Classifications

• • 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
  • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
  • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
• • 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
• • 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
  • B01J2219/00117—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
• • 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
  • B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/02—Processes for making hydrogen or synthesis gas
  • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
  • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
  • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
• • 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
  • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation 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
  • C01B2203/08—Methods of heating or cooling
  • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
  • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
• • 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
  • C01B2203/12—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
  • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
  • C01B2203/143—Three or more reforming, decomposition or partial oxidation steps in series

Definitions

• a disadvantage of the known reformer is the partially incomplete reaction in synthesis gas, especially when using space-saving reformer. By using large reforming zones, the conversion efficiency can be increased; However, especially in the automotive sector, the increased space requirement is undesirable.
• a reformer according to the preamble of claim 6 is known.
• the fuel and combustion exhaust gas from the oxidation zone i. the fuel / oxidizer mixture is first mixed in a feed device upstream of the reforming zone and injected together into the reforming zone. This results in an improvement in the homogeneity of the gas to be reacted, which leads to an increase in the efficiency of the reforming.
• a disadvantage of the known, common feeding device is the technical complexity of the injection device required for this purpose. This requires a complicated mechanism and control electronics, which leads to undesirable cost increase.
• the invention is based on a reformer according to the preamble of claim 1, characterized in that the reforming zone a in the gas flow direction first and a second gas flow in the second catalytic reaction zone, which are arranged separately from each other and which a non-catalytically active homogenizing zone for homogenizing exiting from the first reaction zone gas components is interposed.
• the inner surfaces of the or the pore body are coated with catalytically active material. This supports the desired conversion of the starting gases and production of the synthesis gas.
• the porosity-free homogenization zone serves for thorough mixing of the gas components emerging from the first reaction zone. This mixing is compared to the homogenization before introduction into the first reaction zone by the larger diffusion coefficients of the synthesis gas components, i. of hydrogen and carbon monoxide, as compared to the hydrocarbon
• the homogenization zone has one or more gas conducting elements for generating turbulence.
• gas conducting elements for generating turbulence.
• gas guide elements are suitable, which are known from the flow technology for the generation of turbulence.
• a ring diaphragm is technically easy and inexpensive to implement.
• the annular diaphragm also leads to an acceleration of the gas Stream, so that the introduction into the second reaction zone is improved.
• the invention is based on the reformer according to the preamble of claim 6, characterized in that the feed device is formed as an annular, with its ' end face with the reforming tion zone coupled mixing chamber through openings in their front end fuel or mixture and through openings in their lateral surface mixture or fuel can be supplied.
• This special embodiment of the common feeder for fuel and fuel / oxidant mixture is technically particularly simple executable and therefore particularly advantageous both in terms of the costs incurred and the required space.
• the introduction of the mixture via the openings in the lateral surface of the mixing chamber is advantageous.
• the introduction of fresh fuel via openings in the front end side can be done.
• the mixing in the mixing zone is particularly effective, since two gas streams meet here substantially perpendicular to one another.
• the gas flow introduced via the apertures in the inlet end face has a substantially axial orientation, while the gas flow introduced via the apertures in the lateral surface is directed essentially radially inwards.
• the clear cross section of the mixing zone is reduced from the inlet end side to the outlet end side.
• the mixing zone can be configured as an annular nozzle.
• the mixing chamber as a whole has only a very small volume, in particular only a small axial extent, so that the residence times of the gas components in the mixing chamber are in the range of a few milliseconds, which corresponds approximately to typical reaction times for oxidation reactions of relevance here ,
• the skilled person can make a suitable adjustment of the mixing chamber length to the occurring gas flow rates.
• Figure 2 is an enlarged sectional view through a
• FIG. 3 is a plan view of the mixing chamber central body of FIG. 2.
• FIG. 1 shows a sectional view through a reformer system 10 according to the invention.
• the reformer system 10 comprises the actual reformer 12, a mixing chamber 14 connected thereto and a combustion exhaust gas pipe 16 surrounding it.
• the reformer 12 is equipped with its upstream mixing chamber 14 formed substantially cylindrical, wherein one of a first cylinder jacket 18 enclosed assembly includes the reformer 12 and the upstream mixing chamber 14.
• the first cylinder jacket 18 is arranged coaxially in a second cylinder jacket 20 of larger diameter.
• the space 16 between the cylinder jackets 18 and 20 is connected to the outlet of an oxidation zone, not shown, and passes combustion exhaust gas flowing out of the oxidation zone. Due to the flow around the reformer 12th With the hot combustion exhaust gas there is a heat exchange between the combustion exhaust gas and the reformer 12, so that the thermal energy of the combustion exhaust gas can be used to support the endothermic, catalytic reforming.
• Adjoining the end plate 26 is a truncated cone or hollow truncated conical body 30, the base of which forms the inner region of the outlet end face of the mixing chamber 14 and is coupled to the inlet surface of a first reaction chamber 32 of the reformer 12.
• the diameter of the base of the cone body 30 is less than the diameter of the first cylinder shell 18 and thus less than the diameter of the mixing chamber 14. From end plate 26, cone body 30 and cylinder shell 18 is thus an annular mixing chamber 14 with decreasing towards its output clear
• the cover element 38 is gas-tightly connected to a fuel supply line 42, via which gaseous, fresh fuel can be introduced into the gas distribution chamber 38 and then via the openings 28 into the mixing chamber 40.
• combustion exhaust gas is simultaneously introduced into the mixing chamber 14 via the apertures 34 where it is mixed with the fresh fuel. Due to the reduction in cross-section, which is caused by the conical body 30, there is an acceleration of the gas flow through the mixing chamber 14 into the first reaction zone of the reformer 12.
• the first reaction zone 32 is completely filled with a pore body whose inner surfaces are covered with catalytic material, at which the synthesis gas production takes place.
• the output of the second reaction zone 48 is not shown in FIG. In him, in advantageous embodiments of the invention derivatives for skimming the resulting synthesis gas, in particular for supplying the synthesis gas to a downstream fuel cell, are.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Chemistry (AREA)
• Health & Medical Sciences (AREA)
• General Health & Medical Sciences (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Inorganic Chemistry (AREA)
• Hydrogen, Water And Hydrids (AREA)

Applications Claiming Priority (2)

Publications (1)

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Family Applications (1)

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• 2006
  • 2006-08-25 DE DE102006039933A patent/DE102006039933A1/de not_active Ceased
• 2007
  • 2007-07-06 WO PCT/DE2007/001204 patent/WO2008022610A1/de active Application Filing
  • 2007-07-06 US US12/377,451 patent/US20110058996A1/en not_active Abandoned
  • 2007-07-06 AU AU2007287913A patent/AU2007287913A1/en not_active Abandoned
  • 2007-07-06 CA CA002660675A patent/CA2660675A1/en not_active Abandoned
  • 2007-07-06 EP EP07785602A patent/EP2054147A1/de not_active Withdrawn
  • 2007-07-06 EA EA200970218A patent/EA200970218A1/ru unknown
  • 2007-07-06 CN CNA2007800314986A patent/CN101588861A/zh active Pending
  • 2007-07-06 JP JP2009524893A patent/JP2010501452A/ja not_active Withdrawn

Non-Patent Citations (1)

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