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EP2601443A1 - Système en boucle chimique - Google Patents

Système en boucle chimique

Info

Publication number
EP2601443A1
EP2601443A1 EP10739916.4A EP10739916A EP2601443A1 EP 2601443 A1 EP2601443 A1 EP 2601443A1 EP 10739916 A EP10739916 A EP 10739916A EP 2601443 A1 EP2601443 A1 EP 2601443A1
Authority
EP
European Patent Office
Prior art keywords
fuel
reactor
chemical looping
oxygen carrier
oxide
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP10739916.4A
Other languages
German (de)
English (en)
Inventor
Horst Greiner
Alessandro Zampieri
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Siemens AG
Original Assignee
Siemens AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Siemens AG filed Critical Siemens AG
Publication of EP2601443A1 publication Critical patent/EP2601443A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C99/00—Subject-matter not provided for in other groups of this subclass
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/99008—Unmixed combustion, i.e. without direct mixing of oxygen gas and fuel, but using the oxygen from a metal oxide, e.g. FeO
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • Chemical looping system The present invention relates to a chemical looping system and a method of transferring oxygen between therein.
  • Chemical looping is a combustion technology with inherent separation of greenhouse gas CO 2 .
  • the technique involves the use of a metal oxide as an oxygen carrier for transferring oxygen from the air reactor to the fuel reactor.
  • the output product of oxidation of fuel i.e., carbon dioxide
  • the output product of oxidation of fuel is kept separate from the rest of the flue gases, such as nitrogen and any un- reacted oxygen.
  • Two reactors i.e., the air reactor and the fuel reactor having interconnected fluidized beds are used for this process.
  • the metal is oxidized to metal oxide with air in the air reactor and the oxidized metal oxide is re ⁇ cuted to metal in the fuel reactor.
  • the reduced metal is transported back to the air reactor from the fuel reactor.
  • metal-oxides with different oxidation states can be used as oxygen carriers between the air and the fuel reactor.
  • the outlet gas from the air reactor comprises 2 and un-reacted O 2 if any.
  • the outlet gas from the fuel reactor comprises CO 2 and 3 ⁇ 40 which can be separate by condensation.
  • the CO 2 being separate from the flue gas is sequestration ready without the requirement of additional amount of energy and additional expensive separation units.
  • Chemical looping system can be used for producing power by combusting a gaseous fuel, and the technique is referred to as chemical looping combustion (CLC) .
  • CLC chemical looping combustion
  • CLR chemical looping reforming
  • the CLC system is generally integrated into a combined cycle power process.
  • the oxygen carrier comprising the oxide-dispersion- strengthened alloy particles is oxidized in the air reactor and transported to the fuel reactor.
  • the fuel in the fuel re ⁇ actor reacts with the oxidized oxygen carrier and is oxi ⁇ dized.
  • the oxygen carrier is reduced and the reduced oxygen carrier is transported back to the air reactor, where they are oxidized again.
  • the oxygen carriers are circulated between the air reactor and the fuel reactor for transferring oxygen from the air reactor to the fuel reactor.
  • the oxygen carrier being oxide-dispersion-strengthened alloy particles are less prone to sintering, and thus, more resistance to ag ⁇ glomeration during the high operating temperature of the chemical looping system.
  • the rate of decrease of the available active surface area for the oxidation/reduction re ⁇ actions is reduced and thus, improving the redox activity over time. This enables the oxygen carriers to achieve longer operation life and reduce the operation costs of the chemical looping system.
  • the oxide-dispersion-strengthened alloy particles are composed of a metal having a dispersion of a metal oxide or a carbide. Dispersion of the metal oxide or the carbide into the metal enables in strengthening the metal and increase the redox activity.
  • the oxygen carrier is prepared by using binders such as alumina, silica, etc.
  • the oxygen carrier is generally composed of a metal which can be oxidized to form a metal oxide to provide the oxygen for the combustion process, and an inert element as a binder for increasing the mechanical strength.
  • the metal particles can be im- pregnated with a substrate, such as, a porous alumina sub ⁇ strate.
  • the metal is selected from the group consisting of nickel, copper, iron, cobalt, manganese.
  • the metals have relatively good oxygen transfer capabilities .
  • the metal oxide is selected from the group consisting of cerium oxide, tita ⁇ nium oxide, and zirconium oxide.
  • the carbide is silicon carbide.
  • the metal oxide or the carbide is doped.
  • the fuel comprises a carbonaceous fuel.
  • the carbonaceous fuel can be com ⁇ busted easily.
  • the fuel reactor is adapted to combust the fuel to produce the gas.
  • the fuel is oxidized for combustion by reducing the oxygen carrier.
  • the reduced oxygen carrier can be transported to the air reactor for oxidation, which is an exothermic reaction, thus producing energy.
  • the gas comprises CO2 and H2O .
  • the CO2 from the gas can easily be separated by con ⁇ densing H2O .
  • the CO2 obtained is sequestration ready as the same is separate from the flue gases.
  • the CO2 is sepa- rated from the flue gases without the requirement of addi ⁇ tional amount of energy and additional expensive separation units .
  • the fuel reactor is adapted to partially oxidize the fuel to produce the gas
  • the gas comprises a reformer gas.
  • the fuel is par ⁇ tially oxidized by reducing the oxygen carrier.
  • the reduced oxygen carrier can be transported to the air reactor for oxidation .
  • the reformer gas comprises 3 ⁇ 4, CO, C 2 O and 3 ⁇ 40.
  • the 3 ⁇ 4 of the reformer gas can be used as a fuel. Additional 3 ⁇ 4 can be obtained by reacting CO and 3 ⁇ 40 in a shift reactor.
  • the CO 2 can easily be separated from 3 ⁇ 4, and the separated CO 2 is sequestration ready as the same is separate from the flue gases.
  • the CO 2 is separated from the flue gases without the requirement of additional amount of energy and additional expensive separation units.
  • fuel reactor is further adapted to receive steam.
  • the generation of 3 ⁇ 4 can be enhanced by supplying steam into the fuel reactor.
  • FIG 1 illustrates a schematic block diagram of a chemical looping system according to an embodiment herein
  • FIG 2 illustrates an enlarged view of an ODS alloy
  • FIG 3 is a flow diagram illustrating a method of transfer- ring oxygen in a chemical looping system according to an embodiment herein.
  • FIG 1 illustrates a schematic block diagram of a chemical looping system according to an embodiment herein.
  • the chemical lopping system 10 comprises an air reactor 15 and a fuel reactor 20.
  • the air reactor 15 and the fuel reactor 20 are fluid- ized bed reactors.
  • air is supplied as oxidant is into the air reactor 15, as designated by the arrow 25.
  • a fuel is supplied into the fuel reactor 20, as designated by the arrow 30.
  • the air reactor 15 and the fuel reactor are isolated and thus, there is no direct con ⁇ tact between air and fuel.
  • Oxygen from the air reactor 15 is transferred to the fuel reactor 20 by circulating an oxygen carrier between the air reactor 15 and the fuel reactor 20, as designated by the arrows 35 and 40 respectively.
  • the oxy ⁇ gen carrier is oxidized in the air reactor 15 forming an oxide.
  • the oxide is then transported to the fuel reactor 20 where the fuel reduces the oxide to its original state.
  • the oxygen carrier in its original state is transported back to the air reactor 15, where it is again oxidized and is trans ⁇ ported to the fuel reactor 20.
  • This transportation of the ox ⁇ ide to the fuel reactor 20 from the air reactor 15 and the transportation of the oxygen carrier in its original state from the fuel reactor 20 to the air reactor 15 is the circu ⁇ lation of the oxygen carrier between the air reactor 15 and fuel reactor 20.
  • the air reactor 15 and the fuel reactor 20 are isolated and thus, there is no direct contact between air and fuel.
  • the oxygen carrier transported from the air reactor 15 to the fuel reactor 20 provides the necessary oxygen re ⁇ quired for the oxidation of the fuel in the fuel reactor 20.
  • the oxygen carrier comprises oxide- dispersion-strengthened (ODS) alloy particles.
  • the ODS alloy particles are composed of a metal having a dispersion of a metal oxide or a carbide.
  • the metal particles are strength ⁇ ened by the dispersion of the metal oxide or the carbide.
  • the ODS alloy particles transfer oxygen from the air reactor 15 to the fuel reactor 20.
  • the ODS alloy particles are in powder form, and thus, the particles are not grouped together.
  • the ungrouped ODS alloy particles provide larger surface area for the redox reactions in the air reactor 15 and the fuel reac ⁇ tor 20.
  • the metal used for preparing the ODS alloy particles include, but not limited to, nickel, copper, iron, cobalt, manganese, cadmium, and the like.
  • the metal oxide may include, but not limited to, cerium oxide, titanium oxide, zirconium oxide and the like.
  • the car ⁇ bide may include, but not limited to, silicon carbide and tungsten carbide.
  • the metal oxide and the carbide may be doped or un-doped.
  • the ODS alloy particles may be formed by dispersing the metal oxide or the carbide into the metal by mechanical alloying.
  • advanta ⁇ geously the ODS alloy particles may be supported on alumina, titanium oxide, YSR particles or other ceramics. The ODS al ⁇ loy particles could also be recycled after the operation via thermal treatment to separate the metal and the metal oxide dispersion .
  • the gas exiting the air reactor 15, as designated by the arrow 42, will comprise ni ⁇ trogen and un-reacted oxygen if any.
  • the gas exited from the air reactor 15 can be discharged into the atmosphere causing minimal or no CO 2 pollution.
  • the gas produced due to the oxi ⁇ dation of the fuel by the oxygen carried in the fuel reactor 20 is exited from the reactor 20, as shown by the arrow 44.
  • the chemical looping system 10 can be operated as a chemical looping combustion (CLC) to produce energy by combusting the fuel.
  • a carbona- ceous fuel is supplied as the fuel into the fuel reactor 15.
  • the term "carbonaceous fuel” hereinafter is referred to any material made of or containing carbon which is combustible or flammable.
  • the carbonaceous fuel comprises, but not limited to, fossil fuels and fuels derived from fossil fuels.
  • the carbonaceous fuel supplied into the fuel reac ⁇ tor 20 may be a gaseous fuel, such as, natural gas. Solid fu ⁇ els can also used by gasifying the same to gaseous fuels and thereafter introducing the same into the fuel reactor 20.
  • the gasification of the solid fuel may be performed in the fuel reactor 20 or may be performed externally in a separate reac ⁇ tor.
  • the carbonaceous fuel supplied into the fuel reactor 20 is methane. Air is supplied as the oxidant into the air reactor 15, as shown by the arrow 25.
  • the metal present in the ODS alloy particles is oxidized by air in the air reactor 15 to form a metal oxide (M e O) .
  • the ODS alloy particles containing the metal oxide are trans ⁇ ported to the fuel reactor 20, as shown by the arrow 35.
  • the oxidation of the ODS alloy particles is an exothermic reac ⁇ tion.
  • the fuel in the fuel reactor 20 is completely oxi ⁇ dized by reducing the metal oxide of the ODS alloy particles to metal.
  • the fuel is combusted using the oxygen car- ried by the oxygen carrier from the air reactor 15.
  • the reduction of the metal oxide of the ODS alloy particles to metal is an endothermic reaction.
  • the ODS alloy particles containing the reduced metal are transported back to the air reactor 15, as shown by the arrow 40.
  • the gas stream exiting the fuel reactor 15, illustrated by the arrow 44 comprises CO 2 and 3 ⁇ 40. CO 2 can easily be sepa ⁇ rated from the exited gas stream by condensing 3 ⁇ 40.
  • the sepa ⁇ rated CO 2 is pure as the same is separate from flue gases, and thus, ready for sequestration. This assists in separating CO 2 from 2 and NO x compounds without the consumption of addi ⁇ tional energy and implementation of additional separation units .
  • M e is metal
  • M e O is metal oxide
  • the chemical looping system 10 can be operated as a chemical looping re ⁇ forming (CLR) to produce a reformer gas comprising 3 ⁇ 4 by partially oxidizing the fuel.
  • the fuel supplied into the fuel reactor 20 comprises a carbo ⁇ naceous fuel.
  • the carbonaceous fuel supplied into the fuel reactor 20 may be a natural gas.
  • the carbonaceous fuel supplied into the fuel reactor 20 is methane.
  • ad ⁇ ditional oxygen may be supplied into the fuel reactor 20 in the form of steam (3 ⁇ 40) .
  • the steam may be supplied into the fuel reactor though the same inlet with which the fuel is supplied or may be supplied through a separate inlet.
  • Air is supplied as the oxidant into the air reactor 15, as shown by the arrow 25.
  • the metal present in the ODS alloy particles is oxidized by air in the air reactor 15 to form a metal oxide (M e O) .
  • the ODS alloy particles containing the metal oxide are transported to the fuel reactor 20, as shown by the arrow 35.
  • the oxidation of the ODS alloy particles is an exothermic re ⁇ action.
  • the fuel in the fuel reactor 20 reacts with the metal oxide of the ODS alloy particles and is partially oxidized and the metal oxide is reduced to metal.
  • the reduction of the metal oxide of the ODS alloy particles to metal is an endo ⁇ thermic reaction.
  • the ODS alloy particles containing the re ⁇ quizd metal are transported back to the air reactor 15, as shown by the arrow 44.
  • the partial oxidation of the fuel in the fuel reactor 20 produces a gas comprising a reformer gas.
  • the reformer gas can comprise a syngas, CO 2 and H 2 O.
  • the syngas is a gas comprising a mixture of CO and 3 ⁇ 4 .
  • addi ⁇ tional 3 ⁇ 4 can be produced by reacting CO and 3 ⁇ 40 in a subse ⁇ quent shift reactor.
  • CO 2 can easily be separated from the re ⁇ former gas.
  • the separated CO 2 is pure as the same is separate from flue gases, and thus, ready for sequestration. This as ⁇ sists in separating CO 2 from 2 and NO x compounds without the consumption of additional energy and implementation of additional separation units.
  • the reactions in the air reactor 15, fuel reactor 20 and the shift reactor can be summarized as follows:
  • FIG 2 illustrates an enlarged view of an ODS alloy particle according to an embodiment herein.
  • the ODS alloy particle 45 is formed of a metal 50 and particles of a metal oxide 55 dispersed into the meta1 26.
  • the ODS alloy particles 45 have increased strength relative to particles of simple metal. Using the ODS alloy particles 45 as oxygen carriers prevent sintering of the particles at the high operation temperature, and thus, prevent the de- crease in the surface area per filling volume of the parti ⁇ cles 45. Sintering of the metal-fuel particles leads to ag ⁇ glomeration of the particles during high temperature treat ⁇ ment, and thus, degradation in the performance of a chemical looping system with time, as the surface area per filling volume of the particles decreases.
  • the degradation rate of the performance of the chemical looping system 10 of FIG 1 with time is reduced and the life-time of the chemical loop ⁇ ing system 10 is increased by using ODS alloy particles 45 as oxygen carriers as the same are less prone to sintering, and thus, more resistant to agglomeration.
  • the ODS alloy parti ⁇ cles being more resistant to agglomeration enable in reducing the rate of decrease of the active surface area for redox re ⁇ actions at the fuel reactor 20 of FIG 1 and the oxidation re- actor 15 of FIG 1 and also improve the redox activity over time of the oxygen carrier.
  • the ODS alloy par ⁇ ticles can posses relatively higher ionic conductivity during redox processes if the dispersed oxide on the metal is an O2 conductor.
  • the higher ionic conductivity enables in enhancing the redox reaction rate.
  • FIG 3, with reference to FIG 1 through FIG 2, is a flow dia ⁇ gram illustrating a method of transferring oxygen in a chemical looping system according to an embodiment herein.
  • an air reactor 15 adapted to receive an oxidant for oxidizing an oxygen carrier is provided.
  • a fuel reactor 20 adapted to receive a fuel and the oxidized oxygen carrier for at least partially oxidizing the fuel by reducing the oxygen carrier to produce a gas, and wherein, the oxygen carrier comprises oxide-dispersion-strengthened alloy particles.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un système en boucle chimique (10) et un procédé de transfert d'oxygène à l'intérieur de ce système. Ledit système comprend : un réacteur à air (15) qui est conçu pour recevoir de l'air afin d'oxyder un transporteur d'oxygène ; et un réacteur à combustible (20) qui permet de recevoir un combustible ainsi que le transporteur d'oxygène oxydé en vue d'oxyder au moins en partie le combustible grâce à la réduction du transporteur d'oxygène pour produire un gaz, le transporteur d'oxygène comportant des particules d'alliage renforcé par dispersion d'oxyde (45).
EP10739916.4A 2010-08-02 2010-08-02 Système en boucle chimique Withdrawn EP2601443A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2010/061200 WO2012016582A1 (fr) 2010-08-02 2010-08-02 Système en boucle chimique

Publications (1)

Publication Number Publication Date
EP2601443A1 true EP2601443A1 (fr) 2013-06-12

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EP10739916.4A Withdrawn EP2601443A1 (fr) 2010-08-02 2010-08-02 Système en boucle chimique

Country Status (3)

Country Link
US (1) US20130125462A1 (fr)
EP (1) EP2601443A1 (fr)
WO (1) WO2012016582A1 (fr)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9371227B2 (en) 2009-09-08 2016-06-21 Ohio State Innovation Foundation Integration of reforming/water splitting and electrochemical systems for power generation with integrated carbon capture
US9376318B2 (en) 2008-09-26 2016-06-28 The Ohio State University Conversion of carbonaceous fuels into carbon free energy carriers
US9518236B2 (en) 2009-09-08 2016-12-13 The Ohio State University Research Foundation Synthetic fuels and chemicals production with in-situ CO2 capture
US9616403B2 (en) 2013-03-14 2017-04-11 Ohio State Innovation Foundation Systems and methods for converting carbonaceous fuels
US9777920B2 (en) 2011-05-11 2017-10-03 Ohio State Innovation Foundation Oxygen carrying materials
US9903584B2 (en) 2011-05-11 2018-02-27 Ohio State Innovation Foundation Systems for converting fuel
US10010847B2 (en) 2010-11-08 2018-07-03 Ohio State Innovation Foundation Circulating fluidized bed with moving bed downcomers and gas sealing between reactors
US10022693B2 (en) 2014-02-27 2018-07-17 Ohio State Innovation Foundation Systems and methods for partial or complete oxidation of fuels
US10144640B2 (en) 2013-02-05 2018-12-04 Ohio State Innovation Foundation Methods for fuel conversion
US10549236B2 (en) 2018-01-29 2020-02-04 Ohio State Innovation Foundation Systems, methods and materials for NOx decomposition with metal oxide materials
US11090624B2 (en) 2017-07-31 2021-08-17 Ohio State Innovation Foundation Reactor system with unequal reactor assembly operating pressures
US11111143B2 (en) 2016-04-12 2021-09-07 Ohio State Innovation Foundation Chemical looping syngas production from carbonaceous fuels
US11413574B2 (en) 2018-08-09 2022-08-16 Ohio State Innovation Foundation Systems, methods and materials for hydrogen sulfide conversion
US11453626B2 (en) 2019-04-09 2022-09-27 Ohio State Innovation Foundation Alkene generation using metal sulfide particles

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9004911B1 (en) * 2012-11-29 2015-04-14 U.S. Department Of Energy Apparatus and method for solid fuel chemical looping combustion
US9909756B2 (en) 2012-11-30 2018-03-06 Saudi Arabian Oil Company Staged chemical looping process with integrated oxygen generation
GB2512334A (en) * 2013-03-26 2014-10-01 Gas Recovery & Recycle Ltd Materials for use in chemical looping combustion
US10670262B2 (en) * 2014-02-26 2020-06-02 University Of Connecticut Reactor for chemical-looping combustion
US10214700B1 (en) * 2015-09-29 2019-02-26 National Technology & Engineering Solutions Of Sandia, Llc Methods utilizing durable functional materials for chemical processes that include an oxidation step
US10662130B2 (en) 2017-08-15 2020-05-26 Exxonmobil Research And Engineering Company Process for generation of olefins
US10239763B1 (en) * 2017-12-05 2019-03-26 Saudi Arabian Oil Company System for tail gas treatment of sulfur recovery units
AU2020208415A1 (en) 2019-01-17 2021-07-22 Ohio State Innovation Foundation Systems, methods and materials for stable phase syngas generation
US20220331736A1 (en) * 2019-09-03 2022-10-20 Ohio State Innovation Foundation Redox reaction facilitated carbon dioxide capture from flue gas and conversion to carbon monoxide

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2607668A (en) * 1947-08-12 1952-08-19 Standard Oil Dev Co Production of industrial gases containing carbon monoxide and hydrogen
US4427447A (en) * 1982-03-31 1984-01-24 Exxon Research And Engineering Co. Alumina-yttria mixed oxides in dispersion strengthened high temperature alloy powders
US5268657A (en) * 1992-07-10 1993-12-07 Hughes Aircraft Company High performance oscillator circuit with minimum frequency pulling at power on
FR2850156B1 (fr) * 2003-01-16 2005-12-30 Alstom Switzerland Ltd Installation de combustion avec recuperation de co2
US20090020405A1 (en) * 2007-07-20 2009-01-22 Foster Wheeler Energy Corporation Method of and a plant for combusting carbonaceous fuel by using a solid oxygen carrier

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2012016582A1 *

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US10081772B2 (en) 2008-09-26 2018-09-25 The Ohio State University Conversion of carbonaceous fuels into carbon free energy carriers
US9376318B2 (en) 2008-09-26 2016-06-28 The Ohio State University Conversion of carbonaceous fuels into carbon free energy carriers
US9518236B2 (en) 2009-09-08 2016-12-13 The Ohio State University Research Foundation Synthetic fuels and chemicals production with in-situ CO2 capture
US10865346B2 (en) 2009-09-08 2020-12-15 Ohio State Innovation Foundation Synthetic fuels and chemicals production with in-situ CO2 capture
US10253266B2 (en) 2009-09-08 2019-04-09 Ohio State Innovation Foundation Synthetic fuels and chemicals production with in-situ CO2 capture
US9371227B2 (en) 2009-09-08 2016-06-21 Ohio State Innovation Foundation Integration of reforming/water splitting and electrochemical systems for power generation with integrated carbon capture
US10010847B2 (en) 2010-11-08 2018-07-03 Ohio State Innovation Foundation Circulating fluidized bed with moving bed downcomers and gas sealing between reactors
US9903584B2 (en) 2011-05-11 2018-02-27 Ohio State Innovation Foundation Systems for converting fuel
US9777920B2 (en) 2011-05-11 2017-10-03 Ohio State Innovation Foundation Oxygen carrying materials
US10502414B2 (en) 2011-05-11 2019-12-10 Ohio State Innovation Foundation Oxygen carrying materials
US10501318B2 (en) 2013-02-05 2019-12-10 Ohio State Innovation Foundation Methods for fuel conversion
US10144640B2 (en) 2013-02-05 2018-12-04 Ohio State Innovation Foundation Methods for fuel conversion
US9616403B2 (en) 2013-03-14 2017-04-11 Ohio State Innovation Foundation Systems and methods for converting carbonaceous fuels
US10022693B2 (en) 2014-02-27 2018-07-17 Ohio State Innovation Foundation Systems and methods for partial or complete oxidation of fuels
US11111143B2 (en) 2016-04-12 2021-09-07 Ohio State Innovation Foundation Chemical looping syngas production from carbonaceous fuels
US11090624B2 (en) 2017-07-31 2021-08-17 Ohio State Innovation Foundation Reactor system with unequal reactor assembly operating pressures
US10549236B2 (en) 2018-01-29 2020-02-04 Ohio State Innovation Foundation Systems, methods and materials for NOx decomposition with metal oxide materials
US11413574B2 (en) 2018-08-09 2022-08-16 Ohio State Innovation Foundation Systems, methods and materials for hydrogen sulfide conversion
US11826700B2 (en) 2018-08-09 2023-11-28 Ohio State Innovation Foundation Systems, methods and materials for hydrogen sulfide conversion
US11453626B2 (en) 2019-04-09 2022-09-27 Ohio State Innovation Foundation Alkene generation using metal sulfide particles
US11767275B2 (en) 2019-04-09 2023-09-26 Ohio State Innovation Foundation Alkene generation using metal sulfide particles

Also Published As

Publication number Publication date
US20130125462A1 (en) 2013-05-23
WO2012016582A1 (fr) 2012-02-09

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