WO2011055343A2 - Reactor catalítico de membrana com bombagem electroquímica de hidrogénio ou de oxigénio e suas aplicações - Google Patents
Reactor catalítico de membrana com bombagem electroquímica de hidrogénio ou de oxigénio e suas aplicações Download PDFInfo
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- WO2011055343A2 WO2011055343A2 PCT/IB2010/055045 IB2010055045W WO2011055343A2 WO 2011055343 A2 WO2011055343 A2 WO 2011055343A2 IB 2010055045 W IB2010055045 W IB 2010055045W WO 2011055343 A2 WO2011055343 A2 WO 2011055343A2
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- anode
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- oxygen
- hydrogen
- catalytic reactor
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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
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2475—Membrane reactors
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/02—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of hydrogen atoms by amino groups
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/86—Inert electrodes with catalytic activity, e.g. for fuel cells
- H01M4/90—Selection of catalytic material
- H01M4/9016—Oxides, hydroxides or oxygenated metallic salts
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/86—Inert electrodes with catalytic activity, e.g. for fuel cells
- H01M4/90—Selection of catalytic material
- H01M4/92—Metals of platinum group
- H01M4/921—Alloys or mixtures with metallic elements
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/86—Inert electrodes with catalytic activity, e.g. for fuel cells
- H01M4/94—Non-porous diffusion electrodes, e.g. palladium membranes, ion exchange membranes
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
- H01M8/0681—Reactant purification by the use of electrochemical cells
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/08—Fuel cells with aqueous electrolytes
- H01M8/086—Phosphoric acid fuel cells [PAFC]
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
- H01M2008/1293—Fuel cells with solid oxide electrolytes
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M2250/00—Fuel cells for particular applications; Specific features of fuel cell system
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/002—Shape, form of a fuel cell
- H01M8/004—Cylindrical, tubular or wound
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/1016—Fuel cells with solid electrolytes characterised by the electrolyte material
- H01M8/1018—Polymeric electrolyte materials
- H01M8/102—Polymeric electrolyte materials characterised by the chemical structure of the main chain of the ion-conducting polymer
- H01M8/103—Polymeric electrolyte materials characterised by the chemical structure of the main chain of the ion-conducting polymer having nitrogen, e.g. sulfonated polybenzimidazoles [S-PBI], polybenzimidazoles with phosphoric acid, sulfonated polyamides [S-PA] or sulfonated polyphosphazenes [S-PPh]
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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
- 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
- Y02E60/50—Fuel cells
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
Definitions
- the present invention discloses an electrochemical hydrogen or oxygen pumped membrane catalytic reactor for the purpose of increasing conversion and / or selectivity in hydrogenation, dehydrogenation, deoxidation and oxidation reactions, either in liquid or gas phase.
- the present invention further describes the use of a hydrogen or oxygen electrochemically pumped membrane catalytic reactor for the direct amination of hydrocarbons, in particular for the conversion of benzene to aniline, by reaction with the ammonia.
- the present invention proposes a novel membrane catalytic reactor that increases the yield of direct hydrocarbon amination reactions by electrochemical pumping of oxygen and / or hydrogen.
- a preferred embodiment of the present invention is a description of a membrane catalytic reactor with means for performing electrochemical hydrogen pumping and at least one composite membrane which comprises: two electrodes, anode (3) and cathode (1), between which is the electrolyte (2);
- the anode (3) and the cathode (1) being electrically conductive; said electrolyte (2) being non-electrically conductive and forming a cationic hydrogen selective layer, i.e. protons;
- a suitable catalyst (4) is deposited on anode (3), preferably non-particulate.
- Said composite membrane further comprises:
- electrocatalyst suitable for hydrogen oxidation so that the protons formed can pass through the electrolyte and an electrolyser suitable for receiving the protons and reducing or promoting their reaction with oxygen; said electrocatalysts are preferably at the anode (3) / electrolyte (2) and cathode (1) / electrolyte (2) interface;
- the anode side electrocatalyst should preferably be deposited as nanoparticles decorating the chemical catalyst, i.e. deposited on the surface of the chemical catalyst (4).
- hydrogen permeated through the composite membrane may be oxidized to water on the cathode electrode (1) by the addition of at least one gas injector (or feeder) next to the permeate (ie cathode (1)). ), the gas being introduced contains oxygen.
- This oxidation catalyzed by an oxidation catalyst or electrocatalyst deposited at the cathode, preferably at the interface with the electrolyte, such as nanoparticulate platinum, allows the generation of an electric current which may contribute or be sufficient. for the electrochemical pumping of hydrogen by partially or totally avoiding the imposition of a potential difference necessary for the electrochemical pumping of hydrogen.
- the electrochemical hydrogen-pumped catalytic reactor may further incorporate at least one power supply which applies an electrical potential difference between the two electrodes; this potential difference may preferably be 0.5 V.
- anode (3) may be palladium or a palladium and silver alloy and may form a porous or dense hydrogen permeable film. If it is a dense film, the chemical catalyst should be applied to the anode and the electrocatalyst should be applied to the anode (3) and electrolyte (2) interface.
- the electrode opposite the reaction medium, cathode (1) may be palladium, porous palladium or another hydrogen permeable electrical conductive material.
- said composite membrane known as MEA (membrane electrode assembly) is supported on a ceramic or metallic membrane.
- the operating temperatures of the hydrogen pumped membrane catalytic reactors described above may be as high as 600 ° C, preferably 200 ° C to 500 ° C if the electrolyte (2) comprises yttrium doped zirconium phosphate.
- the electrolyte (2) may be a phosphoric acid doped polybenzimidazole (PBI) membrane with the operating temperature in this case being from 120 ° C to 200 ° C.
- PBI polybenzimidazole
- Another object of the present invention is a description of a membrane catalytic reactor with means for electrochemical pumping of oxygen and at least one composite membrane wherein said membrane comprises:
- the anode (3) and cathode (1) being electrical conductors; said electrolyte (2) being non-conductive and anionic oxygen permeable, i.e. it forms an anionic oxygen selective layer;
- Said composite membrane further comprises:
- this catalyst should be the same catalyst used to conduct the chemical reaction.
- this catalyst should be the same catalyst used to conduct the chemical reaction.
- the electrochemical oxygen-pumped membrane catalytic reactor further comprises a power supply which applies an electrical potential difference between the two electrodes, preferably (0.25 - 1.5) V with even more. preferably 0.5 V, to control the oxygen supply in the reactor.
- the electrolyte (2) may be yttrium doped zirconia (YSZ).
- said composite membrane is formed of three layers, in which:
- porous anode (3) may be an yttria stabilized nickel and zirconia cermet
- electrolyte (2) may be YSZ
- cathode (1) may be lanthanum strontium manganite.
- said composite membrane may be a typical solid oxide fuel cell (SOFC) membrane.
- At operating temperatures of the oxygen-pumped membrane catalytic reactors described above range from 500 ° C to 1000 ° C, preferably from 600 ° C to 1000 ° C.
- gas introduced into the oxygen pumped membrane reactor is air.
- the reactors described above may be used for the direct amination of hydrocarbons, such as benzene amination for aniline production.
- the electrochemical pumped catalytic oxygen or hydrogen reactors described above may incorporate a bundle of tubular composite membranes. These membranes may contain on their surface or anode impregnated the amination reaction catalyst in the form of nanoparticles.
- the membrane should have a convenient structure, as described above, to allow electrochemical pumping of hydrogen formed outside the reaction medium and / or permeation to the surface of the oxygen catalyst to conduct a hydrogen oxidation reaction and / or reoxygenating the catalyst. It is a further object of the present invention to describe a method of direct amination of hydrocarbons, preferably benzene for the production of aniline, by reaction with the ammonia in one of the above described membrane catalytic reactors comprising the following steps:
- hydrocarbon and ammonia streams are introduced in stoichiometric amounts.
- ammonia stream comprises amounts above the stoichiometric amount.
- electrochemical hydrogen or oxygen pumping is described in the open literature in systems related to energy production, ie fuel cells.
- electrochemical pumping exists in so-called polymeric membrane electrolyte or PEMFC fuel cells, where the oxidation reaction at the cathode forces the permeation of the hydrogen in proton form from anode to cathode.
- solid oxide or SOFC fuel cells the electrochemical reaction forces the ionic oxygen to pass from the cathode to the anode.
- Electrochemical pumping of hydrogen or oxygen allows these reagents to be removed or placed on the surface of the chemical catalyst respectively. Removal of hydrogen from the surface of the chemical catalyst as it results from direct amination allows the reaction equilibrium to shift towards the products. In the case of direct amination of benzene this pumping increases the conversion of benzene by over 40%.
- Dehydrogenation is a very important class of reactions that can take advantage of this new technology.
- Direct oxygen feed to the catalyst surface not only increases the reaction conversion by reacting with the formed hydrogen, but also increases the selectivity of the reaction.
- Aniline is currently typically synthesized from benzene in a two-step reaction process: reaction of benzene with nitric acid for nitrobenzene production and reaction of hydrogen with hydrogen for aniline production.
- Aniline may further be synthesized from phenol or chlorobenzene.
- FIG. 1 Schematic representation of a composite membrane of an electrochemical hydrogen pumped catalytic reactor in which:
- (1) - represents the electrode - cathode
- (3) - represents the electrode in contact with the reaction medium - anode
- (1) - represents the electrode - cathode
- (3) - represents the electrode in contact with the reaction medium - anode
- the present invention describes the use of electrochemical pumping of hydrogen or oxygen in a membrane catalytic reactor for the purpose of increasing the conversion of the chemical reaction to occur in the reactor and / or the selectivity of a direct hydrocarbon amination reaction.
- At the base of the present invention is the pumping of hydrogen or oxygen to or from the catalyst surface, where the chemical reaction to be manipulated to increase its conversion and selectivity occurs.
- Increased selectivity is achieved here by the fact that hydrogen is removed directly from the catalyst surface where the reaction occurs. This removal can be achieved by electrochemical pumping of hydrogen from the catalyst surface or by electrochemical pumping of oxygen to the catalyst surface where it reacts with hydrogen to form water. It may therefore be necessary to modify the chemical catalyst, for example by decorating it with an appropriate electrochemical catalyst.
- the electrocatalyst may be platinum and in the case of electrochemical pumping of oxygen may be nickel, which serves both as a chemical and electrochemical catalyst.
- the membrane catalytic reactor with electrochemical pumping of hydrogen or oxygen uses a composite membrane with essentially three layers, the inside being an appropriate electrolyte (2) and the outer two the electrodes. At the electrodes, or at the interface between the electrode and electrolyte, chemical and / or electrochemical catalysts shall be deposited. The location of the electrocatalyst depends on whether the electrodes allow the ionic bridge between the electrocatalyst surface and the electrolyte or not.
- the outer layers or electrodes shall be electrically conductive and may be palladium or a palladium and silver alloy.
- the cathode, ie the outer layer may consist of a porous metal membrane.
- Electrolyte (2) should be protonic conductor and should be selected essentially according to the reactor operating temperature and could be polymeric, for example from a perfluorinated polymer such as Nafion - temperatures up to 90 ° C, or acid doped polybenzimidazole phosphorus - temperatures between 120 ° C and 200 ° C, or may be ceramic, yttrium doped zirconium phosphate - between 200 ° C and 600 ° C.
- the reactor membrane may further be supported on a suitable support such as sintered steel.
- Imposing the potential difference between the electrical conductive layers will cause hydrogen to permeate into or out of the reactor.
- This oxygen-containing gas may be used to conduct a redox reaction, itself giving rise to the potential difference required for hydrogen permeation.
- the permeation of hydrogen by electrochemical pumping may be accomplished by oxidation of hydrogen outside the reactor.
- This redox reaction which can be catalyzed by platinum nanoparticles deposited at the interface between electrolyte (2) and cathode (1), yields a potential difference of up to 1 V. It is this potential difference that will force hydrogen permeation. , in a process all similar to what happens in a proton exchange membrane fuel cell (PEMFC).
- PEMFC proton exchange membrane fuel cell
- Oxygen permeation into the reactor by electrochemical pumping may also be achieved by a redox reaction with hydrogen within the reactor. In these cases, external imposition of a potential difference is optional or minimized.
- Electrocatalysts should be deposited on the electrolyte to allow the ions formed, either protons or oxygen ions, to migrate to or from the electrolyte. They may also be impregnated into the electrodes if they allow the ionic bridge of protons or oxygen anions to or from the electrolyte. On the other hand, the electrocatalysts should be deposited near the chemical catalyst such that they will remove the formed hydrogen or deliver the permeated oxygen. In a preferred arrangement, the nanoparticulate electrocatalyst should be deposited decorating the chemical catalyst. Electrical conduction should be provided by the electrodes. The electrodes shall allow free access of reagents to the chemical catalyst at the anode and cathode.
- the chemical reaction catalyst may be decorated with palladium. This metal will facilitate transport from the catalyst surface to the hydrogen membrane surface.
- Electrochemical pumping of oxygen occurs at temperatures between 500 ° C and 1000 ° C.
- the reactor membrane should be formed of three layers: the porous anode (3) consisting of an electrically conductive yttrium stabilized nickel and zirconia cermet (YSZ); electrolyte (2), which forms a dense, selective, nonconductive oxygen-selective layer, usually YSZ; and cathode (1), for example strontium lanthanum manganite (LSM), electrical conductor.
- YSZ electrically conductive yttrium stabilized nickel and zirconia cermet
- electrolyte (2) which forms a dense, selective, nonconductive oxygen-selective layer, usually YSZ
- cathode (1) for example strontium lanthanum manganite (LSM), electrical conductor.
- Oxygen when added to the reaction medium where hydrogen is formed, eg in the case of direct amination of benzene, reacts with hydrogen giving a potential difference as to which fuel cell.
- the external imposition of a potential difference is optional or minimized.
- Oxygen feeding is controllable by applying an electric potential and is made directly to the catalyst chemical of amination, where hydrogen is formed locally.
- This membrane is similar to those used in solid oxide fuel cells (SOFC). It consists of three layers: the porous anode (3) comprising for example an electrically conductive yttrium-stabilized nickel and zirconia cermet (YSZ); electrolyte (2), which forms an electrically nonconductive, anionic oxygen-selective dense layer, usually YSZ; and cathode (1), comprising for example lanthanum strontium manganite (LSM), electrical conductor.
- SOFC solid oxide fuel cells
- Nickel-based catalysts appear to be the most active. The use of nickel thus has two advantages, it is used in anode 3 as a catalyst for the amination reaction and as a necessary element for this layer.
- a palladium and / or platinum decorated nickel catalyst may also be used to allow the adsorption of hydrogen formed during amination and its subsequent catalytic oxidation with permeated oxygen.
- electrochemical pumping of oxygen is essential in order to remove all hydrogen formed in the reaction medium and thereby increase conversion and selectivity of the amination reaction.
- it further permits continuous regeneration of structural oxygen from the nickel catalyst by oxygen permeation directly to the catalyst. This process prevents the formation of by-products resulting from the direct addition of oxygen to the feed stream.
- This reactor should operate at a temperature between 500 ° C and 1000 ° C, the temperature range in which the electrolyte (2) is capable of ionic conduction.
- a membrane catalytic reactor having means for electrochemical pumping of oxygen which means comprising a composite catalytic membrane, the catalyst for direct amination of nickel and platinum nanoparticulate bimetallic benzene; nanoparticulate platinum permeate side catalyst; porous anode (3) comprising for example an yttrium stabilized nickel and zirconia cermet (YSZ); cathode (1), comprising for example lanthanum strontium manganite (LSM); yttrium doped zirconium phosphate electrolyte (2).
- YSZ yttrium stabilized nickel and zirconia cermet
- cathode (1) comprising for example lanthanum strontium manganite (LSM); yttrium doped zirconium phosphate electrolyte (2).
- a catalytic and electrocatalytic membrane reactor wherein hydrogen may be removed from the surface of the chemical catalyst by electrochemical pumping of hydrogen, comprising a nickel / nickel oxide chemical catalyst to conduct direct amination of benzene to aniline, decorated with nanoparticles of platinum responsible for the electrooxidation of hydrogen.
- the composite catalyst should be deposited at the interface between anode (3) and electrolyte (2);
- Anode (3) is formed by a porous palladium membrane of ca. 1 pm thick; the electrolyte (2) is made of zirconium phosphate
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Abstract
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Priority Applications (12)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EA201290284A EA024313B1 (ru) | 2009-11-06 | 2010-11-05 | Каталитический мембранный реактор с электрохимической перекачкой водорода или кислорода и его использование |
BR112012010764-0A BR112012010764A2 (pt) | 2009-11-06 | 2010-11-05 | reator catalítico de membrana com bombagem eletroquímica de hidrogênio ou de oxigênio e suas aplicações |
US13/508,542 US9498765B2 (en) | 2009-11-06 | 2010-11-05 | Hydrogen or oxygen electrochemical pumping catalytic membrane reactor and its applications |
AP2012006290A AP3617A (en) | 2009-11-06 | 2010-11-05 | A hydrogen or oxygen electrochemical pumping catalytic membrane reactor and its applications |
CN201080057841.6A CN102762292B (zh) | 2009-11-06 | 2010-11-05 | 氢或氧电化学抽吸催化膜反应器及其用途 |
CA2779953A CA2779953A1 (en) | 2009-11-06 | 2010-11-05 | A hydrogen or oxygen electrochemical pumping catalytic membrane reactor and its applications |
JP2012537478A JP5852575B2 (ja) | 2009-11-06 | 2010-11-05 | 水素又は酸素の電気化学的ポンピング触媒膜リアクタ及びその利用 |
MX2012005263A MX346341B (es) | 2009-11-06 | 2010-11-05 | Reactor catalítico de membrana con bombeo electroquímico de hidrógeno u oxígeno y sus aplicaciones. |
AU2010316633A AU2010316633B2 (en) | 2009-11-06 | 2010-11-05 | A hydrogen or oxygen electrochemical pumping catalytic membrane reactor and its applications |
EP10803630A EP2497570A2 (en) | 2009-11-06 | 2010-11-05 | A hydrogen or oxygen electrochemical pumping catalytic membrane reactor and its applications |
MA34839A MA33728B1 (fr) | 2009-11-06 | 2012-05-07 | Réacteur catalytique à membrane avec pompage éléctrochimique d'hydrogène ou d'oxygène et ses applications |
ZA2012/04096A ZA201204096B (en) | 2009-11-06 | 2012-06-05 | A hydrogen or oxygen electrochemical pumping catalytic membrane reactor and its applications |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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PT104812 | 2009-11-06 | ||
PT104812A PT104812A (pt) | 2009-11-06 | 2009-11-06 | Reactor catal?tico de membrana com bombagem electroqu?mica de hidrog?nio ou de oxig?nio e suas aplica??es |
Publications (2)
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WO2011055343A2 true WO2011055343A2 (pt) | 2011-05-12 |
WO2011055343A3 WO2011055343A3 (pt) | 2011-06-30 |
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PCT/IB2010/055045 WO2011055343A2 (pt) | 2009-11-06 | 2010-11-05 | Reactor catalítico de membrana com bombagem electroquímica de hidrogénio ou de oxigénio e suas aplicações |
Country Status (15)
Country | Link |
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US (1) | US9498765B2 (pt) |
EP (1) | EP2497570A2 (pt) |
JP (1) | JP5852575B2 (pt) |
KR (1) | KR20120105461A (pt) |
CN (1) | CN102762292B (pt) |
AP (1) | AP3617A (pt) |
AU (1) | AU2010316633B2 (pt) |
BR (1) | BR112012010764A2 (pt) |
CA (1) | CA2779953A1 (pt) |
EA (1) | EA024313B1 (pt) |
MA (1) | MA33728B1 (pt) |
MX (1) | MX346341B (pt) |
PT (1) | PT104812A (pt) |
WO (1) | WO2011055343A2 (pt) |
ZA (1) | ZA201204096B (pt) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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PT106860A (pt) * | 2013-03-28 | 2014-09-29 | Cuf Químicos Ind S A | Conjunto elétrodos/eletrólito, reator e método para a aminação direta de hidrocarbonetos |
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US9368821B2 (en) * | 2010-10-05 | 2016-06-14 | Industry-Academic Cooperation Foundation Yonsei University | Composite electrolyte membrane for fuel cell, method for producing the electrolyte membrane and fuel cell including the electrolyte membrane |
CN105552411B (zh) * | 2015-12-09 | 2017-09-22 | 佛山索弗克氢能源有限公司 | 氨气在sofc电池中的应用及其应用装置 |
WO2018031893A1 (en) * | 2016-08-11 | 2018-02-15 | Massachusetts Institute Of Technology | Electrochemical oxidation of aliphatic and aromatic compounds |
CN114807983B (zh) * | 2021-01-18 | 2024-06-04 | 武汉理工大学 | 一种用于实现不饱和烯炔烃选择性催化加氢的电化学系统 |
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WO2006138611A2 (en) * | 2005-06-16 | 2006-12-28 | Trustees Of Boston University | Waste to hydrogen conversion process and related apparatus |
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JP2008004312A (ja) * | 2006-06-20 | 2008-01-10 | Kuraray Co Ltd | イオン伝導性バインダー、膜−電極接合体及び燃料電池 |
CN101101887A (zh) * | 2006-07-06 | 2008-01-09 | 通用电气公司 | 抗腐蚀的晶片处理设备及其制造方法 |
JP5430079B2 (ja) * | 2007-06-12 | 2014-02-26 | キヤノン株式会社 | 膜電極接合体の製造方法 |
BR112012000628A2 (pt) * | 2009-07-10 | 2016-02-10 | Basf Se | processo para a aminação direta de hidrocarbonetos em amino hidrocarbonetos |
EP2451770B1 (de) * | 2009-07-10 | 2015-01-07 | Basf Se | Verfahren zur direktaminierung von kohlenwasserstoffen zu aminokohlenwasserstoffen mit elektrochemischer abtrennung von wasserstoff und elektrochemischer umsetzung des wasserstoffs zu wasser |
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-
2009
- 2009-11-06 PT PT104812A patent/PT104812A/pt unknown
-
2010
- 2010-11-05 AU AU2010316633A patent/AU2010316633B2/en not_active Ceased
- 2010-11-05 KR KR1020127014403A patent/KR20120105461A/ko not_active Application Discontinuation
- 2010-11-05 CA CA2779953A patent/CA2779953A1/en not_active Abandoned
- 2010-11-05 BR BR112012010764-0A patent/BR112012010764A2/pt not_active IP Right Cessation
- 2010-11-05 MX MX2012005263A patent/MX346341B/es active IP Right Grant
- 2010-11-05 EP EP10803630A patent/EP2497570A2/en not_active Withdrawn
- 2010-11-05 JP JP2012537478A patent/JP5852575B2/ja not_active Expired - Fee Related
- 2010-11-05 AP AP2012006290A patent/AP3617A/xx active
- 2010-11-05 US US13/508,542 patent/US9498765B2/en not_active Expired - Fee Related
- 2010-11-05 CN CN201080057841.6A patent/CN102762292B/zh not_active Expired - Fee Related
- 2010-11-05 WO PCT/IB2010/055045 patent/WO2011055343A2/pt active Application Filing
- 2010-11-05 EA EA201290284A patent/EA024313B1/ru not_active IP Right Cessation
-
2012
- 2012-05-07 MA MA34839A patent/MA33728B1/fr unknown
- 2012-06-05 ZA ZA2012/04096A patent/ZA201204096B/en unknown
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See also references of EP2497570A2 |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
PT106860A (pt) * | 2013-03-28 | 2014-09-29 | Cuf Químicos Ind S A | Conjunto elétrodos/eletrólito, reator e método para a aminação direta de hidrocarbonetos |
WO2014155360A1 (pt) | 2013-03-28 | 2014-10-02 | Cuf - Químicos Industriais S.A. | Conjunto elétrodos/eletrólito, reator e método para a aminação direta de hidrocarbonetos |
US10273589B2 (en) | 2013-03-28 | 2019-04-30 | Cuf—Quimicos Industriais S.A. | Electrodes/electrolyte assembly, reactor and method for direct amination of hydrocarbons |
US10689767B2 (en) | 2013-03-28 | 2020-06-23 | Bondalti Chemicals, S.A. | Electrodes/electrolyte assembly, reactor and method for direct amination of hydrocarbons |
Also Published As
Publication number | Publication date |
---|---|
BR112012010764A2 (pt) | 2018-03-06 |
AP2012006290A0 (en) | 2012-06-30 |
CN102762292B (zh) | 2015-09-30 |
JP5852575B2 (ja) | 2016-02-03 |
CA2779953A1 (en) | 2011-05-12 |
JP2013514873A (ja) | 2013-05-02 |
EA024313B1 (ru) | 2016-09-30 |
PT104812A (pt) | 2011-05-06 |
ZA201204096B (en) | 2013-08-28 |
US9498765B2 (en) | 2016-11-22 |
AU2010316633B2 (en) | 2016-04-14 |
CN102762292A (zh) | 2012-10-31 |
MX2012005263A (es) | 2012-09-07 |
MX346341B (es) | 2017-03-14 |
MA33728B1 (fr) | 2012-11-01 |
AP3617A (en) | 2016-02-29 |
EA201290284A1 (ru) | 2012-10-30 |
KR20120105461A (ko) | 2012-09-25 |
WO2011055343A3 (pt) | 2011-06-30 |
AU2010316633A1 (en) | 2012-06-14 |
EP2497570A2 (en) | 2012-09-12 |
US20120273366A1 (en) | 2012-11-01 |
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