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WO2008082312A1 - Production d'hydrogène - Google Patents

Production d'hydrogène Download PDF

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Publication number
WO2008082312A1
WO2008082312A1 PCT/NO2008/000004 NO2008000004W WO2008082312A1 WO 2008082312 A1 WO2008082312 A1 WO 2008082312A1 NO 2008000004 W NO2008000004 W NO 2008000004W WO 2008082312 A1 WO2008082312 A1 WO 2008082312A1
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WO
WIPO (PCT)
Prior art keywords
reactor
sorbent
loop
riser
conveyed
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Ceased
Application number
PCT/NO2008/000004
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English (en)
Inventor
Bjørnar ARSTAD
Ivar Martin Dahl
Richard Blom
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Sinvent AS
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Sinvent AS
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Classifications

    • 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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/42—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles
    • C01B3/44—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles using the fluidised bed technique
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/0425—In-situ adsorption process during hydrogen production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane

Definitions

  • the present invention comprises a method and system for continuous production of hydrogen gas and simultaneously separation of at least one gas product component.
  • Hydrogen will be an important energy carrier in the future and much research is focused on various production methods. Hydrogen production may be completed by use of renewable energy sources, via e.g. hydrolysis of water into H 2 and O 2 , or from fossil fuels like, coal, oil and gas.
  • renewable energy sources via e.g. hydrolysis of water into H 2 and O 2
  • fossil fuels like, coal, oil and gas.
  • the major way to produce hydrogen/synthesis gas from fossil fuel today is by steam reforming (SR) of natural gas which is a two step reaction:
  • the highly endothermic SR reaction (3) takes place at 700-900 0 C using a nickel based catalyst.
  • the second reaction is the water-gas shift reaction in which CO reacts with water and produces CO 2 and H 2 . These reactions are reversible and by removing CO 2 with an internal sorbent during reaction more hydrogen will be produced. This is favorable since a typical equilibrium hydrogen concentration in steam reforming of methane is only ca. 70-75 %.
  • SESR sorption enhanced steam reforming
  • sorbents may be suitable for SESR, both natural and synthetic ones.
  • Some common sorbents that have been used, or have a potential use in SESR is natural dolomite, (a mixed carbonate of MgCO 3 and CaCO 3 ), lime (CaO), and potassium promoted hydrotalcite [4-7].
  • Dolomite is a very common mineral in nature and together with two other calcium carbonates (calcite and aragonite) it makes up -2% of the earth's crust [8].
  • Calcium oxide based sorbents may react with CO 2 and form carbonates in an exothermic reaction like:
  • CO 2 desorbs from the material at ca. 800 0 C, and higher, depending on composition of the atmosphere. In a pure CO 2 atmosphere at 1 atm. CO 2 desorbs from the solid material at ca. 900 0 C and at lower temperatures by reducing the partial pressure of CO 2 .
  • the material should last for many absortion/desorption cycles but in reality it will eventually detoriate and become less effective.
  • Several studies have addressed these problems for natural sorbents like dolomite and lime. These materials may deactivate due to sintering, because of impurities and minerals in the feed, or from the formation of hydroxyl groups on the surface [5, 9-11]. Loss of structure and mechanical strength may also take place due to cracking and breaking down of the material during use.
  • Silaban et al. compared dolomite and lime and found that with CaO obtained from CaCO 3 , the first-cycle fractional recarbonation was limited to about 0.80, a value which decreased by 15 to 20% in each subsequent cycle.
  • Sorption enhanced steam reforming is a process suitable for a cyclic reactor unit but most works so far have mostly used systems that switch gases over a catalyst bed during the experiments thus simulating the cyclic process of absorption/desorption of CO 2 . Both fixed beds and fluidized bed reactor systems have been used [4, 21-24].
  • the present invention comprises a method and system for SESR or other sorbent enhanced reactions, e.g. sorbent enhanced watergas shift reactions.
  • the present invention comprises two reactors that operate in a bubbling fluidization regime.
  • the present invention has a riser that is used for transporting powder in the system. In the present invention there are no reaction taking place in the riser.
  • a separate fluidized bed reactor is required in order to regenerate the catalyst due to the relative long regeneration time of the present sorbent.
  • the present invention is a continuous process for the production of H 2 and simultaneously separation of CO 2 and not a combustion process.
  • the objective of the present invention is to provide a method and system for continuous production of hydrogen gas and simultaneously separating produced CO 2 away from the effluent gas.
  • the feed to be converted in the reactor could be natural gas, gasified coal or biomass or it could be suitable oil fractions.
  • the feed into the reactor could also be CO and steam for sorbent enhanced watergas shift reactions.
  • the present invention comprises a method for continuous production of hydrogen gas and simultaneously separation of at least one gas product component, in which at least one feed gas is fed to a first reactor, comprising a sorbent powder, said feed gas is converted into at least one gas product component in which at least one gas product component is substantially absorbed by the sorbent powder, and hydrogen gas produced thereby is separated off, wherein said sorbent is conveyed into a loop-seal, further said sorbent is conveyed out of said loop-seal and into a riser, said sorbent is conveyed via said riser into a second reactor for regeneration, and said at least one gas product component is separated off, said sorbent is conveyed into a second loop-seal, said sorbent is conveyed out of said second loop-seal and further to said first reactor.
  • the present invention comprises an embodiment in which a method for continuous production of hydrogen gas and simultaneously separation of at least one gas product component, in which at least one feed gas is fed to a first reactor, comprising a sorbent powder, said feed gas is converted into at least one gas product component in which at least one gas product component is substantially absorbed by the sorbent powder, and hydrogen gas produced thereby is separated off, wherein said sorbent is conveyed into a loop-seal, further said sorbent is conveyed out of said loop-seal and into a second reactor for regeneration, and said at least one gas product component is separated off, said sorbent is conveyed into a second loop-seal, further said sorbent is conveyed out of said second loop-seal and into a riser, said sorbent is conveyed via said riser into said first reactor.
  • a feature of the present invention is to convey the sorbent substantially vertically into and out of said loop seals.
  • said loop seal comprises a substantially S- shaped tube, and at least one of the following gases is fed to said loop seals: steam and inert gas.
  • the following gases are fed to the reactors according to the invention: steam, inert gas, CO, CO 2 , H 2 and hydrocarbon containing gas.
  • Concerning the riser of the invention at least one of the following gases are fed to said riser: steam, inert gas and CO 2 .
  • the temperature of said first and second reactor is at least 100 ° C. Further, the temperature of said second reactor is in the range of from 300 - 1000 0 C. The temperature of said second reactor is higher than the temperature of said first reactor.
  • the present invention may comprise a catalyst.
  • the sorbent may be conveyed from said riser via a cyclone to a second reactor in the present invention. Another embodiment of the invention is the sorbent being conveyed from said riser via a cyclone to a first reactor.
  • a feature of the present invention is the possibility of conveying the sorbent directly from said riser to said second reactor.
  • the use of the expression directly in the present invention should be understood as directly with no opportunity for other apparatus between the mentioned riser and the mentioned reactor. Further, said sorbent is conveyed directly from said riser to said first reactor.
  • Another aspect of the present invention is a system for continuous production of hydrogen gas and simultaneously separation of at least one gas product component, comprising at least two fluidized bed reactors, at least two loop seals and a riser.
  • the inlet to and an outlet from said loop seals are arranged substantially vertically, and the loop seals are substantially S-shaped.
  • An embodiment of the present invention is a system in which said second reactor and second loop seal is succeeded by said first reactor and said first loop seal and further succeeded by said riser. Further, a cyclone is arranged previous to said second reactor. Another feature of the invention is that the riser is directly connected to said second reactor.
  • a further embodiment of the system according to the invention is the first reactor and first loop seal being succeeded by said second reactor and said second loop seal and further succeeded by said riser.
  • the embodiment can be arranged with a cyclone previous to said first reactor. Further, the mentioned riser is directly connected to said first reactor.
  • An even further embodiment of the system for continuous production of hydrogen gas and simultaneously separation of at least one gas product component comprises the following: a first fluidized bed reactor and a first loop seal substantially vertically thereunder, said first fluidized bed reactor and first fluidized loop seal constituting a first reactor group, further a second fluidized bed reactor, and a second loop seal substantially vertically thereunder, said second fluidized bed reactor and second loop seal constituting a second reactor group, one of said groups being a top group arranged substantially vertically above the other lower group for conveying said sorbent powder substantially vertically downward from the top group to the lower group, and a riser for returning said sorbent powder from a bottom exit of the lower group to an entrance on top of the top group, completing a sorbent powder cycle arrangement, one of said reactors being a main reactor and comprising a H 2 exit, and the other reactor being a regeneration reactor and comprising an exit for said at least one gas product component.
  • the temperature of said first and said second reactor is at least 100 ° C.
  • the present invention comprises a method for continually production of H 2 and simultaneously separation of a combustion gas, wherein at least one feed gas is conveyed to a first reactor optionally together with steam and/or other reactive gases, said first reactor is a fluidized bed reactor comprising a sorbent in which at least one reaction takes place, said sorbent is conveyed into a loop seal and further through a riser, optionally into a cyclone and further into a second reactor for regeneration, said sorbent is conveyed into a second loop seal and further to said first reactor.
  • said loop seal comprises a U shaped tube.
  • U-shape can also be regarded as part of a S-shape.
  • the steam are conveyed to said loop seals and reactors.
  • the system for continually production of H 2 and a combustion gas comprises at least two fluidized bed reactors, at least two loop seals, a riser and optionally a cyclone.
  • the loop seals has a U like shape.
  • Figure 1 shows equilibrium pressure of CO 2 over a CaO/CaCO 3 mixture as a function of temperature [28].
  • Figure 2 shows the stability of lithium zirconate during capture/regeneration cycles. The figure shows high stability and fast kinetics during several sorption/desorption processes [16].
  • Figure 3 shows two selected structures of adsorbed CO 2 on MgO/CaO particles
  • FIG. 29 Note the two different adsorption modes of CO 2 , a) bidentate and b) tridentate. Red atoms are oxygen and green atoms are Mg/Ca [19].
  • Figure 4 is a schematic drawing of the fluidized bed reformer used by Johnsen et al. [4].
  • Figure 5 shows outlet composition (dry basis) as a function of time [4].
  • Figure 6 shows a process diagram of the SESR concept.
  • the sorbent in this case
  • the catalyst is transported between the two reactor units.
  • the effluent gases the reactors do also contain inert gases and unconverted feed.
  • Figure 7 shows a reactor system according to the present invention in which two connected fluidized beds perform continually two different chemical reactions in sequence.
  • the sorbent is conveyed via a cyclone before regeneration.
  • Figure 8 shows a reactor system according to the present invention in which two connected fluidized beds perform continually two different chemical reactions in sequence.
  • Figure 9 shows a reactor system according to the present invention in which a first reactor and first loop seal is succeeded by a second reactor and a second loop seal in which the sorbent is conveyed via a riser to a cyclone previous to said first reactor.
  • Figure 10 shows a reactor system according to the present invention in which a first reactor and first loop seal is succeeded by a second reactor and a second loop seal via a riser to said first reactor.
  • the shape and mentioning of the loop seal as S-shaped in the present invention should be understood according to figure 7 and 8.
  • the shape and expression U- shaped should in the present invention also be understood as mentioned previously as U-shaped, or rather as S-shaped.
  • the loop seal should also be understood as a powder lock.
  • the present invention comprises a process for continuous production of H 2 from natural gas or a hydrocarbon containing gas and simultaneously separation of CO 2 . Further, said invention also comprises a system in which the reactor unit is designed with two connected fluidized bed reactors that makes it possible to perform continually two different chemical reactions in sequence, like e.g. sorption enhanced steam reforming or other sorbent enhanced reactions. Examples:
  • the sorbent Dolomite or others
  • the catalyst Ni-based or a common reforming catalyst
  • the feed is a mixture of CH 4 and steam and the total feed gas flow is from 2-5 L/min.
  • the outlet is enriched of hydrogen. After some residence time in the reactor the powder falls, via a tube, into a chamber in a loop seal.
  • 2x2 cm areal and 10 cm high.
  • 1-1.5 L/min gas nitrogen/steam
  • the loop seal has a S like shape, and function to separate the two reactor gas streams from each other. Without these two loop seals the reactors would be connected and the outlet gases mixed.
  • the powder is transported through the S- shaped loop seal and falls into a pipe that is connected with the riser.
  • the particular design shown in the figure ensures that the powder is transported together with the loop seal feed gas into the riser easily and without problems.
  • the riser is a tube used for transporting used powder to the top of the reactor unit and into reactor 2, via a cyclone.
  • the riser gas (N 2 /CO 2 ) is fed at a rate of 2-3 L/min.
  • Reactor 2 is able to separate the particles from the riser gas stream. In this reactor unit this may be done but it is not necessary. At present the cyclone is used as an intermediate unit before the riser gas and powder is transported into reactor 2. Reactor 2:
  • Reactor 2 is used for regeneration of the sorbent at 300-1000 ° C, preferably 800-900°C.
  • the fluidizing gases in reactor 2 may be CO 2 /N 2 /steam.
  • the sorbent carries CO 2 that is liberated when heated.
  • the outlet of reactor two is the carrier gas and CO 2 . Recirculation of parts of the CO 2 gas may be used for the riser carrier gas. After some minutes in reactor 2, the powder is transported via loop seal 2 (similar to loop seal 1) and into reactor 1 for another cycle of the sorption enhanced steam reforming.
  • the presented reactor system is a design that shows a technical solution for coupling two fluidized beds that can be used for e.g. sorption enhanced steam reforming.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un procédé pour la production d'hydrogène gazeux en continu et simultanément, la séparation d'au moins un composant produit gazeux ; procédé dans lequel un gaz d'alimentation est transporté jusqu'à un premier réacteur comprenant du sorbant en poudre ; le flux d'entrée riche en hydrocarbures est converti en au moins un composant produit gazeux qui est sensiblement absorbé par le sorbant en poudre ; ledit sorbant est transporté de manière sensiblement verticale dans une boucle d'étanchéité et traverse un tuyau sensiblement en forme de S ; ledit sorbant est ensuite transporté de manière sensiblement verticale hors de ladite boucle d'étanchéité vers une colonne montante, ledit sorbant est transporté de manière sensiblement verticale dans une deuxième boucle d'étanchéité et traverse un tuyau sensiblement en forme de S, ledit sorbant étant transporté de manière sensiblement verticale hors de ladite deuxième boucle d'étanchéité et ensuite dans ledit premier réacteur. De plus, la présente invention concerne un système pour la production en continu d'hydrogène gazeux et simultanément la séparation d'au moins un composant produit gazeux, ledit système comprenant au moins deux réacteurs à lit fluidisé et au moins deux boucles d'étanchéité et une colonne montante.
PCT/NO2008/000004 2007-01-05 2008-01-07 Production d'hydrogène Ceased WO2008082312A1 (fr)

Applications Claiming Priority (2)

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US87868807P 2007-01-05 2007-01-05
US60/878,688 2007-01-05

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Cited By (18)

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WO2012064712A1 (fr) * 2010-11-08 2012-05-18 The Ohio State University Lit fluidisé circulant comprenant des goulottes de lit mobiles et une séparation étanche aux gaz entre les réacteurs
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
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
CN110803680A (zh) * 2019-12-16 2020-02-18 广东工业大学 一种循环回收反应副产物的化学链重整制氢的装置
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
US12134560B2 (en) 2019-01-17 2024-11-05 Ohio State Innovation Foundation Systems, methods and materials for stable phase syngas generation
US12161969B2 (en) 2019-09-03 2024-12-10 Ohio State Innovation Foundation Redox reaction facilitated carbon dioxide capture from flue gas and conversion to carbon monoxide
US12350651B2 (en) 2019-08-19 2025-07-08 Ohio State Innovation Foundation Mesoporous support-immobilized metal oxide-based nanoparticles

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WO1993017958A1 (fr) * 1992-03-06 1993-09-16 Commonwealth Scientific And Industrial Research Organisation Procede pour fabriquer un produit gazeux

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