WO2016107868A1 - Réacteur thermique - Google Patents

Réacteur thermique Download PDF

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Publication number
WO2016107868A1
WO2016107868A1 PCT/EP2015/081344 EP2015081344W WO2016107868A1 WO 2016107868 A1 WO2016107868 A1 WO 2016107868A1 EP 2015081344 W EP2015081344 W EP 2015081344W WO 2016107868 A1 WO2016107868 A1 WO 2016107868A1
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WIPO (PCT)
Prior art keywords
chamber
reaction
reaction chamber
reaction product
hydrogen
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Ceased
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PCT/EP2015/081344
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English (en)
Inventor
Gunnar Sanner
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Individual
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Publication of WO2016107868A1 publication Critical patent/WO2016107868A1/fr
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    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/04—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of inorganic compounds
    • C01B3/042—Decomposition of water
    • 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
    • B01J19/0053—Details of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1812—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
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1893—Membrane reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/002—Component parts of these vessels not mentioned in B01J3/004, B01J3/006, B01J3/02 - B01J3/08; Measures taken in conjunction with the process to be carried out, e.g. safety measures
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0251—Physical processing only by making use of membranes
    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/04—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of inorganic compounds
    • C01B3/042—Decomposition of water
    • C01B3/045—Decomposition of water in gaseous phase
    • 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; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/501—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification by diffusion
    • 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; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/508—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification by using hydrogen storage media
    • 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
    • B01J2219/00139—Controlling the temperature using electromagnetic heating
    • B01J2219/00144—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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00155—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • 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 present invention relates to a thermal reactor for performing water splitting or reacting water, nitrogen or C0 2 to hydrogen, ammonia or hydrocarbons, and to a method for preforming the reactions with limited temperature and pressure changes within the reaction chamber.
  • Prior art US2013/0266502 discloses a number of reaction designs for production of hydrogen and oxygen by gas-phase reduction/oxidation reactions at isothermal conditions.
  • the energy may be supplied as concentrates solar energy.
  • the reactions are performed by providing two reactors run in opposite modes generation and regeneration and alternating which of the processes is performed in the reactors.
  • US4332775 discloses a rotary tubular reactor for dissociation of water.
  • US2009/0232716 discloses a reactor for the production of hydrogen using selective membranes.
  • GB1532403 also discloses a device for hydrogen generation
  • US4,873,061 discloses a solar reactor for nitrogen fixation.
  • the objective of the present invention is to provide equipment and a method for thermally splitting water or react water and nitrogen to ammonia or react water and C0 2 to syngas, or hydrocarbons such as alkanes or alcohols, wherein the equipment allows for relative constant temperature and pressures within the reaction chamber.
  • a further objective is to provide equipment that allows for continuously operation.
  • This invention is based on the principles of "reversed combustion”. This is a process to convert e.g.: combinations of Biomass (or natural gas (NG), coal, oil), H 2 0, C0 2 , N 2 , H 2 and air to gaseous or liquid hydrocarbons or other fuels like H 2 and NH 3 .
  • the process is driven by Renewable energy (RE) or Nuclear Energy (NE) fed to the process directly or indirectly, e.g. : through heat from CSP/Nuclear plant, through heat from a medium that has absorbed heat from RE/NE (e.g.: molten salt), or electrical heater driven by RE/NE power.
  • RE Renewable energy
  • NE Nuclear Energy
  • the main principle behind the invention is that reactants are fed into a chamber, the reversed combustion takes place in the chamber under high pressure and high temperature, and the products are taken out of the chamber by sorption (adsorption or absorption) by elements put into and taken out of the chamber without changing the pressure and temperature in the chamber significantly, by filter or by tapping out liquids (if possible).
  • a thermal driven reactor comprising a reaction chamber tolerating to be heated above 500°C and tolerating an internal pressure of above 50 atm, wherein the reaction chamber comprises walls and at least part of said walls are configured to transfer heat energy into the reaction chamber, a reactant inlet in fluid communication with the reaction chamber and at least one sorber element movable between a position within the reaction chamber and a position in a desorption chamber in communication with the reaction chamber, and the communication with the reaction chamber is closable so that the desorption chamber can be depressurized without influencing the pressure in the reaction chamber, and at least one reaction product conduit in fluid communication with the desorption chamber via a closable reaction product outlet.
  • Applicable sorber materials for the sorber element are any absorber material with an ability to selectively absorb oxygen, or hydrogen or ammonia or C0 2 or alkanes or alcohols or other hydrocarbons at the reactor conditions and any adsorber materials with an ability to selectively adsorb oxygen or hydrogen or ammonia or C0 2 or alkanes or alcohols or other hydrocarbons at the reactor conditions.
  • absorber materials include but are not limited to materials disclosed in
  • the reactions chamber tolerates an internal pressure of 700 atm. In a further aspect the reactions chamber tolerates an internal temperature of 2000-3000°C.
  • the at least one sorber element sorbs oxygen at high pressure and releases sorbed oxygen at low pressure in the desorption chamber.
  • the reactor comprises at least two sorber elements adapted to sorb to different reaction products and release these to two separate reaction product conduits.
  • the thermal driven reactor further comprises a hydrogen filter arranged within the reaction chamber and comprising a hydrogen outlet arranged outside the reaction chamber, wherein the hydrogen outlet is in fluid communication with a hydrogen conduit.
  • the reactant is water and optionally nitrogen or air and the reaction products are oxygen and hydrogen or ammonia.
  • the reactant is water and C0 2 and the reaction products are oxygen and syngas (hydrogen + CO) or alkane or alcohol.
  • the reactor may in a further aspect comprise an outlet for a liquid reaction product where the outlet is in fluid communication with the reaction chamber through a valve element allowing for controlled removal of liquid reaction formed within the reaction chamber.
  • the present invention further provides a method of performing a thermal reaction, wherein the method comprises providing a thermal driven reactor according to the present invention, supplying heat to at least part of the walls of the reaction chamber, thereby heating the chamber to above 500°C,
  • the thermal driven reactor comprises a second sorber element for sorbing a second reaction product, the method comprises transferring said second sorber element to a second desorption chamber, desorbing the second reaction product from said second sorber element and supplying the second reaction product to a second reaction product conduit.
  • the reactant is water and optionally nitrogen or air or C0 2 .
  • the first reaction product is oxygen
  • the second reaction product is hydrogen or ammonia or syngas or alkane or alcohol.
  • the pressure within the reaction chamber is kept above 50 atm during the method and the pressure with in the one or more desorption chambers are below 50 atm during the desorption steps.
  • filter refers to a structure which selectively allows for the penetration of one of these gasses there through. Accordingly the filter functions as a selective membrane where hydrogen, oxygen, ammonia CO, syngas, alkanes or alcohols passes though the filter and is transported out of the reaction chamber.
  • the filter is made of a material that can sustain the high temperature within the reaction chamber, the filter may for instances be a ceramic membrane.
  • the filter can have any suitable shape; preferably the shape is adapted to provide the membrane surface with as large a filter surface as possible.
  • Figure 1 schematically illustrates a cross sectional view of a first embodiment of a thermal driven hydrogen/ammonia reactor.
  • Figure 2 illustrates a cross sectional view along the line A-A of the first
  • Figure 3 schematically illustrates a second embodiment of the thermal driven hydrogen/ammonia reactor.
  • Figure 4 schematically illustrates a cross sectional view of a third embodiment of the thermal driven hydrogen/ ammonia reactor.
  • Figure 5 schematically illustrates a cross sectional view along the line B-B of the third embodiment of a thermal driven hydrogen/ammonia reactor, but with an alternative internal configuration.
  • the solution sorts the reaction products at this high temperature through absorption optionally combined with selective filter mechanisms.
  • Applicable combinations of temperature and pressure condition in the reaction chamber are above 500°C and above 50 atm, or a temperature between 500-3000°C and a pressure between 50-1000 atm, or a temperature between 1000-2500°C and a pressure above 100 atm, or a temperature between 1500-2000°C and a pressure above 300 atm.
  • the main part of the solution is a reaction chamber 5 that is capable of receiving heat 30 from e.g. nuclear reactions or solar fields.
  • the heat input can take place through the outer walls 3 when cooling media from nuclear reaction heat transfer towards the reaction chambers outer wall 3, or concentrated solar beams are mirrored towards the reaction chambers outer wall 3.
  • the reaction chamber 5 is the central receiver up in the tower of a concentrated solar thermal park.
  • heat can be lead more directly into the reaction chamber so the cooling media from nuclear reaction heat transfer more directly with the chemical substances taking part in the reaction in the reaction chamber, or solar beams are led into the chamber via transparent walls 3 or part of the walls 3.
  • the thermal splitter comprises at least two but preferably at least four selective absorber elements 13, 13 ' . These absorber elements are adapted to when arranged within the reaction chamber 5 to selectively absorbed one of the reaction products. In the case of water splitting at least one absorber element selectively absorbs oxygen and at least one absorber element selectively absorbs hydrogen.
  • the absorber element 13 is arranged in the reaction chamber 5 and the free end thereof comprises a closing element 15 which is not in contact with the opening 6 between the reaction chamber 5 and the desorption chamber 17.
  • the opening between the desorption chamber 17 and the pipe 12 is blocked by blocking element 19.
  • the blocking element can be removed and reintroduced reversibly to so that when the closing element 15, 15 ' seals the opening 6 the blocking element is removed, and when the desorption is completed the blocking element 19 is reintroduced before the absorber element 13 reenters the reaction chamber.
  • the positioning elements 20, 20' can be moved from the retracted to the extended position and back again by different mechanisms, such as hydraulic or magnetic lifting methods well known in the art.
  • the surface 1 1 of the absorber element 13 may contain catalytic active compounds improving the efficiency of the reaction and/or a membrane improving the selectivity of the absorption.
  • the other illustrated absorber element 13 ' is arranged inside the desorption chamber 17' .
  • the closing element 15 ' arranged at the free end of the absorber element is in sealing contact with the opening between the reaction chamber 5 and the desorption chamber 17'.
  • the desorption chamber 17' is in fluid communication with the product pipe 12' .
  • the positioning elements 20, 20' allows for the absorber elements to be freely moved between the two positions illustrated and thereby between the two chambers. When arranged in the reaction chamber the absorber element 17 absorbs selectively one of the gases generated by the reaction.
  • the thermal driven hydrogen/ammonia reactor preferably contains several absorber elements for selectively absorbing each of the gas products produced by the reaction, thereby at least one absorber element for each gas product can be active within the reaction chamber while at least one absorber element for each gas product is arranged in its respective desorption chamber for release of the produced gas element and regeneration of is absorption capabilities.
  • the pressure within the desorption chamber during the desorption process is in one embodiment below the pressure in the reaction chamber.
  • the pressure is at least 1 atm below the pressure in the reaction chamber.
  • the pressure in the desorption pressure is between 1 atm and 20 atm.
  • the absorbers can be regenerated at higher or lower temperature and/or at lower pressure than within the reaction chamber, optionally combined with the use of inert gases to ventilate out the produced gas.
  • the inert gas is separated from the produced gas in a down stream separation process.
  • Water and optionally nitrogen or air is pumped into the reaction chamber 5 by a pump located upstream of the supply pipe 2.
  • Water is preferably in its liquid phase, so that the pumping is energy efficient.
  • the pump is preferably water cooled with water being pumped into the reactor, this limits energy leakage.
  • the pump will, while in operation, keep constant pressure.
  • a pressure sensor giving signal to and monitoring of the pump can be included in a control and management system.
  • the pump can be two-ways, so that if the pressure is increase above limits, it will pump water out.
  • reaction chamber When water reaches the reactor chamber it will vaporize due to the heat.
  • the reaction chamber comprises both at least one hydrogen absorber element and at least one oxygen absorber element, the absorption of the elements on the right side of the equation will drive the reaction to the right.
  • the shape of the reaction chamber and the absorber elements can be freely selected and can be cylindrical or other spherical shapes.
  • Figure 2 illustrates a cross sectional view a long the line A-A in figure 1 of thermal splitter according to the present invention.
  • twelve absorber elements 13 are visible.
  • all absorber elements are adapted to selectively absorb one of the two reaction products from the reaction.
  • the other reaction product has to be removed directly from the reaction chamber 5, by providing an outlet and a conduit from the outlet to a separation unit wherein the reaction product is separated from unreacted supplied gas (water and optionally nitrogen or air).
  • Figure 3 illustrates a cross sectional view through a thermal reactor according to an embodiment of the present invention wherein two types of absorber elements 1 13 and 1 14 are distributed with in the reaction chamber 5. Each type of absorber element respectively selectively absorbs one of the reaction products. Each of the absorber elements is regenerated and the separated reaction product released as described in connection with figure 1.
  • the absorber elements 1 13 and 1 14 are respectively hydrogen and oxygen absorbers.
  • the number of absorbers used for hydrogen and oxygen will be decided based on their ability to absorb the product gases.
  • Nitrogen gas is fed into the reactor chamber in addition to water, the reactor will produce ammonia and oxygen. Ammonia and oxygen can then be extracted from the reactor chamber by use of described absorber principles. The nitrogen needed as input will be extracted from the air by use of an air separation unit. Alternatively to pure nitrogen, air can be fed into the reactor chamber in addition to water, since air consists of 78.084 mole % nitrogen.
  • Air consist of 78.084 % nitrogen
  • the oxygen (20.947 mole %) that is part of the air, will be extracted from the reactor chamber together with oxygen produced in the reaction. Small volumes of other gases in air ( ⁇ 1 mole %) can be ventilated out of the reaction chamber after a period of running.
  • Figure 4 illustrates an alternative embodiment of a thermal driven
  • the embodiment on figure 4 comprises a selective filter element 216 through which a first of the two reaction products are removed from the reaction chamber.
  • the absorber elements 213 and 213 ' are designed to selectively absorb the second reaction product, and reversibly release the second reaction product in the desorption chamber 17' .
  • the filter 216 within the reaction chamber is in one embodiment thereof a hydrogen filter chamber with walls capable of filtering out H 2 molecules and persist the high pressure in the reaction chamber.
  • the pressure inside the hydrogen filter will be kept low at all time of operation, e.g. in the range from 0.1 to 1 atm.
  • the hydrogen filter in one embodiment has a construction and shape that maximizes the surface area for filtering purposes.
  • the reaction chamber there is one, or preferably several, oxygen absorbers 213 capable of absorbing large amount of oxygen gas under high pressure.
  • the absorbers When the absorbers are retracted into the desorption chambers the pressure is released, and the oxygen is freed from the oxygen absorber.
  • the hydrogen streams out automatically at above 1 atm., or is pumped out at down to 0.1 atm. (to increase speed of the water splitting).
  • the hydrogen is continuous evacuated so the pressure inside the hydrogen filter is kept on the same low level at all time.
  • the change of oxygen absorbers takes place when the valves or blocking plate for oxygen export are closed in the bottom of the filled desorption chambers, another valves for high pressure vapor is opened, so those desorption chambers containing absorber elements to be return into the reaction chamber get the same pressure as the reaction chamber. At that point doors between the desorption chamber and the reaction chamber can be opened and the new oxygen absorbers can be lifted up. On the other hand, filled oxygen absorbers are lowered down in the empty desorption chambers. Doors are closed between these chambers and the reaction chamber and oxygen export valves/blocking plates are opened so mainly oxygen can stream out as the pressure is lowered and/or temperature is changed and/or inert gas is added.
  • the replacement process of oxygen absorbers can either happen by changing half of the absorbers in one round or sequentially one and one to get a smoother operation.
  • the main principals of the present invention may be employed in the production of alkanes, alcohols and other liquid hydro carbons.
  • the total reaction schemes for alkanes is

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un réacteur à entraînement thermique, comprenant une chambre de réaction, qui tolère un chauffage à une température supérieure à 500°C et une pression interne supérieure à 50 atm, la chambre de réaction comprenant des parois et au moins une partie desdites parois étant conçue pour transférer de l'énergie thermique dans la chambre de réaction ; une entrée de réactif en communication fluidique avec la chambre de réaction ; et au moins un élément de sorption mobile entre une position dans la chambre de réaction et une position dans une chambre de désorption en communication avec la chambre de réaction, la communication fluidique avec la chambre de réaction pouvant être fermée de telle sorte que la chambre de désorption peut être dépressurisée sans influencer la pression dans la chambre de réaction ; et au moins un conduit de produit de réaction en communication fluidique avec la chambre de désorption via une sortie de produit de réaction pouvant être fermée ; et un procédé pour effectuer une réaction thermique.
PCT/EP2015/081344 2014-12-30 2015-12-29 Réacteur thermique Ceased WO2016107868A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO20141568 2014-12-30
NO20141568 2014-12-30

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WO2016107868A1 true WO2016107868A1 (fr) 2016-07-07

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GB1532403A (en) 1976-10-04 1978-11-15 Comp Generale Electricite Hydrogen generating device
US4266957A (en) 1979-06-07 1981-05-12 Petrocarbon Development Limited Recovery of hydrogen and ammonia from purge gas
US4332775A (en) 1980-07-03 1982-06-01 Battelle Memorial Institute Hydrogen generator utilizing solar energy to dissociate water
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EP0846745A1 (fr) 1992-09-04 1998-06-10 BP Chemicals Limited Agent de retention d'hydrogène
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WO2012069635A2 (fr) 2010-11-26 2012-05-31 Statoil Asa Système énergétique du type cycle de sanner
US20120276254A1 (en) 2006-06-30 2012-11-01 Global Fresh Foods System and methods for transporting or storing oxidatively-degradable foodstuff
US20120321549A1 (en) 2010-03-29 2012-12-20 Yoshimi Okada Method for producing hydrogen aimed at storage and transportation
US20130266502A1 (en) 2012-04-05 2013-10-10 The Regents of the University of Colorado, a body corporate Methods and apparatus for gas-phase reduction/oxidation processes
CN103864104A (zh) 2012-12-18 2014-06-18 英威达科技公司 在Andrussow 工艺中稳定热交换管的方法
US20140275298A1 (en) * 2013-03-12 2014-09-18 Powerdyne, Inc. Systems and methods for producing fuel from parallel processed syngas

Patent Citations (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4119488A (en) * 1975-04-10 1978-10-10 S.A.E.S. Getters S.P.A. Nuclear reactor fuel element employing Zr2 Ni as a getter metal
GB1532403A (en) 1976-10-04 1978-11-15 Comp Generale Electricite Hydrogen generating device
US4266957A (en) 1979-06-07 1981-05-12 Petrocarbon Development Limited Recovery of hydrogen and ammonia from purge gas
US4332775A (en) 1980-07-03 1982-06-01 Battelle Memorial Institute Hydrogen generator utilizing solar energy to dissociate water
US4521398A (en) 1983-07-18 1985-06-04 Air Products And Chemicals, Inc. Controlled temperature expansion in oxygen production by molten alkali metal salts
US4873061A (en) 1988-01-13 1989-10-10 Hare Louis R O Fixation of nitrogen by solar energy
EP0846745A1 (fr) 1992-09-04 1998-06-10 BP Chemicals Limited Agent de retention d'hydrogène
US5711926A (en) 1996-05-14 1998-01-27 Knaebel; Kent S. Pressure swing adsorption system for ammonia synthesis
US6660066B2 (en) 2002-03-16 2003-12-09 Haldor Topsoe A/S Ammonia recovery from purge gas
US7431151B2 (en) 2004-09-14 2008-10-07 Honda Motor Co., Ltd. Hydrogen storage tank
US20090232716A1 (en) 2006-06-15 2009-09-17 Klaus Rohrich Reactor with a thermal gradient controlled for the production of pure hydrogen
EP2038210B1 (fr) * 2006-06-15 2011-09-07 H2 Power Systems Limited Un reacteur avec gradient thermique controle pour la production d'hydrogene pur
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