WO2020048556A1 - Réacteur à hydrogène et le procédé de chimie régéneratif - Google Patents

Réacteur à hydrogène et le procédé de chimie régéneratif Download PDF

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Publication number
WO2020048556A1
WO2020048556A1 PCT/DE2018/000255 DE2018000255W WO2020048556A1 WO 2020048556 A1 WO2020048556 A1 WO 2020048556A1 DE 2018000255 W DE2018000255 W DE 2018000255W WO 2020048556 A1 WO2020048556 A1 WO 2020048556A1
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Prior art keywords
gas
reactor
hydrogen
reaction
temperature
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PCT/DE2018/000255
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German (de)
English (en)
Inventor
Christoph Gregor WANDZIK
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Wandzik Christoph Gregor
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Priority to PCT/DE2018/000255 priority Critical patent/WO2020048556A1/fr
Priority to DE112018007957.0T priority patent/DE112018007957A5/de
Publication of WO2020048556A1 publication Critical patent/WO2020048556A1/fr

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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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/004—Sparger-type elements
    • 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
    • B01J15/00—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor
    • B01J15/005—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
    • 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
    • B01J19/08—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
    • B01J19/2415—Tubular 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
    • B01J19/28—Moving reactors, e.g. rotary drums
    • 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
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/008—Pyrolysis reactions
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/78—Preparation by contact processes characterised by the catalyst used
    • C01B17/79—Preparation by contact processes characterised by the catalyst used containing vanadium
    • 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
    • C01B3/10—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 metals
    • C01B3/105—Cyclic methods
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/02—Apparatus characterised by their chemically-resistant properties
    • B01J2219/025—Apparatus characterised by their chemically-resistant properties characterised by the construction materials of the reactor vessel proper
    • B01J2219/0277—Metal based
    • 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
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight

Definitions

  • Topic Gas / solid phase reaction of water with elemental iron and sulfur.
  • the invention relates to a thermal process with the aid of a pressure tube reactor for the continuous flow of some chemical
  • the essence of the invention is a solar thermal process based on concentrated solar energy with trough collectors, and the product is a pressure tube reactor for the continuous production of
  • the solar chemical process has six production steps, which can be divided into four main processes: water splitting, regeneration, roasting and rinsing.
  • Hydrogen like electric current, is not a primary energy source, but must first be artificial and with lower efficiencies and yields from others
  • JP 03205302 A describes the production of high-purity hydrogen using activated magnetite as a reactive catalyst. • [0006]
  • JP 2001270701 A produces hydrogen by reacting metallic zinc, magnetite and water with each other at 600 ° C.
  • M. Inoue et al. from Solar Energy (2003) describe the production of hydrogen using a water-Zn0-MnFe2S04 system.
  • the corresponding ferrite powder of the type M x 2+ Zni -x 2+ Fe2S04 can be produced by the method of S. Lorentzou et al., Presented at the Partec 2004 conference. Too complicated in my opinion.
  • the aim of the present invention is therefore a process engineering cycle process for the production of hydrogen gas, which in particular in one
  • Reaction pressure tube can be carried out, in which no solid has to be exchanged.
  • Mixing with mechanical methods may be advantageous, whereby the metals are kept porous.
  • the metals are elementary and are mixed through the cooling pipes on a ring line, after which they can be reacted again.
  • Another object is to provide a solar-powered pressure tube reactor with a parabolic mirror in a vertical design, in which above all
  • Hydrogen gas is continuously produced as a product.
  • Rinsing necessarily run in succession or in parallel in several modules simultaneously.
  • the metal oxide is regenerated with sulfur gas (S (2-) g ). Bound oxygen is released as sulfur dioxide and sulfur trioxide so that the metal is reduced.
  • the remaining metal pyrite is increased compared to the second process step
  • the hydrogen synthesis by water vapor gas splitting is mainly carried out in the process according to the invention in the DRR.
  • the regeneration of the metal redox system takes place in a second reaction space.
  • the invention consists of a method of thermally splitting water vapor in a multi-stage cycle process by using concentrated light irradiation or by waste heat and, as a result, to generate solar hydrogen gas (H2g).
  • the object of the invention has been shown to thermally split water vapor by means of concentrated sunlight and to bind oxygen in an auto-oxidation reaction and thereby generate hydrogen gas (H2g).
  • the hot steam flowing past the metal in a turbulent manner is split by binding the oxygen to the excited metal grid at temperatures of predominantly 500 ° C to 900 ° C.
  • Hydrogen gas (hteg) is released.
  • the oxygen previously incorporated into the metal lattice is released again to the double molecular sulfur gas (S (2-) g) or phosphorus gas (Pg) (substitution reaction); the metal oxide is partially regenerated or reduced back to the more energetic state.
  • the metal pyrite lattice is broken up by a roasting process at somewhat higher temperatures of approx. 1200 ° C to 1350 ° C, whereby sulfur dioxide and sulfur trioxide are produced again.
  • the reaction space is then flushed with nitrogen and the gases are separated off.
  • iron (II, III) and iron gas (H2) ⁇ are formed from iron and water vapor.
  • iron (III) oxide reacts to iron (II) oxide and oxygen (O2).
  • pyrite FeS2
  • FeS2 iron (II) oxide
  • sulfur gas S2-
  • SO2 ⁇ + vanadium (V) SO3 ⁇ should be approx.
  • the reactor is flushed completely with nitrogen and thereby for the rest
  • a significant innovation of the process is the combination of a metal bed made of at least two metals - firstly made of iron and secondly made of vanadium
  • Pressure tube reactor module or double jacket pressure reactor can be heated.
  • the iron and vanadium powder fill which is evenly distributed with metals, forms the mixture in a modular pressure tube reactor, which is fixed in a cylindrical basket.
  • a light concentrating solar system preferably a solar gutter collector in a vertical design
  • Porylysed ruckroh rreaktor brought to the required temperature by the concentrated sunlight. The reactions take place on the surface of the
  • the pressure tube reactor is preferably in a small pilot plant for checking and optimizing the
  • This pilot plant primarily comprises
  • Water vapor dosing system the data acquisition and control systems and measuring systems for pressure and temperature as well as for the product gas aftertreatment.
  • the analysis of the concentrations of hydrogen gas produced or of released sulfur dioxide gas and sulfur trioxide gas is carried out by a mass spectrometer. .
  • the process parameters can be carried out by adapting the energy heating output, the recurring, cyclical temperature and by several gas changes in one reaction chamber.
  • the steam gas is split at a temperature in the range of 500 ° C to 900 ° C and the metal oxide is regenerated at a temperature of 450 ° C to 650 ° C with sulfur gas (S2-) or phosphorus gas.
  • S2- sulfur gas
  • the metal pyrite is then roasted at a temperature of 900 ° C to 1350 ° C, producing elemental metal.
  • the required temperature in the reaction spaces of the modules is modified by periodically changing the heating output for the purpose of one
  • the differentiated thermal positioning of the reactors and / or concave mirrors firstly causes synchronous reactions of water splitting at a given temperature and secondly causes regeneration at a lower temperature.
  • the roasting process is carried out at higher temperatures than water splitting. The sequence of these different batch processes thus enables the continuous production of hydrogen.
  • the procedure is mainly according to the different
  • Energy demand quantities of the successive reactions involved are sequenced.
  • the periodic change in the temperatures of the metals is achieved by modifying the energy heating power. First the split takes place, then the regeneration and then the roasting and rinsing.
  • Temperature are generated by burning fossil fuels and / or using the waste heat energy from the exhaust gas flow from vehicles, because common methods use these energy sources.
  • the generation of the required temperature by means of light energy is also advantageous and essential because conventional energy generation systems by burning fossil energy is not resource-saving and light energy such as sunlight is available everywhere, even in space.
  • optical devices can be built as paraboloid concentrators
  • Solar tower systems parabolic trough collectors, elliptical or spherical mirrors, solar ovens, or line-focusing concentrators.
  • these optical structures can be used to generate hydrogen on a large industrial scale as a sustainable, secondary energy source without carbon dioxide emissions that are harmful to the climate.
  • the reaction modules are mainly rotated on a turret device in order to align them with the radiation source and thus to change the heating power. This can be used to change the temperature at the same
  • Radiant heating output can be achieved easily.
  • reaction paraboloid can be positioned by rotation so that the light from the radiation source is redirected to a desired module. This can also be used to change the temperature at the same
  • a third possibility for the methods listed in points 0028 and 0029 consists in the focus position of several mirrors arranged in fields or To change concave mirrors. A change in temperature can also be achieved in this way.
  • optical components are suitable for reducing and / or increasing the radiation of the solar energy.
  • Light transmission variable optical half mirrors diaphragms, deflecting mirrors or optical filters.
  • Heat transfer media are heated. With preheating, the fluids no longer require as much radiant heating power in the reactor room.
  • the hydrogen synthesis by water splitting can advantageously take place in one reactor and the regeneration of the metal oxide by sulfur and / or phosphorus gas reduction in a further reactor. These two steps are carried out simultaneously for the purpose of preparing the roasting in a further pressure tube reactor module.
  • the process is carried out in several successive production cycles in order to achieve continuous flow reproducibility. It is estimated that a production cycle takes 0.5 to 1.5 hours. With a dis-continuous flow process, this has above all economic advantages. With this method, the production cycles can also be significantly shorter or longer.
  • the temperature and the concentration of hydrogen can be changed - until the metal filling capacity is completely exhausted.
  • the aim of the invention is achieved as follows: With the aid of a reactor for the thermal production of hydrogen from water vapor on a surface in a gas-solid phase reaction with at least two connected pipes, the gas stream of educt gases into and out of a reaction space
  • Heat source at least two metals being provided as reactants in a reaction space.
  • the required temperature in the reaction rooms of the pressure tube reactors is changed by a periodic change in the heat output, which results in a continuous flow of production.
  • the modified thermal control of sunlight on the pressure tube reactors enables the simultaneous reaction sequence of water splitting at a certain temperature and
  • the first pressure tube reactor has a connected cooling pipe system, which enables a liquid flow (permeate) into the reaction space of the first pressure pipe reactor and a flow of water vapor from the cooling system, which feeds into a second pressure pipe reactor.
  • a heat source e.g. engine exhaust or turbine exhaust nozzle
  • the metal powders iron and vanadium each ⁇ 50pm are provided as reactants in a reaction chamber.
  • the metal powders are preferably of one in the double-jacket reactor
  • Feed water cooling is also required so that the operating conditions (i.e. the heating output) can be varied.
  • the sulfur regeneration is made possible with at least one connected pipe, which allows a gas flow of starting gas into a reaction vessel and product gases out of this vessel.
  • the following metals are particularly popular for the metal powder fillings in the pressure tube reactor rooms: iron, manganese and nickel. Vanadium is or are added to one or more of these substances.
  • the following metals can also be used: Ti, Li, Cr, Er, Hf, Ho, Lu, Mo, Nb, Os, Pd, Re, Rh, Ru, Sc, Si, Ta, Tc, Tb, Th, Tm, Ti, W, Y, Zr, Co.
  • These metals can also be used as individual substances or as mixtures, since these - both in pure form and as a mixture - can be used particularly efficiently in hydrogen splitting, the melting point temperature must be above 1400 ° C. The higher the valence of the metal ion, the more hydrogen per atom can be generated.
  • the reaction chamber is cylindrical (tube) and blackened from the outside with heat-resistant black lacquer.
  • the tube is covered with a transparent
  • reaction space there are components between the reaction space and the energy source that weaken and / or intensify the energy flow so that better control of the reactions is made possible.
  • the heat exchanger tubes primarily contain a fluid (permeate), since this enables the heat exchange to be individually tailored.
  • the water vapor is generated in one reactor and passed into another reactor, which is used to return the water vapor to the first reactor.
  • the reactor is equipped with two four-way valves (left and right of the module) to enable the gaseous starting materials to be fed in and the products to be discharged.
  • gaseous products can be discharged separately.
  • the reactor turret is ideally of modular construction - from at least two, better still three reaction pressure tube reactors, since this makes the continuous flow process described above particularly easy to handle.
  • the two reaction modules are used alternately
  • a concentrating solar thermal system is mainly used as the energy supplier - this includes the following variants: a paraboloid concentrator, a solar tower system, a sun oven, an elliptical or spherical mirror and a line-focusing concentrator.
  • a paraboloid concentrator a paraboloid concentrator
  • a solar tower system a sun oven
  • an elliptical or spherical mirror a line-focusing concentrator.
  • an engine exhaust or a turbine exhaust gas space can be used as an energy source, as explained above.
  • the required radiant light output is achieved using a group of heliostats.
  • the radiation power required for regeneration is made possible by another group of heliostats.
  • Hydrogen gas generation can be done using the pressurized gas reactor presented
  • Drawing No .: 01 shows the pressure tube reactor module system, whereby the water vapor is fed into the apparatus with a four-way valve from the left side.
  • the sunlight-focused radiation energy is transferred from the outside to the
  • Pressure tube reactor module blasted.
  • the energy heating power of the incident light can be adjusted by means of an aperture.
  • the pressure tube reactor is based on the already described connection of the metal-gas system with a metal powder filling inside, which consists of a finely divided, loose particle powder structure (10).
  • the metal powder filling is in a modular cell; it is filled with the metals and installed in a cylindrical tube housing (10).
  • the borosilica glass (evacuated) enables high temperatures to be generated in a directly absorbing vacuum with low reflection losses (9).
  • Point (02) steam pipe made of high-alloy steel
  • Point (03) four-way valve (heat-resistant, pressure-resistant)
  • Point (1 1) Feed water cooling system with ring line in the center of the chamber
  • Point (13) flow of cooling system line (permeate from reverse osmosis system)
  • Point (14) right flange connection to the pressure chamber or reaction chamber
  • the operation of the flow reactor is based on the simultaneous use of both modules. While water is split in one of the two reaction rooms, regeneration with sulfur gas takes place in the other reaction room. After the reactions have ended, the regenerated module is switched over to cleavage by changing the gas supply. Requirements for this continuous operation and the
  • Hydrogen production is the separate supply of nitrogen gas, which is called
  • Carrier gas or purge gas is used, as well as the same supply of water vapor.
  • another line is on the one hand for the products of the cleavage and on the other hand for the regeneration gas containing regeneration gas
  • Completion of a reaction step can be switched.
  • One of these valves has to withstand high temperatures up to 600 ° C.
  • the two steps of the process are carried out in the same reactor at different temperature levels with different heat requirements.
  • Regeneration is endothermic and takes place at 450 ° C.
  • the steam splitting is slightly exothermic and takes place at 900 ° C. This is why some of the modules are required
  • EP1019316B1 May 5, 1999 March 24, 2004 Shec Labs - Method for

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Materials Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Thermal Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Electromagnetism (AREA)
  • Toxicology (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un procédé thermique utilisant un réacteur à tube sous pression pour la réalisation continue en écoulement de quelques réactions chimiques sur la surface d'au moins un réactif solide dans une réaction entre un gaz et une phase solide. Le noyau de l'invention est un procédé thermo-solaire sur la base d'énergie solaire concentrée au moyen de collecteurs cylindro-paraboliques, et le produit est un réacteur à tube de force pour la génération continue d'hydrogène de synthèse (H2) à partir de vapeur d'eau (H2Og). L'absorption ou l'adsorption sur la surface de mélanges métalliques de métaux particulier entraîne les réactions suivantes : réaction de craquage, d'auto-oxydation, de substitution, de décomposition à des températures situées dans la plage de 500°C à 1350°C. Le procédé comprend quatre processus principaux : décomposition d'eau, régénération, grillage, rinçage ainsi qu'évacuation. Le problème : l'hydrogène doit être généré en premier de manière artificielle et avec de faibles rendements à partir d'autres sources d'énergie (énergie fossile, énergie nucléaire ou énergies renouvelables). Les concepts pour de futures économies d'hydrogène prévoient par contre la production d'hydrogène à partir d'énergies renouvelables. La solution : le réacteur à tube de force et l'ancien procédé régéneratif, mon invention. De cette façon, les coûts de la production d'hydrogène sont réduits et une production à grande échelle devient possible à long terme. Mon invention est la nouvelle génération des énergies renouvelables, sans émissions dangereuses. déroulement de la régénération schématique uniquement (pas d'équation de régénération) (I)
PCT/DE2018/000255 2018-09-05 2018-09-05 Réacteur à hydrogène et le procédé de chimie régéneratif WO2020048556A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/DE2018/000255 WO2020048556A1 (fr) 2018-09-05 2018-09-05 Réacteur à hydrogène et le procédé de chimie régéneratif
DE112018007957.0T DE112018007957A5 (de) 2018-09-05 2018-09-05 Wasserstoffreaktor und das regenerative Chemie-Verfahren

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022218969A1 (fr) * 2021-04-13 2022-10-20 Uestuen Orhan Procédé et dispositif de production d'hydrogène
CN115232904A (zh) * 2021-04-23 2022-10-25 中国石油大学(北京) 一种生产海绵铁的方法

Citations (12)

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US2664404A (en) * 1949-08-18 1953-12-29 Standard Oil Dev Co Regeneration of selective hydrogenation catalyst
US4054444A (en) * 1975-09-22 1977-10-18 Midrex Corporation Method for controlling the carbon content of directly reduced iron
DE2634662C2 (fr) 1975-08-04 1987-03-19 Ga Technologies Inc., San Diego, Calif., Us
DE2438264C2 (fr) 1973-11-05 1988-02-18 Sun Ventures Inc., St. Davids, Pa., Us
JPH03205302A (ja) 1989-12-29 1991-09-06 Alpha Kuresuto:Kk 水素生成方法
DE4226496A1 (de) 1992-08-11 1993-01-21 Gottfried Von Dipl Czarnowski Verfahren zur erzeugung von wasserstoff nach einem modifizierten eisen-wasserdampf-prozess
EP0675075A1 (fr) * 1994-03-29 1995-10-04 Daimler-Benz Aerospace Aktiengesellschaft Méthode pour la génération d'hydrogène
JP2001270701A (ja) 2000-03-28 2001-10-02 Yutaka Tamaura 水の分解方法
US20030072705A1 (en) * 2001-03-06 2003-04-17 Kindig James Kelly Method for the production of hydrogen and applications thereof
WO2003093205A2 (fr) * 2002-05-02 2003-11-13 Uhde Gmbh Procede de preparation d'hydrocarbures halogenes insatures et dispositif utilise a cet effet
EP1019316B1 (fr) 1998-05-05 2004-03-24 Shec Labs - Solar Hydrogen Energy Corporation Production d'hydrogene par decomposition thermique de l'eau
CN102563931B (zh) * 2012-02-28 2013-08-21 常州大学 具有补偿密封结构的槽式聚光太阳能集热管及其装配工艺

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