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US20110048296A1 - Process for using a facility for combusting carbonaceous materials - Google Patents

Process for using a facility for combusting carbonaceous materials Download PDF

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Publication number
US20110048296A1
US20110048296A1 US12/936,767 US93676709A US2011048296A1 US 20110048296 A1 US20110048296 A1 US 20110048296A1 US 93676709 A US93676709 A US 93676709A US 2011048296 A1 US2011048296 A1 US 2011048296A1
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Prior art keywords
reactor
oxides
oxide
facility
oxygen
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Abandoned
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US12/936,767
Inventor
Laurent MAGHDISSIAN
Jean-Claude Semedard
Antony Piton
Corinne Beal
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GE Vernova GmbH
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Alstom Technology AG
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Filing date
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Publication of US20110048296A1 publication Critical patent/US20110048296A1/en
Assigned to ALSTOM TECHNOLOY, LTD. reassignment ALSTOM TECHNOLOY, LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BEAL, CORINNE, MAGHDISSIAN, LAURENT, PITON, ANTHONY, SEMEDARD, JEAN-CLAUDE
Assigned to ALSTOM TECHNOLOGY LTD reassignment ALSTOM TECHNOLOGY LTD CORRECTIVE ASSIGNMENT TO CORRECT THE ASSIGNEE NAME AND STREET ADDRESS PREVIOUSLY RECORDED ON REEL 026277 FRAME 0387. ASSIGNOR(S) HEREBY CONFIRMS THE FROM "ALSTOM TECHNOLOY, LTD." TO "ALSTOM TECHNOLOGY LTD" AND FROM "BROWN SOVERI STASSE 7" TO "BROWN BOVERI STRASSE 7". Assignors: BEAL, CORINNE, MAGHDISSIAN, LAURENT, PITON, ANTHONY, SEMEDARD, JEAN-CLAUDE
Abandoned legal-status Critical Current

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    • 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
    • F23C10/002—Fluidised bed combustion apparatus for pulverulent solid fuel
    • 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
    • C01B3/344—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 non-catalytic solid particles
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation step
    • 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 
    • F23C2206/00—Fluidised bed combustion
    • 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

  • the invention relates to a process for using a facility for burning carbonaceous materials, in order to produce electricity and/or steam.
  • the carbonaceous materials can be fossil fuels such as coal, for example, waste or biomass, and they are injected into a combustion chamber, for example a fluidized bed combustion chamber.
  • Such a facility for burning carbonaceous materials is described in patent document FR 2 850 156.
  • This facility includes a reactor for reducing oxides, a first cyclone, a reactor for oxidizing oxides, a second cyclone, exchangers for controlling the temperature of the circulating oxides and exchangers for flue gas heat recovery.
  • the facility circulate oxides which are reduced and then oxidized in the two reactors.
  • the solid fuel material is grounded before entering the oxide reduction reactor, and in the case of coal the average particle diameter is less than 500 ⁇ m.
  • the oxides are reduced by having them in contact with the fuel which reacts with the oxygen released by the oxides and are then oxidized by contact with air which regenerates the oxides.
  • the oxides have a particle size range from 50 to 500 ⁇ m and a density from 2000 to 7000 kg/m 3 .
  • This type of facility for combustion of carbonaceous solid materials assures, because of the simplicity and the compactness of this system, reduced costs of capturing carbon dioxide while providing production of steam for generating electricity.
  • the solid particles at the outlet of the first cyclone associated with the reduction reactor consisting of oxides particles and of carbonaceous residues, pass through a seal pot and are then directed towards a device for removing the carbonaceous residues.
  • This removal device is fluidized by steam. With this fluidization, the fine and light particles such as the carbonaceous residues may be separated and re-introduced into the reduction reactor, while the denser and larger oxide particles are transferred towards the oxidation reactor.
  • This removal device is a separator forming a carbon barrier in the facility, essential for capturing carbon dioxide which is a greenhouse gas which should be subjected to emission restrictions.
  • said chemical loopings rely on providing oxygen in solid form by oxides which are oxygen carrier, in order to convert a fuel which can be a gas or a solid fuel. They can be used for combustion with solid, gaseous or liquid fuels or for gasification for production of hydrogen or synthetic gas.
  • reaction of conversion of the fuel can be endothermic.
  • MeO being oxide, for example metal oxide.
  • the temperature of the reactor In order to avoid the stop of the reaction, the temperature of the reactor must be maintained at a certain level.
  • the current way to control the temperature is to introduce in the reactor for oxides reduction solids coming from the reactor for oxides oxidation which is operating at a higher temperature or to add some inert solids mixed within the oxygen carrier if the quantity of oxides which can be injected is limited, as in gasification case, and thus provide the required heat.
  • the object of the invention is to improve such facility in order that the temperature is controlled without necessity of facility with great size.
  • the invention relates to a process for using a facility comprising a first reactor for reducing oxides in which enter a fuel material and metal oxide for providing a reaction of combustion of the fuel material, the first reactor being connected to a second reactor for oxidizing oxide.
  • additional oxygen in a gaseous form is injected into the said first reactor for reducing oxide and the additional oxygen quantity is comprised between 10 and 30% relatively to stoichiometric oxygen for full fuel material combustion.
  • the required solid flow is reduced thanks that part of the carbonaceous material is oxidized by gaseous oxygen in an exothermic reaction. It leads to a smaller reactor.
  • the invention assures an increasing of the residence time of fuel inside the reactor and thus a better carbon conversion rate.
  • the said additional oxygen quantity is controlled, in order to control the temperature of the said first reactor for reducing oxide.
  • a short term response back up can be made by additional oxygen providing quickly heat to recover the required temperature.
  • the additional oxygen is mixed with a media of fluidization before entering the said first reactor for reducing oxide.
  • Fuel material can be coal.
  • Said media of fluidization can be steam and eventually recycled flue gas.
  • FIGURE which only illustrates a preferred embodiment of the invention.
  • FIG. 1 is a schematic view of a facility used in the process according to the invention.
  • a facility for combusting carbonaceous solid materials, in order to produce electricity and/or steam, in which circulates at least one oxide, preferably a mixture of oxides, advantageously metal oxides, which is reduced and then oxidized includes a first reactor 1 for reducing oxides in which enter a fuel material E 1 , for example grounded coal, and oxides E 2 , a first separation cyclone 20 fed with entrained solids from this reactor 1 for reducing oxides, a carbon separator 3 installed at the outlet of this first cyclone 20 in order to send the carbonaceous particles into the reactor 1 for reducing oxides and the oxides E 2 into a second reactor 4 for oxidizing oxides fluidized by air 13 and a second separation cyclone 5 fed with entrained solids from the reactor 1 for oxidizing oxides.
  • a first reactor 1 for reducing oxides in which enter a fuel material E 1 , for example grounded coal, and oxides E 2
  • the facility comprises two back pass 11 , 12 , containing recovery exchangers for the flue gases and for the air, each being dedicated to one of the reactors 1 , 4 .
  • the reactor 1 for reducing oxides is fluidized by a mixture A 1 of steam and recycled flue gas.
  • the separation of the carbonaceous residues from the metal oxides is obtained conventionally by the arrangement of cyclone 20 , seal pot 8 and finally solid separator 3 .
  • the solid oxides particles extracted from the bottom of the second cyclone 5 enter a seal pot 9 from which a first portion is transferred to the bottom of the second reactor 4 for oxidizing oxides, a second portion is re-circulated to the bottom of the first reactor 1 for reducing oxides and a third portion is sent to an external bed 7 fluidized by air where heat exchangers are implemented, and finally sent to the second reactor 4 for oxidizing oxides.
  • This facility is of the type of the known facility described in patent document FR 2 850 156.
  • Additional oxygen O in a gaseous form is injected into the first reactor 1 for reducing oxide and the material E 2 quantity entering into the first reactor 1 for reducing oxide is controlled, in order to obtain a reaction of conversion of the fuel material in thermal equilibrium.
  • the additional oxygen O quantity is comprised between about 10 and 30% relatively to stoichiometric oxygen for full fuel material E 1 combustion.
  • This oxygen quantity depends on the used oxides and their enthalpy of reaction, transport capacity and heat capacity.
  • the additional oxygen O quantity is equal to about 10% relatively to stoechiometric oxygen.
  • the heat quantity is obtained by means of additional oxygen O by chemical reaction
  • the flow of oxides can be divided by 1.5 to 2, by means of the invention.
  • the oxide material can contain inert products for supporting oxides.
  • the required air separation unit for production of oxygen can be 20% of the size in comparison with a conventional air separation unit in a reactor functioning with only oxygen in a gaseous form. It depends of the rate of additional oxygen injected in a gaseous form. The energy penalty due to the air separation unit is decreased by 5.
  • Additional oxygen O is mixed with the media of fluidization, which is a mixture A 1 of steam and recycled flue gas, before entering the first reactor 1 for reducing oxide. Additional oxygen O is introduced into a wind box 1 A of the first reactor 1 for reducing oxide.
  • the oxygen O can be provided with a dedicated oxygen production or by a mixture containing oxygen in gaseous form.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Air Supply (AREA)

Abstract

A process for using a facility having a first reactor (1) for reducing oxide in which enter a fuel material E1) and metal oxide for providing a reaction of combustion of the fuel material (E1), the first reactor (1) being connected to a second reactor (4) for oxidizing oxide, where the process includes additional oxygen (O) in a gaseous form being injected into the first reactor (1) for reducing oxide and in that the additional oxygen (O) quantity is comprised between 10 and 30% relatively to stoichiometric oxygen for full fuel material (E1) combustion.

Description

  • The invention relates to a process for using a facility for burning carbonaceous materials, in order to produce electricity and/or steam. The carbonaceous materials can be fossil fuels such as coal, for example, waste or biomass, and they are injected into a combustion chamber, for example a fluidized bed combustion chamber.
  • Such a facility for burning carbonaceous materials is described in patent document FR 2 850 156. This facility includes a reactor for reducing oxides, a first cyclone, a reactor for oxidizing oxides, a second cyclone, exchangers for controlling the temperature of the circulating oxides and exchangers for flue gas heat recovery. In the facility circulate oxides which are reduced and then oxidized in the two reactors. According to this prior art, the solid fuel material is grounded before entering the oxide reduction reactor, and in the case of coal the average particle diameter is less than 500 μm. The oxides are reduced by having them in contact with the fuel which reacts with the oxygen released by the oxides and are then oxidized by contact with air which regenerates the oxides. The oxides have a particle size range from 50 to 500 μm and a density from 2000 to 7000 kg/m3.
  • This type of facility for combustion of carbonaceous solid materials assures, because of the simplicity and the compactness of this system, reduced costs of capturing carbon dioxide while providing production of steam for generating electricity.
  • The solid particles at the outlet of the first cyclone associated with the reduction reactor, consisting of oxides particles and of carbonaceous residues, pass through a seal pot and are then directed towards a device for removing the carbonaceous residues. This removal device is fluidized by steam. With this fluidization, the fine and light particles such as the carbonaceous residues may be separated and re-introduced into the reduction reactor, while the denser and larger oxide particles are transferred towards the oxidation reactor.
  • This removal device is a separator forming a carbon barrier in the facility, essential for capturing carbon dioxide which is a greenhouse gas which should be subjected to emission restrictions.
  • More generally, such facilities, said chemical loopings, rely on providing oxygen in solid form by oxides which are oxygen carrier, in order to convert a fuel which can be a gas or a solid fuel. They can be used for combustion with solid, gaseous or liquid fuels or for gasification for production of hydrogen or synthetic gas.
  • In case of combustion, the reaction of conversion of the fuel can be endothermic.
  • The chemical reaction is 2MeO+C→2Me+CO2
  • MeO being oxide, for example metal oxide.
  • In order to avoid the stop of the reaction, the temperature of the reactor must be maintained at a certain level.
  • The current way to control the temperature is to introduce in the reactor for oxides reduction solids coming from the reactor for oxides oxidation which is operating at a higher temperature or to add some inert solids mixed within the oxygen carrier if the quantity of oxides which can be injected is limited, as in gasification case, and thus provide the required heat.
  • The technical problem of these two solutions is that the solid flow is such high that it increases by the way the size of the facility.
  • The object of the invention is to improve such facility in order that the temperature is controlled without necessity of facility with great size.
  • To do this, the invention relates to a process for using a facility comprising a first reactor for reducing oxides in which enter a fuel material and metal oxide for providing a reaction of combustion of the fuel material, the first reactor being connected to a second reactor for oxidizing oxide.
  • According to the invention, additional oxygen in a gaseous form is injected into the said first reactor for reducing oxide and the additional oxygen quantity is comprised between 10 and 30% relatively to stoichiometric oxygen for full fuel material combustion.
  • By means of the invention, the required solid flow is reduced thanks that part of the carbonaceous material is oxidized by gaseous oxygen in an exothermic reaction. It leads to a smaller reactor.
  • The invention assures an increasing of the residence time of fuel inside the reactor and thus a better carbon conversion rate.
  • According to a preferred embodiment, the said additional oxygen quantity is controlled, in order to control the temperature of the said first reactor for reducing oxide.
  • A short term response back up can be made by additional oxygen providing quickly heat to recover the required temperature.
  • Preferably, the additional oxygen is mixed with a media of fluidization before entering the said first reactor for reducing oxide.
  • Fuel material can be coal.
  • Said media of fluidization can be steam and eventually recycled flue gas.
  • The invention is described hereafter in more details with FIGURE which only illustrates a preferred embodiment of the invention.
  • The FIG. 1 is a schematic view of a facility used in the process according to the invention.
    •
  • As shown on FIG. 1, a facility for combusting carbonaceous solid materials, in order to produce electricity and/or steam, in which circulates at least one oxide, preferably a mixture of oxides, advantageously metal oxides, which is reduced and then oxidized, includes a first reactor 1 for reducing oxides in which enter a fuel material E1, for example grounded coal, and oxides E2, a first separation cyclone 20 fed with entrained solids from this reactor 1 for reducing oxides, a carbon separator 3 installed at the outlet of this first cyclone 20 in order to send the carbonaceous particles into the reactor 1 for reducing oxides and the oxides E2 into a second reactor 4 for oxidizing oxides fluidized by air 13 and a second separation cyclone 5 fed with entrained solids from the reactor 1 for oxidizing oxides. The facility comprises two back pass 11,12, containing recovery exchangers for the flue gases and for the air, each being dedicated to one of the reactors 1,4. The reactor 1 for reducing oxides is fluidized by a mixture A1 of steam and recycled flue gas.
  • The separation of the carbonaceous residues from the metal oxides is obtained conventionally by the arrangement of cyclone 20, seal pot 8 and finally solid separator 3.
  • The solid oxides particles extracted from the bottom of the second cyclone 5 enter a seal pot 9 from which a first portion is transferred to the bottom of the second reactor 4 for oxidizing oxides, a second portion is re-circulated to the bottom of the first reactor 1 for reducing oxides and a third portion is sent to an external bed 7 fluidized by air where heat exchangers are implemented, and finally sent to the second reactor 4 for oxidizing oxides.
  • This facility is of the type of the known facility described in patent document FR 2 850 156.
  • Additional oxygen O in a gaseous form is injected into the first reactor 1 for reducing oxide and the material E2 quantity entering into the first reactor 1 for reducing oxide is controlled, in order to obtain a reaction of conversion of the fuel material in thermal equilibrium.
  • The additional oxygen O quantity is comprised between about 10 and 30% relatively to stoichiometric oxygen for full fuel material E1 combustion.
  • This oxygen quantity depends on the used oxides and their enthalpy of reaction, transport capacity and heat capacity.
  • For example, if ilmenite FeTiO3 is used, it has been calculated that the additional oxygen O quantity is equal to about 10% relatively to stoechiometric oxygen.
  • The chemical reaction

  • 2MeO+C→Me+CO2
  • is endothermic and needs a providing of heat. Instead of providing the total amount of oxygen by the oxides and consequently using a great quantity of oxides and a reactor with a great size, the heat quantity is obtained by means of additional oxygen O by chemical reaction

  • C+O2→CO2
  • which is exothermic.
  • The flow of oxides can be divided by 1.5 to 2, by means of the invention.
  • The oxide material can contain inert products for supporting oxides. The required air separation unit for production of oxygen can be 20% of the size in comparison with a conventional air separation unit in a reactor functioning with only oxygen in a gaseous form. It depends of the rate of additional oxygen injected in a gaseous form. The energy penalty due to the air separation unit is decreased by 5.
  • Additional oxygen O is mixed with the media of fluidization, which is a mixture A1 of steam and recycled flue gas, before entering the first reactor 1 for reducing oxide. Additional oxygen O is introduced into a wind box 1A of the first reactor 1 for reducing oxide.
  • The oxygen O can be provided with a dedicated oxygen production or by a mixture containing oxygen in gaseous form.

Claims (4)

1. Process for using a facility having a first reactor for reducing oxide in which enter a fuel material and metal oxide for providing a reaction of combustion of the fuel material, the first reactor being connected to a second reactor for oxidizing oxide, said process comprising the steps of:
injecting additional oxygen (O) in a gaseous form into the said first reactor for reducing oxide wherein the additional oxygen quantity is between 10 and 30% relatively to stoichiometric oxygen for full fuel material combustion.
2. Process according to claim 1, wherein the additional oxygen is mixed with a media of fluidization before entering the said first reactor for reducing oxide.
3. Process according claim 1, wherein said fuel material is coal.
4. Process according to claim 2, wherein said media of fluidization is steam and recycled flue gas.
US12/936,767 2008-05-23 2009-05-15 Process for using a facility for combusting carbonaceous materials Abandoned US20110048296A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP08305194.6 2008-05-23
EP08305194A EP2123978A1 (en) 2008-05-23 2008-05-23 Process for using a facility for combusting carbonaceous materials and relating facility
PCT/EP2009/055935 WO2009141281A1 (en) 2008-05-23 2009-05-15 Process for using a facility for combusting carbonaceous materials

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US (1) US20110048296A1 (en)
EP (1) EP2123978A1 (en)
JP (1) JP2011521197A (en)
CN (2) CN102037280A (en)
AU (1) AU2009249749B2 (en)
CA (1) CA2721101C (en)
WO (1) WO2009141281A1 (en)

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WO2013062800A1 (en) * 2011-10-26 2013-05-02 Rentech, Inc. Gasifier fluidization
WO2013062801A1 (en) * 2011-10-26 2013-05-02 Rentech, Inc. Seal pot design
US20140065559A1 (en) * 2012-09-06 2014-03-06 Alstom Technology Ltd. Pressurized oxy-combustion power boiler and power plant and method of operating the same
US20140295359A1 (en) * 2011-09-20 2014-10-02 Thierry Gauthier Chemical-looping combustion method with ashes and fines removal in the reduction zone and plant using same
US9765961B2 (en) 2015-03-17 2017-09-19 Saudi Arabian Oil Company Chemical looping combustion process with multiple fuel reaction zones and gravity feed of oxidized particles
US10006632B2 (en) 2012-03-30 2018-06-26 General Electric Technology Gmbh Methods and apparatus for oxidation of unburnts
US10222060B2 (en) * 2016-02-16 2019-03-05 Thermochem Recovery International, Inc. Two-stage energy-integrated product gas generation system and method
US10766059B2 (en) 2016-03-25 2020-09-08 Thermochem Recovery International, Inc. System and method for recovering inert feedstock contaminants from municipal solid waste during gasification
US10800655B2 (en) 2011-09-27 2020-10-13 Thermochem Recovery International, Inc. Conditioned syngas composition, method of making same and method of processing same to produce fuels and/or fischer-tropsch products
US11370982B2 (en) 2016-08-30 2022-06-28 Thermochem Recovery International, Inc. Method of producing liquid fuel from carbonaceous feedstock through gasification and recycling of downstream products
US12187969B2 (en) 2020-03-10 2025-01-07 Thermochem Recovery International, Inc. System and method for liquid fuel production from carbonaceous materials using recycled conditioned syngas

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Cited By (20)

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US20140295359A1 (en) * 2011-09-20 2014-10-02 Thierry Gauthier Chemical-looping combustion method with ashes and fines removal in the reduction zone and plant using same
US9726369B2 (en) * 2011-09-20 2017-08-08 Total Sa Chemical-looping combustion method with ashes and fines removal in the reduction zone and plant using same
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US11760631B2 (en) 2011-09-27 2023-09-19 Thermochem Recovery International, Inc. Method of producing a cooled syngas of improved quality
US11186483B2 (en) 2011-09-27 2021-11-30 Thermochem Recovery International, Inc. Method of producing sulfur-depleted syngas
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JP2011521197A (en) 2011-07-21
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EP2123978A1 (en) 2009-11-25
WO2009141281A1 (en) 2009-11-26
CN104006383A (en) 2014-08-27
AU2009249749A1 (en) 2009-11-26
CA2721101C (en) 2016-03-29
AU2009249749B2 (en) 2015-01-22

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