Classifications

• • 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
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  • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
  • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/24—Stationary reactors without moving elements inside
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  • B01J19/2485—Monolithic reactors
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  • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
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  • B01J23/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the alkali- or alkaline earth metals or beryllium
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  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
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  • B01J23/56—Platinum group metals
  • B01J23/58—Platinum group metals with alkali- or alkaline earth metals
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  • B01J23/56—Platinum group metals
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  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/78—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali- or alkaline earth metals
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  • B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
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  • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/894—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
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  • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/8946—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali or alkaline earth metals
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  • 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
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  • 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
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  • 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
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
  • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
  • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
  • C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
• • B—PERFORMING OPERATIONS; TRANSPORTING
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  • B01J2208/00407—Controlling the temperature using electric heating or cooling elements outside the reactor bed
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• • C—CHEMISTRY; METALLURGY
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  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
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  • 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
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• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Definitions

• the present invention relates to a process for the production of synthesis gas, comprising the steps of providing a flow reactor, setting thresholds, comparing energy prices, energy composition with respect to regenerative sources and / or desired ratios of IL to CO, and selection between dry reforming / steam reforming modes on the one hand and reverse water gas shift reaction on the other.
• An alternative method is autothermal reforming.
• a portion of the fuel is burned by the addition of oxygen within the reformer, so that the reaction gas is heated and the expiring endothermic reactions are supplied with heat.
• DE 10 2007 022 723 A1 and US 2010/0305221 describe a process for the production and conversion of synthesis gas, which is characterized in that it has a plurality of different operating states which essentially comprise the alternating (i) daytime operation and (ii) nighttime operation where the daily operation (i) mainly comprises dry reforming and steam reforming under the supply of regenerative energy and night operation (ii) mainly the partial oxidation of hydrocarbons and wherein the produced synthesis gas is used for the production of value products.
• US 2007/003478 Al discloses the production of synthesis gas with a combination of steam reforming and oxidation chemistry. The process involves the use of solids to heat the hydrocarbon feed and cool the gaseous product.
• WO 2007/042279 AI deals with a reformer system with a reformer for the chemical reaction of a hydrocarbon-containing fuel in a hydrogen gas-rich reformate gas, and electric heating means by which the reformer heat energy for producing a reaction temperature required for the feed can be supplied, wherein the reformer system further comprises a capacitor has, which can supply the electric heating means with electric current.
• WO 2004/071947 A2 / US 2006/0207178 A1 relate to a system for the production of hydrogen, comprising a reformer for generating hydrogen from a hydrocarbon fuel, a compressor for compressing the hydrogen produced, a renewable energy source for converting a hydrogen renewable resource into electrical energy for driving the compressor and a storage device for storing the hydrogen from the compressor.
• the object of the present invention is to provide such a method.
• it has set itself the task of specifying a method for the production of synthesis gas, which is suitable for an alternating operation between two different modes of operation.
• a method for the production of synthesis gas comprising the steps a) providing a flow reactor, which is arranged for the reaction of a fluid comprising reactants, wherein the reactor comprises at least one heating level, which is electrically heated by means of one or more heating elements, wherein the heating level can be traversed by the fluid and at least one heating element, a catalyst is arranged and is heated there; b) setting a threshold value S l for the costs of the electrical energy available for the flow reactor and / or a threshold value S2 for the relative proportion of electrical energy from regenerative sources of the electrical energy available for the flow reactor and / or a threshold S3 for a desired ratio of hydrogen to carbon monoxide in the resulting synthesis gas; and c) comparing the costs of the electrical energy available for the flow reactor with the threshold value S l and / or the relative proportion of electrical energy from regenerative sources of the electrical energy available for the flow reactor with the threshold value S2 and / or the ratio from hydrogen too
• Carbon monoxide in the resulting synthesis gas with the threshold S3 d) reaction of hydrocarbons with carbon dioxide and / or water in the flow reactor, wherein carbon monoxide and hydrogen are formed, with electric heating by one or more heating elements, when the threshold value S l falls below and / or the floating value S2 exceeded and / or the Threshold S3 be fallen below, wherein at least a portion of the hydrogen formed is fed to a storage and / or a reaction in another reactor is fed; e) Reaction of carbon dioxide with hydrogen in the flow reactor, wherein carbon monoxide and water are formed, under electrical heating by one or more heating elements, when the threshold value S 1 is exceeded and / or the threshold value S2 is exceeded and / or the threshold value S3 is exceeded in which at least part of the hydrogen used originates from the previously stored hydrogen and / or originates from a reaction in another reactor.
• the first threshold S l relates to the electricity costs for the reactor, in particular the cost of electrical heating of the reactor by the heating elements in the Fleizebenen. Here it can be determined to what extent the electric heating of the respective endothermic reaction is still economically reasonable.
• the second threshold S2 relates to the relative proportion of electrical energy from regenerative sources available to the reactor and, in particular, to the electrical heating of the reactor by the heating elements in the heating levels.
• the relative proportion is in this case based on the total electrical energy of the electric current available for the flow reactor and can of course vary over time. Examples of regenerative sources from which electrical energy can be derived are wind, solar, geothermal, wave and hydro.
• the relative share can be determined by providing information to the energy supplier. If, for example, a plant's own regenerative energy sources such as solar power plants and wind turbines are used, this relative proportion of energy can also be indicated via performance monitoring.
• the third threshold S3 relates to the requirements of the users of the synthesis gas in terms of its composition. Depending on your wishes, you can operate between an excess of hydrogen and a deficit.
• the threshold value S l can be understood as a price upper limit
• the visual threshold value S2 can be regarded as a requirement to use renewable energies to the greatest extent possible.
• S2 may mean that from a proportion of 5%, 10%, 20% or 30% of electrical energy from renewable sources, the electrical heating of the reactor should take place.
• a comparison of the desired values with the actual values in the method can now reach the conclusion that electrical energy is available inexpensively, enough electrical energy is available from renewable sources and / or the desired composition of the synthesis gas is maintained. Then the flow reactor is operated so that, for example, run a dry reforming reaction or a steam reforming reaction.
• the hydrocarbons involved are preferably alkanes, alkenes, alkynes, alkanols, alkenols and / or alkynols.
• alkanes methane is particularly suitable, among the alkanols methanol and / or ethanol are preferred.
• the RWGS reaction of methane is much less endothermic at +41 kJ / mol and is therefore suitable for times of high energy prices or too low a share of electrical energy from renewable sources.
• the combustion of hydrogen can be used. It is both possible that the combustion of hydrogen in the RWGS reaction by metering of O2 into the educt gas (ideally, a locally distributed or lateral metering) takes place, as well as possible hydrogen-rich residual gases (for example, PSA exhaust gas), as be incurred in the purification of the synthesis gas, recycled and burned together with O2, which then the process gas is heated.
• hydrogen-rich residual gases for example, PSA exhaust gas
• endothermic reactions are heated from the outside through the walls of the reaction tubes. Opposite is the autothermal reforming with 02 addition.
• the endothermic reaction can be efficiently internally supplied with heat via an electrical heating within the reactor (the undesired alternative would be electrical heating via radiation through the reactor wall).
• This type of reactor operation is particularly economical if the excess supply resulting from the expansion of renewable energy sources can be used cost-effectively.
• the hydrogen required for the desired ifc / CO ratio can then be added again.
• the first option is to store the hydrogen withdrawn during the DR and SMR reactions in suitable storage tanks and then add it to the product of the RWGS reaction in an appropriate amount.
• the cheaper for a Verbund site under certain circumstances - in a variant the extracted hydrogen is consumed in other reactions and, if necessary, is taken from hydrogen-producing reactions elsewhere in the Verbund site. Likewise, it is possible to feed the hydrogen into a central line of the site and to remove the required hydrogen from this line.
• the process according to the invention provides for the DR, SMR and RWGS reactions to proceed in the same reactor. A mixed operation of two or three of the reactions is expressly intended.
• One of the advantages of this approach is the gradual onset of the other reaction, for example, by continuously reducing the hydrogen supply while increasing the methane feed, or by continuously increasing the hydrocarbon feed while reducing the methane feed.
• the degree of endothermy can be set arbitrarily.
• FIG. 1 shows schematically a flow reactor in an expanded representation.
• the hydrogen is stored in pressure accumulators, in caverns, in the form of hydrides and / or in the form of organic compounds.
• Suitable pressure accumulators are, for example, pressure vessels, tube stores or pipelines.
• Suitable hydride compounds are especially elemental hydrogen compounds such as PtH 2 , Mni l.
• the hydrogen used in the reaction of carbon dioxide with hydrogen, at least part of the hydrogen used originates from the electrolysis of water.
• the operating strategy of the water electrolysis can also be coupled to the parameters S l and S2: the electrolysis is carried out when the eleutician electric energy is cheap and / or if the proportion of electrical energy from renewable sources is large enough. This operating strategy yields an additional degree of freedom for the initial hydrogenation of RWGS phases.
• the flow reactor comprises in the flow direction of the fluid a plurality of heating levels, which are electrically heated by heating elements and wherein the heating levels are permeable by the fluid, wherein a catalyst is arranged on at least one heating element and is heatable there, wherein further at least once an intermediate plane between two heating levels is arranged and wherein the intermediate plane is also traversed by the fluid.
• FIG. 1 schematically shown flow reactor used according to the invention is flowed through by a fluid comprising reactants from top to bottom, as shown by the arrows in the drawing.
• the fluid may be liquid or gaseous and may be single-phase or multi-phase.
• the fluid is gaseous. It is conceivable that the fluid contains only reactants and reaction products, but also that additionally inert components such as inert gases are present in the fluid.
• the reactor has a plurality of (four in the present case) heating levels 100, 101, 102, 103, which are electrically heated by means of corresponding heating elements 110, 111, 112, 13.
• the heating levels 100, 101, 102, 103 are flowed through during operation of the reactor of the fluid and the heating elements 1 10, 1 1 1, 1 12, 1 13 are contacted by the fluid. At least one heating element 1 10, 1 1 1, 1 12, 1 13, a catalyst is arranged and is heated there.
• the catalyst may be directly or indirectly connected to the heating elements 1 10, 1 1 1, 1 12, 1 13, so that these heating elements represent the catalyst support or a support for the catalyst support.
• the heat supply of the reaction takes place electrically and is not introduced from the outside by means of radiation through the walls of the reactor, but directly into the interior of the reaction space. It is realized a direct electrical heating of the catalyst.
• a ceramic intermediate level 200, 201, 202 between two levels of fuel 100, 101, 102, 103 are arranged, wherein the intermediate level (s) 200, 201, 202 are also traversed by the fluid in the operation of the reactor. This has the effect of homogenizing the fluid flow. It is also possible that additional Catalyst in one or more intermediate levels 200, 201, 202 or further Isolationsseiementen in the reactor is present.
• Said at least one intermediate ceramic layer is preferably supported by a ceramic or metallic support frame and / or a ceramic or metallic support plane.
• the material forms an AhC protective layer by the action of temperature in the presence of air / oxygen.
• This passivation layer can serve as a basecoat of a washcoat, which acts as a catalytically active coating.
• the direct resistance heating of the catalyst or the heat supply of the reaction is realized directly through the catalytic structure.
• the formation of other protective layers such as Si-O-C systems.
• the pressure in the reactor can take place via a pressure-resistant steel jacket. Using suitable ceramic insulation materials it can be achieved that the pressure-bearing steel is exposed to temperatures of less than 200 ° C and, if necessary, less than 60 ° C.
• the electrical connections are shown in FIG. 1 only shown very schematically. They can be performed in the cold area of the reactor within an insulation to the ends of the reactor or laterally from the Schuel ementen 1 10, 1 1 1, 1 12, 1 13 performed so that the actual electrical connections can be provided in the cold region of the reactor can.
• the electrical heating is done with direct current or alternating current. By appropriate shaping an increase in surface area can be achieved. It is possible that in the heating levels 100, 101, 102, 103 heating elements 1 10, 1 1 1, 1 12, 1 13 are arranged, which are spirally, meandering, lattice-shaped and / or net-shaped.
• At least one heating element 1 10, 11 1, 12, 13 can have a different amount and / or type of catalyst than the remaining heating elements 110, 11, 12, 13.
• the heating elements 1 10, 1 1 1, 1 12, 1 13 are arranged so that they can each be electrically heated independently.
• the individual heating levels can be individually controlled and regulated.
• In the reactor inlet area can be dispensed with a catalyst in the heating levels as needed so that only the heating and no reaction takes place in the inlet area. This is particularly advantageous in view of starting the reactor.
• a temperature profile adapted for the respective reaction can be achieved. With regard to the application for endothermic equilibrium reactions, this is, for example, a temperature profile which reaches the highest temperatures and thus the highest conversion at the reactor outlet.
• the (for example ceramic) intermediate levels 200, 201, 202 or their contents 210, 21 1, 212 comprise a material resistant to the reaction conditions, for example a ceramic foam. They serve for mechanical support of the heating levels 100, 101, 102, 103 and for mixing and distribution of the gas stream. At the same time an electrical insulation between two heating levels is possible. It is preferred that the material of the content 210, 2 1 1, 212 of an intermediate level 200, 201, 202 comprises oxides, carbides, nitrides, phosphides and / or borides of aluminum, silicon and / or zirconium. An example of this is SiC. Further preferred is cordierite.
• the intermediate level 200, 201, 202 may comprise, for example, a loose bed of solids and / or a one-piece porous solid. These solids themselves may be porous or solid, so that the fluid flows through gaps between the solids.
• the case of the one-piece porous solid is shown in FIG. 1 shown.
• the fluid flows through the intermediate plane via the pores of the solid.
• the material of the solid bodies comprises oxides, carbides, nitrides, phosphides and / or borides of aluminum, silicon and / or zirconium. An example of this is SiC. Further preferred is cordierite.
• Another conceivable possibility is that one or more of the intermediate levels are voids.
• the average length of a heating level 100, 101, 102, 103 is viewed in the direction of flow of the fluid and the average length of an intermediate level 200, 201, 202 in the direction of flow of the fluid is in a ratio of> 0.01: 1 to ⁇ 100: 1 to each other. Even more advantageous are ratios of> 0, 1: 1 to ⁇ 10: 1 or 0.5: 1 to ⁇ 5: 1.
• Suitable catalysts can be selected for example from the group consisting of: (I) mixed metal oxides of the formula A (i-w-x) A 'A "x B (iy z) B' y B" z 03-Deita where:
• A, A 'and A are independently selected from the group: Mg, Ca, Sr, Ba, Li, Na, K, Rb, Cs, Sn, Sc, Y, La, Ce, Pr, Nd, Pm, Sm Lu, Gd, Tb, Dy, Ho, Er, Tm. Yb, i ' l, Lu.
• B, B 'and B are independently selected from the group: Cr, Mn, Fe, Bi, Cd,
• A, A 'and A are independently selected from the group: Mg, Ca, Sr, Ba, Li, Na, K. Rb, Cs, Sn, Sc, Y. La, Ce, Pr. Nd, Sm. Lu Gd, Tb, Dy. Ho, Er, Tm. Yb. ⁇ 1, Lu, Ni,
• B is selected from the group: Cr, Mn, Fe, Bi, Cd, Co, Cu, Ni, Sn, Al, Ga, Sc, Ti, V, Nb, Ta, Mo, Pb. I i f. Zr. Tb. W, Gd. Yb. Mg, Cd, Zn, Re, Ru. Rh. Pd, Os, Ir and / or Pt; and
• B ' is selected from the group: Re, Ru, Rh, Pd, Os, Ir and / or Pt;
• B is selected from the group: Cr, Mn, Fe, Bi, Cd, Co, Cu, Ni, Sn, Al, Ga, Sc, Ti, V, Nb, Ta, Mo, Pb, II, Zr, Tb W, Gd, Yb, Mg, Cd and / or Zn;
• Ml and M2 are independently selected from the group: Re, Ru, Rh, Ir, Os, Pd and / or Pt;
• M3 is selected from the group: Sc, Y, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, I lo, Er, Tm, Yb and / or Lu;
• L is selected from the group: Na, K, Rb. Cs, Mg, Ca, Sr, Ba, Sc, Y, Sn, Pb, Pd, Mn, In,
• M is selected from the group: " I i, Zr, II for V, Nb, Ta, Cr, Mo, W, Mn, Re, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt, Zn, Cu, Ag and / or Au, and
• L is selected from the group: Na, K, Rb. Cs, Mg, Ca, Sr, Ba, Sc, Y, Sn, Pb, Mn, In, Tl, La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb and / or Lu; and
• Ml and M2 are independently selected from the group: Cr, Mn, Fe, Co, Ni, Re, Ru, Rh, Ir, Os, Pd, Pt, Zn, Cu, La, Ce, Pr, Nd, Sm, Eu , Gd, Tb, Dy, FIo, Er, Tm, Yb, and / or Lu;
• a and B are independently selected from the group: Be, Mg, Ca, Sc, Ti, V, Cr, Mn, Fe, Co, Ni, Y, Zr, Nb, Mo, I I f. Ta, W, La. Ce, Pr. Nd, Sm. Eu, Gd. Tb. Y. l io. He,
• Tm Tm, Yb, and / or Lu;
• reaction products includes the catalyst phases present under reaction conditions. Preferred are for:
• the reactor according to the invention may be modular.
• a module may include, for example, a heating level, an intermediate level, the electrical contact and the corresponding further insulation materials and thermal insulation materials.
• an electric heating of at least one of the heating elements 110, 1111, 112, 13 takes place in the reactor provided. This can, but does not have to, be before the passage of a reactant through the flow reactor under at least partial reaction of the reactants of the fluid respectively.
• the reactor can be modular.
• a module can contain, for example, a heating level, an insulation level, electrical contact, and the corresponding further insulation materials and thermal insulation materials.
• the individual heating elements 110, 111, 112, 113 are operated with a respective different heating power.
• the reaction temperature in the reactor is at least in places> 700 ° C to ⁇ 1300 ° C. More preferred ranges are> 800 ° C to ⁇ 1200 ° C and> 900 ° C to ⁇ 1100 ° C,
• the average (median) contact time of the fluid to a heating element 110, 111, 112, 113 may be for example> 0.01 seconds to ⁇ 1 second and / or the average contact time of the fluid to an intermediate level 110, 111, 112, 113 may For example, be> 0.001 seconds to ⁇ 5 seconds.
• Preferred contact times are> 0.005 to ⁇ 1 second, more preferably> 0.01 to ⁇ 0.9 seconds.
• the reaction can be carried out at a pressure of> 1 bar to ⁇ 200 bar.
• the pressure is> 2 bar to ⁇ 50 bar, more preferably> 10 bar to ⁇ 30 bar.

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• 2013
  • 2013-03-12 WO PCT/EP2013/054959 patent/WO2013135667A1/fr not_active Ceased

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