US20090028783A1 - Gas/solid phase reaction - Google Patents

Gas/solid phase reaction Download PDF

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Publication number
US20090028783A1
US20090028783A1 US11/918,359 US91835906A US2009028783A1 US 20090028783 A1 US20090028783 A1 US 20090028783A1 US 91835906 A US91835906 A US 91835906A US 2009028783 A1 US2009028783 A1 US 2009028783A1
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Prior art keywords
process according
reaction
hydrogen
metal oxide
reactor
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US11/918,359
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English (en)
Inventor
Martin Roeb
Christian Sattler
Peter-Michael Rietbrock
Ruth Kluser
Athanasios G. Konstandopoulos
Christos Agrafiotis
Lamark de Oliveira
Mark Schmitz
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CHEMICAL PROCESS ENGINEERING RESEARCH INSTITUTE CENTER FOR RESEARCH AND TECHNOLOGY-HELLAS (CERTH/CPER)
Deutsches Zentrum fuer Luft und Raumfahrt eV
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Priority claimed from PCT/EP2006/061238 external-priority patent/WO2006108769A1/fr
Assigned to CHEMICAL PROCESS ENGINEERING RESEARCH INSTITUTE CENTER FOR RESEARCH AND TECHNOLOGY-HELLAS (CERTH/CPER), DEUTSCHES ZENTRUM FUR LUFT-UND RAUMFAHRT E.V. reassignment CHEMICAL PROCESS ENGINEERING RESEARCH INSTITUTE CENTER FOR RESEARCH AND TECHNOLOGY-HELLAS (CERTH/CPER) ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KLUSER, RUTH, DE OLIVEIRA, LAMARK, RIETBROCK, PETER-MICHAEL, ROEB, MARTIN, SATTLER, CHRISTIAN, SCHMITZ, MARK, AGRAFIOTIS, CHRISTOS, KONSTANDOPOULOS, ATHANASIOS G.
Publication of US20090028783A1 publication Critical patent/US20090028783A1/en
Abandoned legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J19/12—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electromagnetic waves
    • B01J19/122—Incoherent waves
    • B01J19/127—Sunlight; Visible light
    • 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
    • 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
    • C01B3/061—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 metal oxides with water
    • C01B3/063—Cyclic methods
    • 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
    • B01J2219/00027—Process aspects
    • B01J2219/00038—Processes in parallel
    • 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
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the invention relates to a process and reactor for the quasi-continuous performance of a chemical reaction on the surface of a fixed reactant in a gas/solid phase reaction.
  • the invention relates to a thermal process and a reactor for the continuous preparation of hydrogen from water vapor on the surface of a metal oxide in a gas/solid phase reaction.
  • JP 03205302 A describes the preparation of highly pure hydrogen using activated magnetite as a reactive catalyst.
  • JP 2001270701 A hydrogen is prepared by reacting metallic zinc, magnetite and water at 600° C.
  • this object of the invention is achieved by a process for the quasi-continuous performance of a chemical reaction consisting of at least two sequential reversible steps, characterized in that:
  • reaction chambers in each of which at least one reactant is locally fixed are operated in parallel, wherein cyclically alternating reaction conditions are provided in the reaction chambers.
  • Sequential steps within the meaning of the invention are successive reaction steps of a chemical reaction in which the reaction products can be isolated.
  • Reversible steps within the meaning of the invention are reaction steps in which the chemical equilibrium can be adjusted in such a way that alternatively either the forward or the backward reaction preferably proceeds.
  • a chemical reaction within the meaning of the invention is in principle any chemical reaction in which one of the reactants is fixed and in which the energy is supplied as heat energy, light energy, nuclear energy or in the form of other electromagnetic radiation.
  • the process according to the invention is employed in the following reaction types listed in an exemplary manner:
  • the process according to the invention for solar-thermochemical water splitting on the basis of metal oxides for continuous hydrogen production can be performed continuously by means of the design of an appropriate receiver reactor as described herein.
  • FIG. 1 shows a schematic representation of the time course of different reactions in different reaction chambers in the quasi-continuous process according to the invention.
  • FIG. 2 shows a perspective schematic representation (vertical-horizontal section) of the Konti reactor according to the invention.
  • FIG. 3 shows a horizontal section through the reactor.
  • FIG. 4 shows a representation of the heat-resistant four-way valve in the reactor.
  • a second sequential reaction step other than said first sequential reaction step proceeds at least one time in a second reaction chamber, which is different from the first.
  • the energy input in the reaction chambers can be selected differently to adjust the reaction rates; b) the mass flow of the reactants can be adjusted; and/or c) the number of reaction chambers can be adjusted in accordance with the reaction times in which the reactions proceed in a corresponding time-shifted mode.
  • FIG. 1 it is shown in FIG. 1 how a quasi-continuous process according to the invention can be operated with three reaction chambers for two reaction steps in which the second reaction step takes twice as much time as the first reaction step.
  • all reversible reaction steps of the chemical reaction are preferably performed sequentially in the same reaction chambers.
  • separation or isolation of intermediate products can be dispensed with.
  • radiation-heated reactors are employed as reaction chambers.
  • thermal reactions can be performed with light energy.
  • Any electromagnetic radiation can be employed as the radiation.
  • photoreactions may also advantageously take place when the process is performed. Reactions that are thermal in principle may also proceed in a photoassisted manner, in particular, according to the invention.
  • Photoassisted within the meaning of the invention means that the reaction product is formed with enhancement by a photoreaction.
  • Said cyclically alternating reaction conditions are preferably provided by cycling the temperature of the reaction chambers, for example, by varying the heating power.
  • the required temperature in the reaction chambers is varied by periodically changing the heating power to enable a quasi-continuous product stream.
  • the different thermal addressing of the reactors enables simultaneous reactions of water splitting at a lower temperature and regeneration at a higher temperature.
  • the sequence of these different batch processes enables a quasi-continuous production of hydrogen, for example.
  • the process is performed in several successive cycles is a quasi-continuous reproducible way.
  • one cycle takes a period of time within a range of from 0.3 to 1.5 hours, especially from 0.3 to 1 hour. Over a discontinuous process, this has mainly economical advantages.
  • the cycles may also be substantially shorter or longer.
  • the absorbed energy of the optical component is utilized for heating fluids.
  • Such fluids may be, inter alia, reactants, auxiliary agents or heat transfer media. Being preheated, the fluids do not require that much radiated power in the reactor space any more. It is particularly preferred if the optical component is a tube bundle flowed through by the fluid.
  • fossil energy, electric energy, light energy and/or nuclear energy is preferably employed.
  • the required temperature can be generated by burning fossil energy carriers and/or utilizing electric energy, because usual processes utilize these energy sources.
  • the energy input takes place by light energy, especially by concentrated solar radiation, because this energy source is available at particularly low cost and is suitable for both thermal and photoreactions alike.
  • the generation of the required temperature by means of light energy is advantageous, because conventional energy-producing systems burning fossil energy carriers are not as resource efficient as the process according to the invention, and light energy, such as sunlight, is available worldwide.
  • sunlight can be irradiated into the reaction chamber by means of optical set-ups in order to generate the required temperature.
  • optical set-ups have particularly preferred manifestations, such as solar tower systems, paraboloid concentrators, sun ovens, elliptical or spherical mirrors or line-focusing concentrators.
  • the required radiated power is preferably achieved by a group of heliostats, and the radiated power required for regeneration is achieved by another group of heliostats, the focus of the second group being rearranged onto the individual reaction fields.
  • the heliostat array is separated in such a way that at least one group of heliostats covers the base load of the necessary radiated power in accordance with the reaction step with the lowest energy requirement by being “regularly” tracked in accordance with the daily course of the sun, and that at least one group of heliostats covers additional loads of necessary radiated power for reaction steps with an increased energy requirement by guiding the focus of this group to another area of the radiation receptor at defined intervals respectively after completion of the respective reaction step.
  • reaction chambers are shifted relative to the radiation source in order to vary the heating power.
  • a temperature change can be effected uncomplicatedly thereby while maintaining the radiated power.
  • reaction chambers can preferably be changeable relative to the optical set-up in order to vary the heating power.
  • a temperature change can be effected uncomplicatedly thereby while maintaining the radiated power.
  • optical components For varying the solar-thermal heating power, the use of optical components is advantageously suitable for reducing the irradiation. More particularly, optical attenuators, apertures, deflector mirrors or filters that can be shifted in space or are variable in terms of transparency are suitable for this.
  • This may be advantageously achieved, inter alia, by varying the focal position due to a change in the orientation of mirrors or mirror arrays, so-called heliostat arrays. This can be realized substantially more easily than the shifting of the reactor, which is mostly very heavy.
  • the temperatures employed may also deviate substantially from these values.
  • the fixed reactant in the two reaction chambers is advantageously selected from the group of metal hydrides, dyes, chemical compounds having redox properties, and complexing agents.
  • Chemical compounds having redox properties within the meaning of the invention are those compounds that can be reversibly oxidized and reduced.
  • these chemical compounds having redox properties are selected from the group of metal oxides, mixed metal oxides and/or doped metal oxides.
  • metal oxides have proven particularly advantageous because they are most versatile to employ and can be particularly easily fixed, for example, in contrast to metal hydrides.
  • a multivalent metal oxide is employed as a fixed reactant because it can be fixed and regenerated particularly easily.
  • “Multivalent” within the meaning of the invention means a metal oxide having several coexisting oxidation states, especially if the metal is in an oxidation state of more than +1, especially more than +2.
  • the metal oxides include ferrites and/or zinc oxides and/or manganese oxides and/or cerium oxides and/or lanthanum oxides and/or other lanthanoide oxides and/or oxides of general formula Me x 2+ Zn 1- x 2+ Fe 2 O 4 , wherein Me x 2+ is a divalent metal ion selected from the group of Mg, Ca, Mn, Fe, Co, Ni, Cu, Zn, Sr, Sn, Ba, Cd or Pb, and/or mixtures of such oxides, or oxides with general formula Me′ x Me′′ 1-x FeO, wherein Me′ and Me′′ are metal ions selected from the group of Mg, Ca, Mn, Fe, Co, Ni, Cu, Zn, Sr, Sn, Ba, Cd, Pb or lanthanoides, because these can be employed particularly efficiently in hydrogen splitting, wherein x is a number in a range of from 1 to 5, especially from 2 to 3.
  • the chemical compound having redox properties is employed as a coating of a heat-resistant support structure, more preferably a ceramic one. Due to the use of a support structure, the chemical compound having redox properties need be in the reaction chambers only in a thin layer.
  • a support structure having a conical, hemispherical or paraboloid shape is employed because scattered radiation from the radiation source can be optimally utilized in the reaction chamber thereby.
  • At least one of the mobile reactants is advantageously selected from the group of water, alcohols, carbon dioxide, hydrogen sulfide, nitrogen oxides, hydrocarbons, halo- or pseudohalohydrocarbons, ammonia and sulfur oxides.
  • water has proven to be particularly advantageous because it is readily available and is an easily handled reactant, above all in the gas phase.
  • At least one, more preferably all mobile reactants in the process according to the invention are advantageously gaseous. In this way, the reactant or reactants can be transferred to the reaction chambers particularly easily.
  • at least one and more preferably all mobile reaction products are gaseous, because it is equally easy then to extract them from the reaction chambers.
  • the object of the invention is advantageously achieved by a process for producing hydrogen from water vapor on a surface of at least one chemical compound having redox properties, wherein:
  • water vapor is split by associating oxygen to the excited chemical compound having redox properties to release hydrogen; and in the second step, the chemical compound having redox properties is regenerated at a temperature which is higher than that of the first step to release bound oxygen.
  • the invention can relate to a process of splitting water vapor thermally in a multi-step process by using concentrated radiation and thus producing solar hydrogen.
  • water vapor can be thermally split by concentrated sunlight to produce hydrogen.
  • This is the basis for developing the process according to the invention with which hydrogen can be produced by a solar-thermal process.
  • hydrogen is produced here from water vapor in a two-step cycle process, preferably at temperatures within a range of from 800° C. to 1200° C.
  • What is recirculated, for example, is a metal oxide system that can cleave oxygen from water molecules and reversibly bind it into its crystal structure.
  • metal oxides with different doping are employed and are cyclically oxidized and reduced.
  • the hot water vapor flowing past the metal oxide is split by binding the oxygen to the excited metal oxide lattice at temperatures preferably within a range of from 500 to 1000° C., especially from 550 to 850° C., to release hydrogen.
  • the oxygen previously incorporated into the lattice is released again at temperatures preferably within a range of from 1000 to 1400° C., especially from 1050 to 1350° C., and the metal oxide is regenerated or reduced again to the high-energy state.
  • These temperatures preferably apply to ferrites or iron mixed oxides. More preferably, the reaction temperature may advantageously be within a range of from 600° C.
  • the regeneration temperature may be within a range of from 900° C. to 1200° C.
  • water is split into its elements by means of the metal oxide.
  • the metal oxides employed are advantageously mixed oxides, more preferably zinc-doted ferrites.
  • One important innovation of the process is the advantageous combination of a ceramic support and absorber structure that can be heated at high temperatures with concentrated solar radiation, with a redox system that is capable of reversibly splitting water, for example.
  • a redox system that is capable of reversibly splitting water, for example.
  • porous honeycomb structures functioning as radiation absorbers are coated with ferrites.
  • solids need not be circulated, and because the oxygen binds to the metal oxide, the product separation is reduced to one gas separation.
  • this system enables the water splitting process to be performed at clearly lower temperatures that can be mastered in terms of material technology.
  • the metal oxide is recycled, so that only water is consumed. All these technical advantages also offer economical advantages over other processes for hydrogen production.
  • the ceramic structure coated with metal oxide advantageously forms the core of a receiver reactor.
  • a concentrating solar plant preferably a solar tower
  • the structure is brought to the necessary temperature by the incident concentrated solar radiation.
  • the reactions take place on the surface of the coated ceramics.
  • the reactor is preferably integrated in a small plant for checking and optimizing the operational behavior during water splitting or regeneration.
  • This plant preferably comprises fittings and mass flow controllers for supplying the necessary gases, a water vapor dosing system, measuring systems for pressure and temperature, product gas treatment, and data acquisition and control.
  • the analysis of the concentrations of produced hydrogen or released oxygen is preferably effected by a mass spectrometer.
  • the water vapor is split at a temperature within a range of from 500° C. to 1000° C., especially up to 900° C., even more preferably from 550 to 850° C., and the metal oxide is regenerated at a temperature within a range of from 1000° C. to 1400° C., especially from 1050 to 1350° C.
  • temperatures of a few thousand degrees, but at least 2000° C. for one-step thermal water splitting.
  • the lower temperature range is more easily handled in terms of materials and process technology and significantly reduces the cost of the process.
  • the object of the invention is preferably achieved by a process for the quasi-continuous production of hydrogen from water vapor on a surface of a metal oxide followed by regeneration of the surface.
  • the object of the invention is achieved by a thermal process for the preparation of hydrogen from water vapor on a surface of a metal oxide in a gas/solid phase reaction, wherein in a reaction chamber, in a first step, water vapor is split by associating oxygen to the excited metal oxide to release hydrogen, and in a second step, the metal oxide is regenerated at a temperature which is higher than that of the first step to release bound oxygen, so that the metal oxide is available for further reactions.
  • the invention relates to a process for thermally splitting water vapor in a multistep process by utilizing concentrated radiation and thus to produce solar hydrogen.
  • the object of the invention is achieved by a photoreactor for performing the process according to the invention, characterized by having two reaction chambers.
  • the object of the invention is achieved by a radiation-heated reactor for performing the process according to the invention, characterized by having two reaction chambers.
  • This reactor is preferably a reactor for the thermal preparation of hydrogen from water vapor on a surface in a gas/solid phase reaction comprising at least one connected tube that enables a gas stream of educt gases to flow into a reaction chamber and of product gases to flow out, and a heat source, metal oxide being provided as a reactant in one reaction chamber.
  • the metal oxide is coated on a heat-resistant ceramic support structure in the reactor.
  • This fixation has the advantage that the metal oxide is always available and thus can be exposed to the heat source optimally in the reactor. Due to the fixation of the metal oxide on the support structure, the metal oxide need not be recovered tediously by separation processes.
  • the heat necessary for the reactions can also be supplied out of the support structure.
  • the ceramic support structure consists of a porous honeycomb structure, because porous ceramic honeycomb structures have proven particularly heat-resistant. Pores within the meaning of this invention are the interstices formed by the honeycomb structure. This does not exclude that the material as such advantageously has itself a porosity within a range of from 10 to 60%. The porosity is obtained from the weight ratio of the actual weight to the weight when the theoretical maximum density is assumed.
  • the ceramic support structure has a conical, hemispherical or paraboloid shape in order to capture the radiation optimally onto the metal oxide.
  • peripheral radiation can also be captured more readily thereby.
  • the reaction chamber is advantageously provided with a transparent window because the light source can be arranged outside the actual reactor in this way.
  • tubes that attenuate the energy flow run between the reaction chamber and energy source, because this enables a better control of the reaction.
  • the tubes contain a fluid because the heat exchange can be adjusted individually thereby.
  • the reactor is advantageously provided with a multiport valve to enable the supply of the gaseous educts.
  • the multiport valve has such a design that the gaseous products can be removed separately.
  • the reactor has a modular structure consisting of at least two reaction chambers, because the quasi-continuous process described above can be implemented particularly easily thereby.
  • the two reaction chambers are alternately provided with water vapor or inert gas, especially nitrogen, the switching being effected in such a way that a hydrogen production constant in time is provided.
  • the metal oxides are ferrites and/or zinc oxides and/or manganese oxides and/or lanthanum oxides and/or oxides of general formula Me x 2+ Zn 1- x 2+ Fe 2 O 4 , wherein Me x 2+ is a divalent metal ion selected from the group of Mg, Ca, Mn, Fe, Co, Ni, Cu, Zn, Sr, Sn, Ba, Cd, Pb or lanthanoides, and/or mixtures of such oxides, because these can be employed particularly efficiently in water splitting, wherein x is a number within a range of from 1 to 5, especially from 2 to 3.
  • a concentrating solar-thermal system such as a solar tower system, a paraboloid concentrator, a sun oven, an elliptical or spherical mirror or a line-focusing concentrator, is employed as the energy source.
  • the required radiated power is achieved by a group of heliostats, and the radiated power required for regeneration is achieved by another group of heliostats, the focus of the second group being rearranged onto the individual reaction fields.
  • FIG. 2 shows the receiver reactor, the concentrated solar radiation being incident from the right-hand side onto the aperture with quartz windows ( 1 ).
  • the power of the incident light can be adjusted by an aperture.
  • the receiver reactor is based on the connection as described above of the metal oxide redox system with a support and absorber structure which consists of a ceramic monolith having a honeycomb structure ( 2 ).
  • the monolith is coated with the metal oxide and built into a cylindrical housing ( 3 ).
  • the honeycomb structure enables high temperatures to be generated with low back radiation losses.
  • the reactor consists of a modular two-component system of permanently installed honeycomb-like absorbers. Two neighboring, but separated reaction chambers form a minimum arrangement of modules for the continuous production of hydrogen.
  • the square aperture ( 1 ) allows the formation of large and flexible receiver areas by serial connection of individual modules.
  • a double tube is provided for preheating the supplied gases nitrogen and water vapor by recovering the heat from the product gas ( 4 ).
  • the operation of the Konti reactor is based on the simultaneous use of the two modules. While water is split in one of the reaction chambers, regeneration takes place in the other. After the reactions are completed, the regenerated module is switched for splitting and vice versa by swapping the gas supply. A precondition of this continuous operation and the hydrogen production is the separate supply of nitrogen gas, which is employed as a carrier gas or scavenging gas, and water vapor ( 6 ). In addition, separate lines for the products of the splitting on the one hand and for the oxygen-containing scavenging gas for the regeneration on the other hand are necessary ( 7 ). This is enabled by four-way valves ( 5 and 5 a ), which are respectively switched over after a reaction step is completed. One of these valves ( 5 ) must withstand high temperatures of up to 600° C. FIG. 4 shows the positions of this valve.
  • the two steps of the process are performed in the same reactor at different temperature levels with a different heat demand.
  • the regeneration is endothermal and advantageously proceeds within a temperature range of from 1100 to 1200° C.
  • the splitting of the water vapor is slightly exothermal and takes place at 800° C. Therefore, part of the modules (regeneration) requires a higher solar flux density (intensity) as compared to the second part, i.e., that for the splitting of water, which demands only a little energy for the compensation of heat losses.
  • cycling of the irradiation intensity is required when the cycle is switched over from regeneration to splitting or vice versa.
  • a change of mirror focusing between two equal foci by suitably adjusting the concentrating mirrors of the solar plant is provided.
  • the periodic change of the irradiation intensity is achieved by optical components that can be changed in time, for example, optical lattices as attenuators, deflector mirrors or semitransparent mirrors.
  • optical components that can be changed in time, for example, optical lattices as attenuators, deflector mirrors or semitransparent mirrors.
  • Such a component is moveable and is positioned in front of one of the two apertures. When the supplied gas is changed, the position of the component can be switched over accordingly. It is also possible, though with higher technical expenditure, to change the receiver position in time between locations with different irradiation intensities.

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US11/918,359 2005-04-14 2006-03-31 Gas/solid phase reaction Abandoned US20090028783A1 (en)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE102005017216.4 2005-04-14
DE102005017216A DE102005017216A1 (de) 2005-04-14 2005-04-14 Thermische Wasserstoffherstellung in einer Gas-Festphasenreaktion
EP05106614.0A EP1712517B1 (fr) 2005-04-14 2005-07-19 Réaction entre un gaz et une phase solide
EP05106614.0 2005-07-19
PCT/EP2006/061238 WO2006108769A1 (fr) 2005-04-14 2006-03-31 Reaction gaz-phase solide

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US13/011,667 Active US9492807B2 (en) 2005-04-14 2011-01-21 Gas/solid phase reaction

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EP (1) EP1712517B1 (fr)
CY (1) CY1117055T1 (fr)
DE (1) DE102005017216A1 (fr)
ES (1) ES2558865T3 (fr)
PT (1) PT1712517E (fr)
ZA (1) ZA200708374B (fr)

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US20070196268A1 (en) * 2006-02-22 2007-08-23 Smith John R Thermal activation of photocatalytic generation of hydrogen
US20090321244A1 (en) * 2008-06-25 2009-12-31 Hydrogen Generation Inc. Process for producing hydrogen
US20110076575A1 (en) * 2008-05-20 2011-03-31 Commissariat A L'energie Atomique Et Aux Energies Alternatives System for the autonomous generation of hydrogen for an on-board system
US20130004801A1 (en) * 2011-07-01 2013-01-03 Asegun Henry Reactor, system and method for solid reactant based thermochemical processes

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WO2014053168A1 (fr) 2012-10-02 2014-04-10 Caterpillar Energy Solutions Gmbh Production d'hydrogène à partir d'eau
DE102013213330B4 (de) 2013-07-08 2020-06-10 Deutsches Zentrum für Luft- und Raumfahrt e.V. Regeneration von inertem Spülgas beim Betrieb solarthermischer Kreisprozesse
DE102014210482A1 (de) 2014-06-03 2015-12-03 Deutsches Zentrum für Luft- und Raumfahrt e.V. Wärmeträgerpartikel für solarbetriebene, thermochemische Prozesse
DE102014213987B4 (de) * 2014-07-17 2018-05-17 Deutsches Zentrum für Luft- und Raumfahrt e.V. Solare Ammoniakproduktion
DE202014006825U1 (de) 2014-08-18 2014-09-17 Anatoly Borodin Reaktor für die Durchführung eines zweistufigen thermochemischen Wasserstoffherstellungsverfahrens
CN112383997B (zh) * 2020-10-05 2024-10-25 四川大学 一种大功率微波等离子体煤粉裂解装置
WO2022218969A1 (fr) 2021-04-13 2022-10-20 Uestuen Orhan Procédé et dispositif de production d'hydrogène
WO2023079017A1 (fr) * 2021-11-05 2023-05-11 Sms Group Gmbh Procédé et dispositif de réduction d'oxyde métallique au moyen d'un gaz ou d'un mélange gazeux réducteur à l'aide de chaleur solaire
DE102021128851A1 (de) * 2021-11-05 2023-05-11 Sms Group Gmbh Verfahren und Verarbeitungssystem zum Erwärmen und Weiterverarbeiten von metallhaltigen Produkten unter Nutzung von Solarthermie
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US20110135566A1 (en) 2011-06-09
US9492807B2 (en) 2016-11-15
EP1712517B1 (fr) 2015-11-11
EP1712517A1 (fr) 2006-10-18
DE102005017216A1 (de) 2006-10-19
PT1712517E (pt) 2016-01-25
ES2558865T3 (es) 2016-02-09

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