process step G preferably reduces the carbon monoxide level to less than 50 ppm, which is a suitable level for use in fuel cells, but one of skill in the art should appreciate that the present invention can be adapted to produce a hydrogen rich product with higher and lower levels of carbon monoxide. [0033]
  • The effluent exiting the fuel processor is a hydrogen rich gas containing carbon dioxide and other constituents which may be present such as water, inert components (e.g., nitrogen, argon), residual hydrocarbon, etc. Product gas may be used as the feed for a fuel cell or for other applications where a hydrogen rich feed stream is desired. Optionally, product gas may be sent on to further processing, for example, to remove the carbon dioxide, water or other components. [0034]
  • In one illustrative embodiment of the above described fuel processor, a compact fuel processor is of modular construction with individual modular units, which are separable, rearrangeable, and individually replaceable. [0035]
  • The present invention is an improvement to process step G described above, and utilizes a porous distribution tube to add air for the carbon monoxide oxidation throughout the catalyst bed length instead of one or two fixed injection points. By distributing the air injection hot and cold areas in the catalyst bed can be avoided. [0036]
  • Referring to the [0037] oxidation reactor 200 in FIG. 2, air A is injected through a porous tube 210, such as a sintered stainless steel tube manufactured by the Mott Corporation or an alumina tube as manufactured by the NGK corporation of Japan. By maintaining the air supply at a slightly higher pressure than the hydrogen rich gas feed H, supply air A will enter the chamber containing a carbon monoxide selective oxidation catalyst 220, such as that manufactured by the Engelhard Corporation. Upon coming into contact with the catalyst 220, the oxygen in the air will oxidize carbon monoxide and hydrogen (according to equations V and VI, above) causing the catalyst 220 and reactor 200 to warm. By using a cooling jacket 230 containing water, steam, air, or a cool hydrocarbon fuel feed stream, reactor 200 can be maintained in the desired operating temperature range of from about 90° C. to about 180° C. This oxidation step preferably reduces the carbon monoxide level to less than 50 ppm, which is a suitable level for use in fuel cells, but one of skill in the art should appreciate that the present invention can be adapted to produce a hydrogen rich product P with higher and lower levels of carbon monoxide.
  • In view of the above disclosure, one of skill in the art should understand and appreciate that one illustrative embodiment of the present invention includes a method and apparatus for reducing the carbon monoxide content of a hydrogen rich gas. Such an illustrative embodiment includes a catalyst bed containing an oxidation catalyst, a porous tube positioned substantially within the catalyst bed for distributing an oxygen-containing stream throughout the catalyst bed, and a cooling jacket for maintaining the reactor operating temperature in a desired range. The porous tube can be constructed as a sintered stainless steel tube or as an alumina tube or as any equivalent porous tube that is known to those of skill in the art to perform the objectives of this method and apparatus. The porous tube is positioned along the catalyst bed length, or may be aligned in any orientation that one of skill in the art would appreciate to result in optimal dispersion of the oxygen-containing stream throughout the catalyst bed. In one illustrative embodiment of the present invention is for the reactor operating temperature to be controlled by the cooling jacket from about 90° C. to about 180° C., more preferably from about 90° C. to about 150° C. The cooling jacket should contain a circulating coolant that can be water, air, or the hydrocarbon fuel to the fuel processor for energy efficiency improvements. [0038]
  • The present invention is intended not only for general oxidation reactors, but is also a preferred technology selection for the carbon monoxide oxidation reactors of fuel processors. Because of the direct feed to a fuel cell, there is a great need to ensure continuous on-specification hydrogen rich gas produced from compact fuel processors. [0039]
  • While the apparatus, compositions and methods of this invention have been described in terms of preferred or illustrative embodiments, it will be apparent to those of skill in the art that variations may be applied to the process described herein without departing from the concept and scope of the invention. All such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the scope and concept of the invention as it is set out in the following claims. [0040]

Claims (21)

What is claimed is:
1. A method for reducing the carbon monoxide content of a hydrogen rich gas, comprising:
providing a reactor having a catalyst bed containing an oxidation catalyst;
distributing an oxygen-containing stream throughout the catalyst bed in the presence of the hydrogen rich gas and the oxidation catalyst bed;
maintaining the reactor operating temperature in a desired range.
2. The method of claim 1, wherein the reactor has a porous tube substantially positioned within the catalyst bed for distributing the oxygen-containing stream throughout the catalyst bed.
3. The method of claim 2, wherein the oxygen-containing stream is maintained at a higher pressure than the hydrogen rich gas.
4. The method of claim 1, wherein the desired range for the reactor operating temperature minimizes the oxidation of hydrogen.
5. The method of claim 1, wherein the desired range for the reactor operating temperature is from about 90° C. to about 180° C.
6. The method of claim 1, wherein the desired range for the reactor operating temperature is from about 90° C. to about 150° C.
7. The method of claim 1, wherein the reactor has a cooling jacket for maintaining the reactor operating temperature.
8. The method of claim 7, wherein the cooling jacket contains a circulating coolant selected from the group consisting of water, steam, air, and hydrocarbon fuel.
9. An apparatus for selectively reducing the carbon monoxide content of a hydrogen rich gas, comprising:
a catalyst bed containing an oxidation catalyst;
a porous tube positioned substantially within the catalyst bed for distributing an oxygen-containing stream throughout the catalyst bed; and
a cooling jacket for maintaining the reactor operating temperature in a desired range.
10. The apparatus of claim 9, wherein the porous tube is a sintered stainless steel tube.
11. The apparatus of claim 9, wherein the porous tube is an alumina tube.
12. The apparatus of claim 9, wherein the porous tube is substantially positioned along the catalyst bed length.
13. The apparatus of claim 9, wherein the desired range for the reactor operating temperature is from about 90° C. to about 180° C.
14. The apparatus of claim 9, wherein the desired range for the reactor operating temperature is from about 90° C. to about 150° C.
15. The apparatus of claim 9, wherein the cooling jacket contains a circulating coolant selected from the group consisting of water, steam, air, and hydrocarbon fuel.
16. A reactor module for use in a compact fuel processor for selectively reducing the carbon monoxide content of a hydrogen rich gas, comprising:
a catalyst bed containing an oxidation catalyst;
a porous tube positioned substantially within the catalyst bed along the catalyst bed length for distributing an oxygen-containing stream throughout the catalyst bed; and
a cooling jacket surrounding the catalyst bed for maintaining the reactor operating temperature in a desired range.
17. The reactor of claim 16, wherein the porous tube is a sintered stainless steel tube.
18. The reactor of claim 16, wherein the porous tube is an alumina tube.
19. The reactor of claim 16, wherein the desired range for the reactor operating temperature is from about 90° C. to about 180° C.
20. The reactor of claim 16, wherein the desired range for the reactor operating temperature is from about 90° C. to about 150° C.
21. The reactor of claim 16, wherein the cooling jacket contains a circulating coolant selected from the group consisting of water, air, and hydrocarbon fuel.
US10/006,876 2000-12-05 2001-12-05 Method for reducing the carbon monoxide content of a hydrogen rich gas Abandoned US20020090334A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US10/006,876 US20020090334A1 (en) 2000-12-05 2001-12-05 Method for reducing the carbon monoxide content of a hydrogen rich gas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US25122600P 2000-12-05 2000-12-05
US10/006,876 US20020090334A1 (en) 2000-12-05 2001-12-05 Method for reducing the carbon monoxide content of a hydrogen rich gas

Publications (1)

Publication Number Publication Date
US20020090334A1 true US20020090334A1 (en) 2002-07-11

Family

ID=22951014

Family Applications (7)

Application Number Title Priority Date Filing Date
US10/006,880 Expired - Fee Related US7135154B2 (en) 2000-12-05 2001-12-05 Reactor module for use in a compact fuel processor
US10/006,963 Expired - Fee Related US7455817B2 (en) 2000-12-05 2001-12-05 Compact fuel processor for producing a hydrogen rich gas
US10/006,875 Abandoned US20020098129A1 (en) 2000-12-05 2001-12-05 Apparatus and method for heating catalyst for start-up of a compact fuel processor
US10/006,876 Abandoned US20020090334A1 (en) 2000-12-05 2001-12-05 Method for reducing the carbon monoxide content of a hydrogen rich gas
US10/006,879 Expired - Fee Related US7226490B2 (en) 2000-12-05 2001-12-05 Fuel processor for producing a hydrogen rich gas
US11/489,362 Expired - Fee Related US7544346B2 (en) 2000-12-05 2006-07-19 Compact fuel processor for producing a hydrogen rich gas
US11/740,099 Abandoned US20070186475A1 (en) 2000-12-05 2007-04-25 Fuel processor for producing a hydrogen rich gas

Family Applications Before (3)

Application Number Title Priority Date Filing Date
US10/006,880 Expired - Fee Related US7135154B2 (en) 2000-12-05 2001-12-05 Reactor module for use in a compact fuel processor
US10/006,963 Expired - Fee Related US7455817B2 (en) 2000-12-05 2001-12-05 Compact fuel processor for producing a hydrogen rich gas
US10/006,875 Abandoned US20020098129A1 (en) 2000-12-05 2001-12-05 Apparatus and method for heating catalyst for start-up of a compact fuel processor

Family Applications After (3)

Application Number Title Priority Date Filing Date
US10/006,879 Expired - Fee Related US7226490B2 (en) 2000-12-05 2001-12-05 Fuel processor for producing a hydrogen rich gas
US11/489,362 Expired - Fee Related US7544346B2 (en) 2000-12-05 2006-07-19 Compact fuel processor for producing a hydrogen rich gas
US11/740,099 Abandoned US20070186475A1 (en) 2000-12-05 2007-04-25 Fuel processor for producing a hydrogen rich gas

Country Status (16)

Country Link
US (7) US7135154B2 (en)
EP (4) EP1346183A4 (en)
JP (3) JP4596735B2 (en)
KR (2) KR100929886B1 (en)
CN (2) CN100368753C (en)
AT (1) ATE455591T1 (en)
AU (8) AU2729102A (en)
BR (2) BR0115948B1 (en)
CA (3) CA2436884C (en)
DE (1) DE60141163D1 (en)
DK (1) DK1347826T3 (en)
ES (1) ES2340760T3 (en)
HK (2) HK1061886A1 (en)
MX (2) MXPA03004997A (en)
NO (2) NO329361B1 (en)
WO (5) WO2002047186A2 (en)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020083646A1 (en) * 2000-12-05 2002-07-04 Deshpande Vijay A. Fuel processor for producing a hydrogen rich gas
US20020088740A1 (en) * 2000-12-13 2002-07-11 Krause Curtis L. Single chamber compact fuel processor
US20020090328A1 (en) * 2000-12-12 2002-07-11 Deshpande Vijay A. Nested compact fuel processor for producing hydrogen rich gas
US20030103880A1 (en) * 2001-08-11 2003-06-05 Bunk Kenneth J. Fuel processor utilizing heat pipe cooling
US20040018134A1 (en) * 2002-07-26 2004-01-29 Ke Liu Preferential oxidation reactor and process
US6759156B1 (en) 2003-04-04 2004-07-06 Texaco Inc. Operating states for fuel processor subsystems
US6796332B1 (en) 2003-04-04 2004-09-28 Texaco Inc Fluid balance control system for use in a fuel processor
US20040197615A1 (en) * 2003-04-04 2004-10-07 Texaco Inc. Architectural hierarchy of control for a fuel processor
US20040197238A1 (en) * 2003-04-04 2004-10-07 Mirkovic Vesna R. Firstout shutdown tracing for fuel processor control system
US20040197619A1 (en) * 2003-04-04 2004-10-07 Deshpande Vijay A. Coolant system for fuel processor
US20040194383A1 (en) * 2003-04-04 2004-10-07 Wheat W. Spencer Autothermal reforming in a fuel processor utilizing non-pyrophoric shift catalyst
US20040197239A1 (en) * 2003-04-04 2004-10-07 Mirkovic Vesna R. Temperature control in combustion process
US20050232858A1 (en) * 2003-11-26 2005-10-20 Hampden-Smith Mark J Fuel reformer catalyst and absorbent materials
US6979503B2 (en) 2003-04-04 2005-12-27 Texaco Inc. Method and apparatus for burst disk identification
US20070151232A1 (en) * 2002-11-15 2007-07-05 Eaton Corporation Devices and methods for reduction of NOx emissions from lean burn engines
US7267811B2 (en) 2003-11-26 2007-09-11 Cabot Corporation Fuel reformer catalyst and absorbent materials
US20120269709A1 (en) * 2009-12-22 2012-10-25 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources Method and apparatus for catalytic and thermochemical reactions

Families Citing this family (99)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003020410A1 (en) * 2001-04-26 2003-03-13 Texaco Development Corporation Compact fuel processor for producing a hydrogen rich gas
JP4648566B2 (en) * 2001-05-11 2011-03-09 Ｊｘ日鉱日石エネルギー株式会社 Autothermal reforming catalyst and method for producing fuel gas for fuel cell
JP4648567B2 (en) * 2001-05-11 2011-03-09 Ｊｘ日鉱日石エネルギー株式会社 Autothermal reforming catalyst and method for producing fuel gas for fuel cell
EP1451453B1 (en) 2001-12-03 2008-02-27 EATON Corporation System and methods for improved emission control of internal combustion engines
US7082753B2 (en) 2001-12-03 2006-08-01 Catalytica Energy Systems, Inc. System and methods for improved emission control of internal combustion engines using pulsed fuel flow
US7052636B2 (en) * 2002-01-15 2006-05-30 3M Innovative Properties Company Heat treated profile extruded hook
US6693057B1 (en) * 2002-03-22 2004-02-17 Sud-Chemie Inc. Water gas shift catalyst
WO2004040672A2 (en) * 2002-10-25 2004-05-13 Nuvera Fuel Cells Autothermal reforming catalyst
US7069981B2 (en) * 2002-11-08 2006-07-04 Modine Manufacturing Company Heat exchanger
EP1419812B1 (en) * 2002-11-15 2015-09-16 Haldor Topsoe A/S High temperature fixed bed reactor and its use
US7156887B1 (en) 2002-11-26 2007-01-02 General Motors Corporation Methods, apparatus, and systems for producing hydrogen from a fuel
US7105148B2 (en) * 2002-11-26 2006-09-12 General Motors Corporation Methods for producing hydrogen from a fuel
US7459224B1 (en) 2002-11-26 2008-12-02 General Motors Corporation Methods, apparatus, and systems for producing hydrogen from a fuel
US7488359B1 (en) 2002-12-19 2009-02-10 Hyradix, Inc. Compact reformer and water gas shift reactor for producing varying amounts of hydrogen
FR2850372B1 (en) * 2003-01-23 2006-06-09 Inst Francais Du Petrole NEW PARTIAL OXIDATION REACTOR
JP3663422B2 (en) * 2003-03-14 2005-06-22 独立行政法人科学技術振興機構 Hydrogen production method using methanol as a raw material and hydrogen production apparatus using this method
US7722832B2 (en) 2003-03-25 2010-05-25 Crystaphase International, Inc. Separation method and assembly for process streams in component separation units
US20040197622A1 (en) * 2003-04-04 2004-10-07 Texaco Inc. Method and apparatus for separating liquid from a gas stream
US7829227B2 (en) * 2003-04-04 2010-11-09 Texaco Inc. Integrated fuel processor apparatus and enclosure and methods of using same
US7101175B2 (en) * 2003-04-04 2006-09-05 Texaco Inc. Anode tailgas oxidizer
US7235217B2 (en) * 2003-04-04 2007-06-26 Texaco Inc. Method and apparatus for rapid heating of fuel reforming reactants
US7153334B2 (en) * 2003-05-21 2006-12-26 General Motors Corporation Fuel reforming system and method of operation
DE10355494B4 (en) * 2003-11-27 2009-12-03 Enerday Gmbh System and method for converting fuel and oxidant to reformate
US7629289B2 (en) * 2004-06-23 2009-12-08 Uop Llc Selective naphtha desulfurization process and catalyst
DE102004059014B4 (en) * 2004-12-08 2009-02-05 Lurgi Gmbh Reaction vessel for the production of synthesis gas containing H2 and CO
US7892304B2 (en) * 2004-12-17 2011-02-22 Texaco Inc. Apparatus and method for controlling compressor motor speed in a hydrogen generator
US7645307B2 (en) * 2004-12-17 2010-01-12 Texaco Inc. Combinational control strategy for fuel processor reactor shift temperature control
US7354464B2 (en) * 2004-12-17 2008-04-08 Texaco Inc. Apparatus and method for producing hydrogen
US7354463B2 (en) * 2004-12-17 2008-04-08 Texaco Inc. Apparatus and methods for producing hydrogen
US7402287B2 (en) * 2004-12-17 2008-07-22 Texaco Inc. Apparatus and methods for producing hydrogen
US7438079B2 (en) * 2005-02-04 2008-10-21 Air Products And Chemicals, Inc. In-line gas purity monitoring and control system
US7749376B2 (en) * 2005-08-15 2010-07-06 Sud-Chemie Inc. Process for sulfur adsorption using copper-containing catalyst
US20070072949A1 (en) * 2005-09-28 2007-03-29 General Electric Company Methods and apparatus for hydrogen gas production
US20070151154A1 (en) * 2005-11-04 2007-07-05 Maxim Lyubovsky Catalytic system for converting liquid fuels into syngas
US8444951B2 (en) * 2005-11-04 2013-05-21 Precision Combustion, Inc. Catalytic process and system for converting liquid fuels into syngas
US8557189B2 (en) 2005-11-04 2013-10-15 Precision Combustion, Inc. Catalytic system for converting liquid fuels into syngas
US8679545B2 (en) * 2005-11-12 2014-03-25 The Regents Of The University Of California Topical corticosteroids for the treatment of inflammatory diseases of the gastrointestinal tract
US7506685B2 (en) * 2006-03-29 2009-03-24 Pioneer Energy, Inc. Apparatus and method for extracting petroleum from underground sites using reformed gases
US9605522B2 (en) * 2006-03-29 2017-03-28 Pioneer Energy, Inc. Apparatus and method for extracting petroleum from underground sites using reformed gases
JP2007269615A (en) * 2006-03-31 2007-10-18 Miura Co Ltd Hydrogen generator and fuel cell system using the same
US20080069765A1 (en) * 2006-09-19 2008-03-20 Weibin Jiang Catalyst configuration and methods for syngas production
GB0619835D0 (en) * 2006-10-06 2006-11-15 Univ Bath Apparatus and process for use in three-phase catalytic reactions
CN101616865B (en) * 2006-11-30 2012-11-07 国际壳牌研究有限公司 Systems and processes for producing hydrogen and carbon dioxide
US7832364B2 (en) 2006-12-14 2010-11-16 Texaco Inc. Heat transfer unit for steam generation and gas preheating
US7578669B2 (en) * 2006-12-14 2009-08-25 Texaco Inc. Hybrid combustor for fuel processing applications
US20080141584A1 (en) * 2006-12-14 2008-06-19 Texaco Inc. Methods for Using a Catalyst Preburner in Fuel Processing Applications
DE102007001396A1 (en) * 2007-01-09 2008-07-10 Pierburg Gmbh Thermolysis reactor for decomposing solids, e.g. to produce ammonia from urea, has electric heater of positive resistance-temperature coefficient material to ensure even temperature
US8616294B2 (en) * 2007-05-20 2013-12-31 Pioneer Energy, Inc. Systems and methods for generating in-situ carbon dioxide driver gas for use in enhanced oil recovery
US7918906B2 (en) * 2007-05-20 2011-04-05 Pioneer Energy Inc. Compact natural gas steam reformer with linear countercurrent heat exchanger
ITVR20070114A1 (en) * 2007-08-07 2009-02-08 I C I Caldaie S P A CHEMICAL REACTOR STRUCTURE
JP5396749B2 (en) * 2008-06-11 2014-01-22 株式会社Ｉｈｉ Glycerin reforming apparatus and reforming method
DE102008031092A1 (en) * 2008-07-01 2010-01-07 Linde Aktiengesellschaft Method and device for generating hydrogen
US8450536B2 (en) 2008-07-17 2013-05-28 Pioneer Energy, Inc. Methods of higher alcohol synthesis
KR100991263B1 (en) * 2008-08-01 2010-11-01 현대중공업 주식회사 Nickel based Catalyst for reforming of natural gas with mixture of steam and carbon dioxide
US8940660B2 (en) * 2008-12-04 2015-01-27 Uop Llc Simultaneous warm gas desulfurization and complete CO-shift for improved syngas cleanup
WO2010087791A1 (en) * 2009-01-27 2010-08-05 Utc Power Corporation Distributively cooled, integrated water-gas shift reactor and vaporizer
US8795912B2 (en) * 2009-06-16 2014-08-05 Shell Oil Company Systems and processes for operating fuel cell systems
US8632922B2 (en) * 2009-06-16 2014-01-21 Shell Oil Company Systems and processes for operating fuel cell systems
US7937948B2 (en) * 2009-09-23 2011-05-10 Pioneer Energy, Inc. Systems and methods for generating electricity from carbonaceous material with substantially no carbon dioxide emissions
FR2953150B1 (en) * 2009-12-01 2013-08-09 Air Liquide CATALYTIC REACTOR COMPRISING A CATALYTIC ALVEOL STRUCTURE AND AT LEAST ONE STRUCTURAL ELEMENT
FR2956040B1 (en) * 2010-02-05 2013-09-27 Inst Francais Du Petrole LABORATORY REACTOR CONTAINING DIFFERENT INTERNAL DEVICES TO IMPROVE FLUID DISTRIBUTION
CA2795015A1 (en) 2010-03-31 2011-10-06 Council Of Scientific & Industrial Research Hydrogen/syngas generator
EP2455334A1 (en) 2010-11-18 2012-05-23 Tecnicas Reunidas, S.A. Ethanol processing system
DE102011014217A1 (en) * 2011-03-17 2012-09-20 Thyssenkrupp Uhde Gmbh Method for commissioning autothermal reforming reactors
WO2013135660A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Axial flow reactor having heating planes and intermediate planes
WO2013135663A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on mixed metal oxide catalysts comprising noble metal
WO2013135656A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on mixed metal oxide catalysts in the form of hexaaluminates
WO2013135668A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Chemical reactor system, comprising an axial flow reactor with heating levels and intermediate levels
WO2013135673A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on catalysts especially carbide supported catalysts
AU2013231342A1 (en) * 2012-03-13 2014-10-16 Bayer Intellectual Property Gmbh Method for producing CO and/or H2 in an alternating operation between two operating modes
WO2013135665A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on mixed metal oxide catalysts in the form of partially substituted hexaaluminates
WO2013135664A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on mixed metal oxide catalysts on oxidic substrates doped with aluminum, cerium, and/or zirconium
WO2013135659A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on oxidic catalysts comprising nickel and ruthenium
WO2013135662A1 (en) * 2012-03-13 2013-09-19 Bayer Intellectual Property Gmbh Method for reducing carbon dioxide at high temperatures on mixed metal oxide catalysts
KR101179539B1 (en) 2012-05-09 2012-09-04 국방과학연구소 A Reformer for Fuel Cell System
US9238781B2 (en) 2012-09-05 2016-01-19 University Of South Carolina Systems and methods for liquid fuel desulfurization
US20140335625A1 (en) * 2013-05-10 2014-11-13 Cdti Temperature Control Method in a Laboratory Scale Reactor
DE102013113101B4 (en) * 2013-07-02 2015-11-12 Windmöller & Hölscher Kg Extrusion tool for a film blowing head and blowing head
US9499403B2 (en) 2013-07-10 2016-11-22 Saudi Arabian Oil Company Catalyst and process for thermo-neutral reforming of liquid hydrocarbons
WO2015069319A1 (en) * 2013-11-11 2015-05-14 Aerojet Rocketdyne, Inc. Reactor system for producing synthesis gas
US9595726B2 (en) 2014-01-07 2017-03-14 Advanced Cooling Technologies, Inc. Fuel reforming system and process
WO2015198186A1 (en) 2014-06-23 2015-12-30 Tubitak An autothermal reformer reactor and a feeding system thereof
US10744426B2 (en) 2015-12-31 2020-08-18 Crystaphase Products, Inc. Structured elements and methods of use
US10054140B2 (en) 2016-02-12 2018-08-21 Crystaphase Products, Inc. Use of treating elements to facilitate flow in vessels
US9732774B1 (en) * 2016-02-12 2017-08-15 Crystaphase Products, Inc. Use of treating elements to facilitate flow in vessels
US10557391B1 (en) 2017-05-18 2020-02-11 Advanced Cooling Technologies, Inc. Incineration system and process
EP3574991A1 (en) 2018-05-31 2019-12-04 Haldor Topsøe A/S Steam reforming heated by resistance heating
US20210113983A1 (en) * 2018-05-31 2021-04-22 Haldor Topsøe A/S Endothermic reactions heated by resistance heating
US10746075B2 (en) * 2018-07-12 2020-08-18 GM Global Technology Operations LLC Thermoelectric module for use in a vehicle system
AT522323B1 (en) * 2019-05-21 2020-10-15 Lec Gmbh Membrane reactor
CA3162061A1 (en) 2019-12-20 2021-06-24 John N. Glover Resaturation of gas into a liquid feedstream
US11322766B2 (en) * 2020-05-28 2022-05-03 Saudi Arabian Oil Company Direct hydrocarbon metal supported solid oxide fuel cell
CA3192003A1 (en) 2020-09-09 2022-03-17 Crystaphase Products, Inc. Process vessel entry zones
TWI769612B (en) * 2020-11-02 2022-07-01 國立成功大學 Scroll heating device
EP4323102A1 (en) * 2021-04-15 2024-02-21 Shell Internationale Research Maatschappij B.V. Modular reactor configuration for production of chemicals with electrical heating for carrying out reactions
WO2022248581A1 (en) * 2021-05-28 2022-12-01 Topsoe A/S Electrical heater with catalytic activity
DE102021210249A1 (en) 2021-09-16 2023-03-16 Thyssenkrupp Ag Ammonia Synthesis Device
BE1029758B1 (en) 2021-09-16 2023-04-11 Thyssenkrupp Ind Solutions Ag Ammonia Synthesis Device
WO2023041619A1 (en) 2021-09-16 2023-03-23 Thyssenkrupp Industrial Solutions Ag Ammonia synthesis device

Citations (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3572046A (en) * 1965-10-22 1971-03-23 Braun & Co C F Apparatus for purification of raw ammonia synthesis gas
US3653846A (en) * 1968-06-03 1972-04-04 Kralovopolska Strojirna Z Chem Converter for high pressure synthesis
US3720602A (en) * 1971-02-26 1973-03-13 Exxon Research Engineering Co Water injection in a hydrodesulfurization process
US3729936A (en) * 1971-05-24 1973-05-01 Universal Oil Prod Co Method and means for catalytically treating engine exhaust gases
US3838994A (en) * 1972-02-14 1974-10-01 Exxon Research Engineering Co Conversion of heavy hydrocarbons to a methane rich gas product
US3909299A (en) * 1973-10-01 1975-09-30 United Technologies Corp Fuel cell system including reform reactor
US3996016A (en) * 1975-12-29 1976-12-07 Uop Inc. Variable capacity catalytic converter
US4363654A (en) * 1980-04-08 1982-12-14 Geoffrey Frederick Production of reducing gas for furnace injection
US4522894A (en) * 1982-09-30 1985-06-11 Engelhard Corporation Fuel cell electric power production
US4876409A (en) * 1987-03-30 1989-10-24 Atlantic Richfield Company Thin bed cofeed reactors for methane conversion
US4976747A (en) * 1989-10-10 1990-12-11 International Fuel Cells Corporation Fuel treatment apparatus for fuel cells
US5132007A (en) * 1987-06-08 1992-07-21 Carbon Fuels Corporation Co-generation system for co-producing clean, coal-based fuels and electricity
US5209906A (en) * 1991-05-10 1993-05-11 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of National Defence Modular isothermal reactor
US5248566A (en) * 1991-11-25 1993-09-28 The United States Of America As Represented By The United States Department Of Energy Fuel cell system for transportation applications
US5330727A (en) * 1992-03-19 1994-07-19 International Fuel Cells Corporation Apparatus for removing carbon monoxide from gaseous media
US5385712A (en) * 1993-12-07 1995-01-31 Sprunk; Darren K. Modular chemical reactor
US5656494A (en) * 1992-09-16 1997-08-12 Rotron Incorporated Biofilter with modular trays
US5725756A (en) * 1995-04-18 1998-03-10 Center For Research, Inc. In situ mitigation of coke buildup in porous catalysts with supercritical reaction media
US5874051A (en) * 1995-12-01 1999-02-23 Daimler-Benz Ag Method and apparatus for selective catalytic oxidation of carbon monoxide
US5997594A (en) * 1996-10-30 1999-12-07 Northwest Power Systems, Llc Steam reformer with internal hydrogen purification
US6024774A (en) * 1996-09-26 2000-02-15 Kabushiki Kaisha Toshiba Chemical reaction apparatus and method of collecting main product gas
US6033793A (en) * 1996-11-01 2000-03-07 Hydrogen Burner Technology, Inc. Integrated power module
US6086839A (en) * 1997-12-05 2000-07-11 Dbb Fuel Cell Engines Gmbh System and process for the water vapor reforming of a hydrocarbon
US6238815B1 (en) * 1998-07-29 2001-05-29 General Motors Corporation Thermally integrated staged methanol reformer and method
US20020083646A1 (en) * 2000-12-05 2002-07-04 Deshpande Vijay A. Fuel processor for producing a hydrogen rich gas
US20020090327A1 (en) * 2000-12-12 2002-07-11 Deshpande Vijay A. Dual stack compact fuel processor for producing hydrogen rich gas
US20020088740A1 (en) * 2000-12-13 2002-07-11 Krause Curtis L. Single chamber compact fuel processor
US6641625B1 (en) * 1999-05-03 2003-11-04 Nuvera Fuel Cells, Inc. Integrated hydrocarbon reforming system and controls

Family Cites Families (67)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1986348A (en) * 1931-06-13 1935-01-01 Du Pont Apparatus for effecting gas reactions
US2443423A (en) * 1946-04-29 1948-06-15 Phillips Petroleum Co Apparatus for conducting endothermic catalytic conversions
US3023803A (en) * 1959-01-12 1962-03-06 Honeywell Regulator Co Control apparatus
US3572048A (en) 1968-10-14 1971-03-23 Wiremold Co Ominpositional cryogenic underwater breathind apparatus
US3976507A (en) * 1975-02-12 1976-08-24 United Technologies Corporation Pressurized fuel cell power plant with single reactant gas stream
US4033133A (en) * 1976-03-22 1977-07-05 California Institute Of Technology Start up system for hydrogen generator used with an internal combustion engine
US4046956A (en) * 1976-05-27 1977-09-06 United Technologies Corporation Process for controlling the output of a selective oxidizer
US4190641A (en) * 1978-12-06 1980-02-26 United Technologies Corporation Method for producing hydrogen
IT1141102B (en) * 1980-11-28 1986-10-01 Ammonia Casale Sa AXIAL-RADIAL REACTOR FOR HETEROGENEOUS SYNTHESIS
US4483691A (en) * 1982-09-30 1984-11-20 Engelhard Corporation Production of synthetic natural gas from coal gasification liquid by-products
US4927857A (en) * 1982-09-30 1990-05-22 Engelhard Corporation Method of methanol production
US4863707A (en) * 1982-09-30 1989-09-05 Engelhard Corporation Method of ammonia production
JPH0642940B2 (en) * 1987-03-31 1994-06-08 東洋エンジニアリング株式会社 Device for gas endothermic reaction
JP2791130B2 (en) * 1989-09-18 1998-08-27 株式会社東芝 Fuel cell power plant
JPH03237002A (en) * 1990-02-14 1991-10-22 Kobe Steel Ltd Reactor for fuel cell
JP2931362B2 (en) * 1990-04-12 1999-08-09 日本碍子株式会社 Resistance control type heater and catalytic converter
JPH0474701A (en) * 1990-07-12 1992-03-10 Fuji Electric Co Ltd Reactor for converting carbon monoxide
US5141432A (en) * 1990-07-18 1992-08-25 Radian Corporation Apparatus and method for combustion within porous matrix elements
JPH04196061A (en) * 1990-11-28 1992-07-15 Tokyo Gas Co Ltd Carbon monoxide reformer
JPH04298228A (en) * 1991-03-27 1992-10-22 Tokyo Gas Co Ltd Desulfurization reactor
DE4132439A1 (en) * 1991-09-28 1993-04-01 Behr Gmbh & Co EXHAUST CATALYST
JP2659504B2 (en) * 1991-12-26 1997-09-30 大阪瓦斯株式会社 Catalytic combustion device
GB9225188D0 (en) * 1992-12-02 1993-01-20 Rolls Royce & Ass Combined reformer and shift reactor
US5582805A (en) * 1992-12-21 1996-12-10 Toyota Jidosha Kabushiki Kaisha Electrically heated catalytic apparatus
US5326537A (en) * 1993-01-29 1994-07-05 Cleary James M Counterflow catalytic device
DE4303850C1 (en) * 1993-02-10 1994-10-13 Alfred Buck Device for the catalytic cleaning of flowing gases, in particular exhaust gases from internal combustion engines
JPH06240268A (en) * 1993-02-19 1994-08-30 Ube Ind Ltd Fluidized bed reforming equipment
US5840270A (en) * 1993-04-23 1998-11-24 H Power Corporation Catalytic method of generating hydrogen
US5360679A (en) * 1993-08-20 1994-11-01 Ballard Power Systems Inc. Hydrocarbon fueled solid polymer fuel cell electric power generation system
JP3403494B2 (en) * 1994-05-23 2003-05-06 日本碍子株式会社 Reforming reactor
US5811062A (en) * 1994-07-29 1998-09-22 Battelle Memorial Institute Microcomponent chemical process sheet architecture
US5512251A (en) * 1994-07-29 1996-04-30 W. R. Grace & Co.-Conn. Combined electrically heatable converter body
JP3711577B2 (en) * 1994-10-28 2005-11-02 株式会社エクォス・リサーチ Fuel reformer
JPH08217405A (en) * 1995-02-10 1996-08-27 Fuji Electric Co Ltd Fuel reforming reactor for fuel cell power-generating plant
US5669960A (en) * 1995-11-02 1997-09-23 Praxair Technology, Inc. Hydrogen generation process
US6126908A (en) * 1996-08-26 2000-10-03 Arthur D. Little, Inc. Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide
US6221117B1 (en) 1996-10-30 2001-04-24 Idatech, Llc Hydrogen producing fuel processing system
JP3129670B2 (en) * 1997-02-28 2001-01-31 三菱電機株式会社 Fuel reformer
JP3743119B2 (en) * 1997-06-03 2006-02-08 ダイキン工業株式会社 Fuel cell power generation system
JPH111302A (en) * 1997-06-10 1999-01-06 Toyota Motor Corp Reforming of fuel and fuel reforming unit, and fuel cell unit equipped with the same fuel reforming unit
CA2291771A1 (en) * 1997-07-03 1999-01-14 David Julian Bueker Method of inductively igniting a chemical reaction
BR9810275A (en) * 1997-07-03 2000-09-05 Du Pont Apparatus for continuously conducting a catalyzed gas phase reaction
JPH1143303A (en) * 1997-07-25 1999-02-16 Matsushita Electric Works Ltd Reforming unit
US5977421A (en) * 1997-09-03 1999-11-02 Hanson; Curtiss D. Pyrolysis method for increasing limonene production and novel oven to facilitate such method
DE19746251C2 (en) * 1997-10-20 1999-09-09 Dbb Fuel Cell Engines Gmbh Plant for the steam reforming of a hydrocarbon and operating method therefor
JPH11130405A (en) * 1997-10-28 1999-05-18 Ngk Insulators Ltd Reforming reaction device, catalytic device, exothermic catalytic body used for the same and operation of reforming reaction device
US5938800A (en) * 1997-11-13 1999-08-17 Mcdermott Technology, Inc. Compact multi-fuel steam reformer
JP3490877B2 (en) * 1997-11-17 2004-01-26 三洋電機株式会社 Starting method of reformer for fuel cell
US6077620A (en) * 1997-11-26 2000-06-20 General Motors Corporation Fuel cell system with combustor-heated reformer
US6063515A (en) * 1997-12-22 2000-05-16 Ballard Power Systems Inc. Integrated fuel cell electric power generation system for submarine applications
WO1999044736A1 (en) 1998-03-04 1999-09-10 INSTITUT FüR MIKROTECHNIK MAINZ GMBH Method for carrying out chemical reactions in a microreactor, and such a microreactor
JP4161147B2 (en) * 1998-03-27 2008-10-08 大阪瓦斯株式会社 Hydrogen production equipment
JP2000007301A (en) * 1998-06-29 2000-01-11 Ngk Insulators Ltd Reforming reactor
US6576203B2 (en) * 1998-06-29 2003-06-10 Ngk Insulators, Ltd. Reformer
US6132007A (en) * 1998-08-13 2000-10-17 Harmsen; Wayne A. Wheel weight system
US6180846B1 (en) * 1998-09-08 2001-01-30 Uop Llc Process and apparatus using plate arrangement for combustive reactant heating
JP3898892B2 (en) * 1998-10-14 2007-03-28 アイダテック・エルエルシー Reformer
KR100286572B1 (en) * 1998-11-19 2001-04-16 남창우 Fuel cell vehicle small fuel reformer and its system using metal thin film
DE19903168C2 (en) * 1999-01-27 2002-06-20 Xcellsis Gmbh Spiral heat exchanger
DE10080450T1 (en) * 1999-02-10 2001-05-17 Toshiba Kawasaki Kk Carbon monoxide conversion device for a fuel cell and fuel cell power generation system
US6140266A (en) * 1999-02-18 2000-10-31 International Fuel Cells, Co., Llc Compact and light weight catalyst bed for use in a fuel cell power plant and method for forming the same
WO2000066487A1 (en) * 1999-05-03 2000-11-09 Nuvera Fuel Cells Autothermal reforming system with integrated shift beds, preferential oxidation reactor, auxiliary reactor, and system controls
JP2001295707A (en) * 1999-06-03 2001-10-26 Toyota Motor Corp Fuel reforming device carried on vehicle
US6299994B1 (en) * 1999-06-18 2001-10-09 Uop Llc Process for providing a pure hydrogen stream for use with fuel cells
US6316134B1 (en) * 1999-09-13 2001-11-13 Ballard Generation Systems, Inc. Fuel cell electric power generation system
JP3813391B2 (en) * 1999-09-27 2006-08-23 株式会社東芝 Solid polymer fuel cell power generator and method of operating the same
US6972119B2 (en) * 1999-12-28 2005-12-06 Matsushita Electric Industrial Co., Ltd. Apparatus for forming hydrogen

Patent Citations (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3572046A (en) * 1965-10-22 1971-03-23 Braun & Co C F Apparatus for purification of raw ammonia synthesis gas
US3653846A (en) * 1968-06-03 1972-04-04 Kralovopolska Strojirna Z Chem Converter for high pressure synthesis
US3720602A (en) * 1971-02-26 1973-03-13 Exxon Research Engineering Co Water injection in a hydrodesulfurization process
US3729936A (en) * 1971-05-24 1973-05-01 Universal Oil Prod Co Method and means for catalytically treating engine exhaust gases
US3838994A (en) * 1972-02-14 1974-10-01 Exxon Research Engineering Co Conversion of heavy hydrocarbons to a methane rich gas product
US3909299A (en) * 1973-10-01 1975-09-30 United Technologies Corp Fuel cell system including reform reactor
US3996016A (en) * 1975-12-29 1976-12-07 Uop Inc. Variable capacity catalytic converter
US4363654A (en) * 1980-04-08 1982-12-14 Geoffrey Frederick Production of reducing gas for furnace injection
US4522894A (en) * 1982-09-30 1985-06-11 Engelhard Corporation Fuel cell electric power production
US4876409A (en) * 1987-03-30 1989-10-24 Atlantic Richfield Company Thin bed cofeed reactors for methane conversion
US5132007A (en) * 1987-06-08 1992-07-21 Carbon Fuels Corporation Co-generation system for co-producing clean, coal-based fuels and electricity
US4976747A (en) * 1989-10-10 1990-12-11 International Fuel Cells Corporation Fuel treatment apparatus for fuel cells
US5209906A (en) * 1991-05-10 1993-05-11 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of National Defence Modular isothermal reactor
US5248566A (en) * 1991-11-25 1993-09-28 The United States Of America As Represented By The United States Department Of Energy Fuel cell system for transportation applications
US5330727A (en) * 1992-03-19 1994-07-19 International Fuel Cells Corporation Apparatus for removing carbon monoxide from gaseous media
US5656494A (en) * 1992-09-16 1997-08-12 Rotron Incorporated Biofilter with modular trays
US5385712A (en) * 1993-12-07 1995-01-31 Sprunk; Darren K. Modular chemical reactor
US5725756A (en) * 1995-04-18 1998-03-10 Center For Research, Inc. In situ mitigation of coke buildup in porous catalysts with supercritical reaction media
US5874051A (en) * 1995-12-01 1999-02-23 Daimler-Benz Ag Method and apparatus for selective catalytic oxidation of carbon monoxide
US6024774A (en) * 1996-09-26 2000-02-15 Kabushiki Kaisha Toshiba Chemical reaction apparatus and method of collecting main product gas
US5997594A (en) * 1996-10-30 1999-12-07 Northwest Power Systems, Llc Steam reformer with internal hydrogen purification
US6033793A (en) * 1996-11-01 2000-03-07 Hydrogen Burner Technology, Inc. Integrated power module
US6086839A (en) * 1997-12-05 2000-07-11 Dbb Fuel Cell Engines Gmbh System and process for the water vapor reforming of a hydrocarbon
US6238815B1 (en) * 1998-07-29 2001-05-29 General Motors Corporation Thermally integrated staged methanol reformer and method
US6641625B1 (en) * 1999-05-03 2003-11-04 Nuvera Fuel Cells, Inc. Integrated hydrocarbon reforming system and controls
US20020083646A1 (en) * 2000-12-05 2002-07-04 Deshpande Vijay A. Fuel processor for producing a hydrogen rich gas
US20020090326A1 (en) * 2000-12-05 2002-07-11 Deshpande Vijay A. Reactor module for use in a compact fuel processor
US20020094310A1 (en) * 2000-12-05 2002-07-18 Krause Curtis L. Compact fuel processor for producing a hydrogen rich gas
US20020098129A1 (en) * 2000-12-05 2002-07-25 Paul Martin Apparatus and method for heating catalyst for start-up of a compact fuel processor
US20020090328A1 (en) * 2000-12-12 2002-07-11 Deshpande Vijay A. Nested compact fuel processor for producing hydrogen rich gas
US20020090327A1 (en) * 2000-12-12 2002-07-11 Deshpande Vijay A. Dual stack compact fuel processor for producing hydrogen rich gas
US20020088740A1 (en) * 2000-12-13 2002-07-11 Krause Curtis L. Single chamber compact fuel processor

Cited By (59)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7455817B2 (en) 2000-12-05 2008-11-25 Texaco Inc. Compact fuel processor for producing a hydrogen rich gas
US20070186475A1 (en) * 2000-12-05 2007-08-16 Texaco Inc. Fuel processor for producing a hydrogen rich gas
US20060254141A1 (en) * 2000-12-05 2006-11-16 Texaco Inc. Compact fuel processor for producing a hydrogen rich gas
US7226490B2 (en) 2000-12-05 2007-06-05 Texaco, Inc. Fuel processor for producing a hydrogen rich gas
US20020090326A1 (en) * 2000-12-05 2002-07-11 Deshpande Vijay A. Reactor module for use in a compact fuel processor
US20020094310A1 (en) * 2000-12-05 2002-07-18 Krause Curtis L. Compact fuel processor for producing a hydrogen rich gas
US20020098129A1 (en) * 2000-12-05 2002-07-25 Paul Martin Apparatus and method for heating catalyst for start-up of a compact fuel processor
US7544346B2 (en) 2000-12-05 2009-06-09 Texaco Inc. Compact fuel processor for producing a hydrogen rich gas
US20020083646A1 (en) * 2000-12-05 2002-07-04 Deshpande Vijay A. Fuel processor for producing a hydrogen rich gas
US7135154B2 (en) 2000-12-05 2006-11-14 Texaco Inc. Reactor module for use in a compact fuel processor
US20050204628A1 (en) * 2000-12-12 2005-09-22 Texaco Inc. Dual stack compact fuel processor for producing a hydrogen rich gas
US6887285B2 (en) 2000-12-12 2005-05-03 Texaco Inc. Dual stack compact fuel processor for producing hydrogen rich gas
US7524343B2 (en) 2000-12-12 2009-04-28 Texaco Inc. Dual stack compact fuel processor for producing a hydrogen rich gas
US6824577B2 (en) 2000-12-12 2004-11-30 Texaco Inc. Nested compact fuel processor for producing hydrogen rich gas
US20050204627A1 (en) * 2000-12-12 2005-09-22 Texaco Inc. Dual stack compact fuel processor for producing a hydrogen rich gas
US20020090327A1 (en) * 2000-12-12 2002-07-11 Deshpande Vijay A. Dual stack compact fuel processor for producing hydrogen rich gas
US20020090328A1 (en) * 2000-12-12 2002-07-11 Deshpande Vijay A. Nested compact fuel processor for producing hydrogen rich gas
US7022149B2 (en) 2000-12-13 2006-04-04 Texaco Inc. Single chamber compact fuel processor
US20020088740A1 (en) * 2000-12-13 2002-07-11 Krause Curtis L. Single chamber compact fuel processor
US20030103880A1 (en) * 2001-08-11 2003-06-05 Bunk Kenneth J. Fuel processor utilizing heat pipe cooling
US7195742B2 (en) * 2002-07-26 2007-03-27 Utc Fuel Cells, Llc Preferential oxidation reactor and process
US20040018134A1 (en) * 2002-07-26 2004-01-29 Ke Liu Preferential oxidation reactor and process
US20070151232A1 (en) * 2002-11-15 2007-07-05 Eaton Corporation Devices and methods for reduction of NOx emissions from lean burn engines
US7610752B2 (en) 2002-11-15 2009-11-03 Eaton Corporation Devices and methods for reduction of NOx emissions from lean burn engines
US6979503B2 (en) 2003-04-04 2005-12-27 Texaco Inc. Method and apparatus for burst disk identification
US7318970B2 (en) 2003-04-04 2008-01-15 Texaco Inc. Architectural hierarchy of control for a fuel processor
US6966327B2 (en) 2003-04-04 2005-11-22 Texaco Development Corporation Fluid balance control system for use in a fuel processor
US20050188614A1 (en) * 2003-04-04 2005-09-01 Texaco Inc. Control system for a hydrogen generator
US20060057438A1 (en) * 2003-04-04 2006-03-16 Wheat W S Method and apparatus for burst disk identification
US20050143862A1 (en) * 2003-04-04 2005-06-30 Texaco Inc. Automated control strategy for fuel processor reactor shift catalyst regeneration
US7081144B2 (en) 2003-04-04 2006-07-25 Texaco Inc. Autothermal reforming in a fuel processor utilizing non-pyrophoric shift catalyst
US20060201064A1 (en) * 2003-04-04 2006-09-14 Texaco Inc. Autothermal reforming in a fuel processor utilizing non-pyrophoric shift catalyst
US20050042486A1 (en) * 2003-04-04 2005-02-24 Texaco Inc. Coolant system for fuel processor
US20050034773A1 (en) * 2003-04-04 2005-02-17 Texaco Inc. Fluid balance control system for use in a fuel processor
US20040197239A1 (en) * 2003-04-04 2004-10-07 Mirkovic Vesna R. Temperature control in combustion process
US20040194383A1 (en) * 2003-04-04 2004-10-07 Wheat W. Spencer Autothermal reforming in a fuel processor utilizing non-pyrophoric shift catalyst
US20040194827A1 (en) * 2003-04-04 2004-10-07 Nguyen Kevin H. Fluid balance control system for use in a fuel processor
US20040197619A1 (en) * 2003-04-04 2004-10-07 Deshpande Vijay A. Coolant system for fuel processor
US8260464B2 (en) 2003-04-04 2012-09-04 Texaco Inc. Architectural hierarchy of control for a fuel processor
US8153311B2 (en) 2003-04-04 2012-04-10 Texaco Inc. And Texaco Development Corporation Method and apparatus for burst disk identification
US20070243436A1 (en) * 2003-04-04 2007-10-18 Texaco Inc. Coolant System for Fuel Processor
US8119299B2 (en) 2003-04-04 2012-02-21 Texaco Inc. Coolant system for fuel processor
US20080070074A1 (en) * 2003-04-04 2008-03-20 Texaco Inc. Architectural Hierarchy of Control for a Fuel Processor
US7410710B2 (en) 2003-04-04 2008-08-12 Texaco Inc. Firstout shutdown tracing for fuel processor control system
US20040197238A1 (en) * 2003-04-04 2004-10-07 Mirkovic Vesna R. Firstout shutdown tracing for fuel processor control system
US20040197615A1 (en) * 2003-04-04 2004-10-07 Texaco Inc. Architectural hierarchy of control for a fuel processor
US6796332B1 (en) 2003-04-04 2004-09-28 Texaco Inc Fluid balance control system for use in a fuel processor
US7593788B2 (en) 2003-04-04 2009-09-22 Texaco Inc. Automated control strategy for fuel processor reactor shift catalyst regeneration
US6759156B1 (en) 2003-04-04 2004-07-06 Texaco Inc. Operating states for fuel processor subsystems
US7857875B2 (en) 2003-04-04 2010-12-28 Texaco Inc. Autothermal reforming in a fuel processor utilizing non-pyrophoric shift catalyst
US7785539B2 (en) 2003-04-04 2010-08-31 Texaco Inc. Method of controlling a hydrogen generator
US20100158791A1 (en) * 2003-11-26 2010-06-24 Cabot Corporation Fuel reformer catalyst and absorbent materials
US20050232858A1 (en) * 2003-11-26 2005-10-20 Hampden-Smith Mark J Fuel reformer catalyst and absorbent materials
US7267811B2 (en) 2003-11-26 2007-09-11 Cabot Corporation Fuel reformer catalyst and absorbent materials
US8163669B2 (en) 2003-11-26 2012-04-24 Cabot Corporation Fuel reformer catalyst and absorbent materials
US7264788B2 (en) 2003-11-26 2007-09-04 Cabot Corporation Fuel reformer catalyst and absorbent materials
US20120269709A1 (en) * 2009-12-22 2012-10-25 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources Method and apparatus for catalytic and thermochemical reactions
US8609052B2 (en) * 2009-12-22 2013-12-17 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Natural Resources Hybrid reactor with two reaction zones
US8728426B2 (en) 2009-12-22 2014-05-20 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Natural Resources Hybrid reactor with two reaction zones

Also Published As

Publication number Publication date
CA2436868C (en) 2011-02-15
US20020090326A1 (en) 2002-07-11
EP1345679A2 (en) 2003-09-24
CA2436868A1 (en) 2002-06-13
ES2340760T3 (en) 2010-06-09
WO2002047186A2 (en) 2002-06-13
AU2002236584B2 (en) 2007-03-15
US7455817B2 (en) 2008-11-25
EP1345679A4 (en) 2006-05-03
DK1347826T3 (en) 2010-05-17
CN1323748C (en) 2007-07-04
JP2004525484A (en) 2004-08-19
WO2002046676A1 (en) 2002-06-13
HK1061886A1 (en) 2004-10-08
AU2002227291B2 (en) 2007-08-30
NO20032521D0 (en) 2003-06-04
HK1077247A1 (en) 2006-02-10
CA2436884A1 (en) 2002-06-13
US7135154B2 (en) 2006-11-14
CN1627986A (en) 2005-06-15
CN1483133A (en) 2004-03-17
KR20040010571A (en) 2004-01-31
AU3658402A (en) 2002-06-18
JP2007326777A (en) 2007-12-20
EP1347826A1 (en) 2003-10-01
MXPA03004997A (en) 2003-09-05
WO2002045836A1 (en) 2002-06-13
AU2729102A (en) 2002-06-18
US7544346B2 (en) 2009-06-09
DE60141163D1 (en) 2010-03-11
BR0115947A (en) 2003-11-04
NO332183B1 (en) 2012-07-23
CN100368753C (en) 2008-02-13
NO20032522D0 (en) 2003-06-04
JP2004515432A (en) 2004-05-27
US20020083646A1 (en) 2002-07-04
JP4318917B2 (en) 2009-08-26
US20020098129A1 (en) 2002-07-25
EP1347826B1 (en) 2010-01-20
KR100929886B1 (en) 2009-12-04
JP5015690B2 (en) 2012-08-29
WO2002045838A1 (en) 2002-06-13
BR0115948B1 (en) 2010-05-18
EP2278247A1 (en) 2011-01-26
KR20040010569A (en) 2004-01-31
CA2436884C (en) 2010-06-22
NO329361B1 (en) 2010-10-04
US20020094310A1 (en) 2002-07-18
AU2002226039B2 (en) 2007-09-13
US20070186475A1 (en) 2007-08-16
US20060254141A1 (en) 2006-11-16
KR100798134B1 (en) 2008-01-28
AU2002227307A1 (en) 2002-06-18
EP1346183A1 (en) 2003-09-24
NO20032521L (en) 2003-07-24
NO20032522L (en) 2003-06-04
AU2002226038A1 (en) 2002-06-18
US7226490B2 (en) 2007-06-05
EP1346183A4 (en) 2006-11-08
CA2436997C (en) 2010-07-20
MXPA03004998A (en) 2003-09-05
EP1345679B1 (en) 2013-03-13
BR0115948A (en) 2004-02-25
WO2002045839A1 (en) 2002-06-13
JP4596735B2 (en) 2010-12-15
AU2603902A (en) 2002-06-18
ATE455591T1 (en) 2010-02-15
EP1347826A4 (en) 2006-05-03
WO2002047186A3 (en) 2003-01-30
CA2436997A1 (en) 2002-06-13

Similar Documents

Publication Publication Date Title
US20020090334A1 (en) Method for reducing the carbon monoxide content of a hydrogen rich gas
US7160340B2 (en) Single chamber compact fuel processor
US7022149B2 (en) Single chamber compact fuel processor
US6824577B2 (en) Nested compact fuel processor for producing hydrogen rich gas
AU2002305234A1 (en) Single chamber compact fuel processor
AU2002226039A1 (en) Apparatus and method for heating catalyst for start-up of a compact fuel processor
AU2002236584A1 (en) Reactor module for use in a compact fuel processor

Legal Events

Date Code Title Description
AS Assignment

Owner name: TEXACO, INC., CALIFORNIA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:KRAUSE, CURTIS;STEVENS, JAMES;NAAE, DOUG;REEL/FRAME:012684/0753

Effective date: 20020206

STCB Information on status: application discontinuation

Free format text: ABANDONED -- AFTER EXAMINER'S ANSWER OR BOARD OF APPEALS DECISION