WO2011151535A2 - Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede - Google Patents
Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede Download PDFInfo
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- WO2011151535A2 WO2011151535A2 PCT/FR2011/000308 FR2011000308W WO2011151535A2 WO 2011151535 A2 WO2011151535 A2 WO 2011151535A2 FR 2011000308 W FR2011000308 W FR 2011000308W WO 2011151535 A2 WO2011151535 A2 WO 2011151535A2
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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
- F23C10/01—Fluidised bed combustion apparatus in a fluidised bed of catalytic particles
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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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
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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
- 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
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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
- 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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/725—Redox processes
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- 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
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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
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
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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
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
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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
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
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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
- F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
- F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/0084—Stationary elements inside the bed, e.g. baffles
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1606—Combustion processes
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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
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/40—Intercepting solids by cyclones
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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
- 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 field of the invention is that of chemical loop combustion (CLC) for producing energy, synthesis gas and / or hydrogen.
- CLC chemical loop combustion
- a chemical loop combustion process generally comprises one or more reaction zones in which the combustion of a fuel is carried out by contact with an oxygen carrier solid which is then reoxidized in at least one oxidation zone by contacting. with air or water vapor before being returned to the zone (s) of combustion (or reduction).
- the chemical loop combustion thus consists in bringing into contact in a high-temperature chamber a gaseous, liquid and / or solid hydrocarbon feedstock with an oxygen-carrying metal oxide solid.
- the metal oxide gives up some of the oxygen it contains, the latter participating in the combustion of hydrocarbons.
- the fumes mainly contain carbon oxides, water and possibly hydrogen. Indeed, it is not necessary to put the hydrocarbon feedstock in contact with air and the fumes are therefore mainly composed of combustion gases and possibly a dilution gas used for transporting and fluidizing the particles (for example water vapor).
- metal oxides are generally contained either in ore particles or in particles resulting from industrial treatment (residues of the iron or steel industry, used catalysts of the chemical industry or refining). Synthetic materials may also be used, such as, for example, alumina or silica-alumina supports, on which oxidizable metals will have been deposited (nickel oxide, for example).
- the maximum oxygen capacity actually available varies considerably from one oxide to another, and is generally between 0.1 and 15%, and often between 0.3 and 6% by weight.
- the Implementation in a fluidized bed is therefore particularly advantageous for conducting the combustion.
- the finely divided oxide particles circulate more easily in the combustion and oxidation reaction chambers, as well as between these enclosures, if the particles are given the properties of a fluid.
- the patent application FR 2,850,156 describes a chemical loop combustion process for which the fuel is ground before entering the reduction reactor operating in a circulating fluidized bed.
- the small size of the solid fuel particles allows more complete and faster combustion and allows almost 100% fly ash to be produced which is separated from the circulating oxides.
- the downstream separation of the circulating bed is first provided by a cyclone and then by a device for separating the unburnt particles from the metal oxide particles. The entrainment of unburnt in the oxidation zone and thus the CO 2 emissions in the effluents of the oxidation reactor is thus avoided.
- the separation device comprises a fluidized bed with water vapor, which separates the fine and light particles such as the carbonaceous residue and reintroduce the latter into the reactor, while the denser and larger particles of oxides are transferred to the oxidation reactor.
- This device is relatively sophisticated equipment since it contains two internal compartments.
- the fly ash is separated from the oxide particles in a second circuit where a separator operating in a fluidized bed operates the separation, the fluidized fly ash being sent to a silo via a pneumatic transport and the oxides metal being extracted at the base of the fluidized bed reactor after settling.
- the high gas velocities employed in the reduction reactor operating in a circulating fluidized bed do not make it possible to obtain sufficient residence times for the particles to gasify all the solid fuel and then to operate the combustion of the gasification products. .
- a large recycling of the unburnt particles, by passage through the separator, is therefore necessary.
- the unburnt separation of the oxide particles is delicate because it requires the addition of additional gas in large quantities, which is expensive in energy.
- This device consists of an oxidation reactor using metal particles, a cyclone allowing the separation of particles and depleted air after oxidation, a fluidized bed supplied with oxidized metal oxides by the leg of return located under the cyclone, in which the reduction of the metal oxide by burning coal.
- the coal is fed into the upper part of the fluidized bed in the dilute phase.
- the combustion of the coal takes place progressively: the coal particles begin to descend and devolatilize in the dilute phase, in countercurrent of the fluidization gases, and in which the metal oxides are present only in small quantities; then they come into contact with the dense phase fluidized metal oxides.
- the high residence time makes it possible to gasify the coal and to produce combustion gases containing large amounts of carbon monoxide and hydrogen which pass into the dilute phase.
- the fluidization rates are low - generally between 5 and 30 cm / s - which does not allow the entrainment of significant amounts of metal oxides in the dilute phase which could promote the combustion of gas such as CO, H 2 or volatile hydrocarbons that are removed from the diluted zone.
- the amounts of CO and hydrocarbons (HC) in the effluents of the reduction reactor are large and greater than several percent by volume. The combustion efficiency is therefore not very good and an afterburner zone is also necessary to finish the combustion.
- the reduction reactor is equipped with a particle separator integrated in the dense phase which requires the addition of additional gas to effect the separation.
- Applicants have developed an improved chemical loop combustion process that allows, even from coarse fuel particles, to achieve total combustion of the solid charge by minimizing the amount of solid charge to recycle. which maximizes the energy efficiency of the process.
- the combustion process according to the invention makes it possible to capture at least 90% of the CO 2 emitted by the combustion in the flue gases directly at the outlet of the combustion reactor, the capture rate being defined by the ratio:
- the CO / CO 2 molar ratio of the fumes downstream of the cyclones is less than 0.05 and the H 2 / H 2 O ratio is less than 0.05.
- the contact between the particles transporting oxygen and the solid fuel is optimized to promote coal gasification reactions, and on the other hand, the contact between gasification products and metal oxides is also optimized to produce fully flared (H 2 , CO and HC ⁇ 1% vol smoke in flue gas) effluents.
- the separation of the unburnt particles from the metal oxide particles is carried out upstream of the flue gas dedusting step of the reduction reactor in order to best utilize the maximum kinetic energy of the fumes for the separation of the two types of particles.
- the present invention relates to a method of combustion of a solid charge in a chemical loop in which an oxygen-carrying material circulates, said method comprising at least:
- the admission of the mixture of particles to be separated in the separation zone can be carried out in a dilute phase of the fluidized bed that comprises this zone.
- the solid feed may be selected from coal, coke, petcoke, biomass, oil sands, and household waste.
- the average residence time of the solid phase in the reaction zone may be between 0.25 and 20 minutes and the superficial gas velocity between 0.3 and 3 m / s.
- the average residence time of the gas in the second zone can be between 1 and 20 seconds and the average residence time of the solids between 2 seconds and 1 minute, and in which the void rate in the zone is greater than 0.9.
- a gaseous flow rate imposed can be induced at least 80% by the gaseous effluent containing the particles from the second zone.
- the superficial gas velocity in the dilute phase of the separation zone can be set to a value between 30 and 300% of the average terminal rate of drop of the oxygen carrier particles.
- the superficial gas velocity in the dilute phase of the separation zone can be set to a value between 50 and 150% of the average terminal rate of drop of the oxygen carrier particles.
- the gas stream containing the light particles and a fraction of oxygen carrier particles is sent to at least one gas-solid separation stage in order to recover substantially all the particles contained in the gas stream. from the separation zone and then recycled to the reaction zone.
- the separator enclosure may be powered by a gas from an external source.
- the invention also relates to an installation for carrying out the combustion of a solid charge, said installation comprising at least:
- a first reaction zone comprising a supply of solid fuel, a fluidization gas and oxygen carrier particles
- a second reaction zone receiving by a feed the combustion gases containing particles originating from the first reaction zone, - a separation zone receiving by its admission a gaseous effluent of the second zone and containing ash, oxygen carrier particles and unburnt particles;
- an oxidation zone supplied with oxygen carrier particles by the separation zone and in air.
- the second reaction zone may comprise a fresh oxygen carrier feed.
- the second reaction zone may comprise an oxygen supply.
- the separation zone may comprise an enclosure with at least one intake pipe of said mixture, an exhaust pipe situated in the lower part of the enclosure and an outlet pipe situated at the upper part of the device, the intake and discharge / outlet being chosen to create in the enclosure a dense phase in the lower part and a diluted phase in the upper part, and wherein said intake duct opens into the dilute phase.
- the separator enclosure may further include a supply line for a gas from an external source.
- the passage section of the second reaction zone may be smaller than the passage section of the reaction zone.
- At least one gas-solid separation stage may be provided to recover the particles contained in the gas stream from the separation zone and recycle them via a pipe to the first reaction zone.
- the plant may comprise two gas-solid separation stages in which one of the separation stages is fed with a gas stream containing particles from the other of the separation stages.
- At least one chamber containing a fluidized bed for separating the light particles remaining among the unburnt particles may be present on the pipes.
- FIG. 1 describes the general principle of the invention
- FIG. 2 describes a particular implementation of the reaction zones (R1), (R2) and the separation zone (S3),
- FIG. 3 represents a possible configuration of the connection between the second reaction zone (R2) and the separation zone (S3),
- the reaction zone or reactor (R1) is supplied with fuel, in this case a solid fuel, via a pipe (1).
- the solid fuel can be introduced through a conduit which is penetrating inside the reactor.
- the flow of the solid fuel particles is either continuous or intermittent with an injection frequency corresponding to a period equal to at least half the mean residence time of all the solid fuel particles in the reaction zone ( R1).
- the solid fuel is injected into the reaction zone (R1), in which it undergoes a devolatilization of the volatile compounds, which generally represent from 5 to 50% by weight of the solid fuel according to its origin, in contact with the oxygen carrier particles. from an oxidation zone (R4) and fed via a pipe (3).
- the reaction zone (R1) is also fed with a fluidization gas supplied via a pipe (2).
- the fluidization means (not shown) are well known to those skilled in the art and are, for example, flat or frustoconical distribution grids, dispensing rings or "spargers".
- the injected fluidization gas is preferably water vapor, or optionally a mixture of water vapor and CO 2 .
- the temperature in the reaction zone (R1) is substantially homogeneous in view of the fluidization conditions leading to the formation of a dense phase. The temperature is preferably greater than 800 ° C and preferably between 900 and 1000 ° C, so as to minimize the time required to gasify the solid fuel.
- reaction zone (R1) metal oxide particles and an unburned solid fuel fraction, together with the combustion gases containing water vapor, nitrogen, carbon dioxide, are discharged through a pipe (4). hydrogen, CO and / or CO 2 or a mixture of these gases.
- the conduit (4) transfers the gaseous mixture containing the particles to a second reaction zone (R2).
- the duct (4) is preferably a duct of variable section so as to join the reaction zones (R1) and (R2).
- a pipe (5) also makes it possible to extract, in the lower part of the reaction zone (R1), the ashes formed and agglomerated together in the reactor as well as, optionally, oxygen carrier particles and unburnt particles. .
- the second reaction zone (R2) ensures the combustion of the gaseous mixture from the reaction zone (R1).
- the gaseous effluent containing particles is extracted via a pipe (8) to be sent to a separation zone (S3) in which there is a rapid separation between the particles the lightest - mostly unburnt particles and possibly fly ash and metal oxide fines - extracted via a pipe (10) with the gas, and the heaviest particles - mostly metal oxide particles - extracted in the lower part of the separation zone (S3) by a conduit (13) supplying an enclosure (F4) acting as a buffer zone.
- the buffer zone (F4) may be materialized by a concentric fluidized bed and peripheral to the second reaction zone (2), the fluidization being obtained by injection of a gas brought by a pipe (14).
- the latter participates in the separation in the separation zone (S3) by being channeled to it by a pipe (17).
- heat exchange means (16) which may be tubes in the wall or in the fluidized bed making it possible to recover a variable part generally representing from 5 to 60% of the heat produced in the chemical loop combustion process.
- a conduit (15) is used to draw oxygen carrier particles from the buffer zone to an oxidation zone (R4) to reoxidize them.
- This gas may contain oxygen or an oxidizing gas to continue the combustion reactions of CO and hydrogen in the separator (S3).
- a part of the decanted heavy particles (mainly oxygen carrier particles) is extracted via a pipe (11) to be recycled to the reaction zone (R1). It is thus possible to promote the homogeneity of temperature in the reaction zones (R1), (R2) and in the separation zone (S3).
- a pipe (10) conveys the gas stream containing the lightest particles - mainly unburnt particles and possibly fly ash - and a minor fraction of carrier particles.
- gas-solid separation stage here two gas-solid separation stages (S5, S6), cyclones for example, which make it possible to recover almost all the particles contained in the gaseous flow of the pipe (10 ) and which are then recycled to the reaction zone (R1) respectively by the pipes (19) and (20), after possible removal of the fly ash by fluidized bed elutriation, for example.
- S5, S6 gas-solid separation stages
- R1 reaction zone
- the gas stream is extracted by a pipe (17) to be sent to the second cyclone (S6) and at the outlet of this cyclone (S6) the substantially particle-free gas is extracted by a pipe (18), the latter no longer containing a particle content generally between 100 mg / m 3 and 1 g / m 3 .
- the method of combustion of a solid charge in a chemical loop in which an oxygen carrier material circulates comprises at least a first reaction zone (R1) operating in a dense fluidized bed and for gasifying the solid charge particles. in the presence of metal oxide particles; a second combustion or reduction reaction zone (R2) preferably operating in a dilute fluidized bed and making it possible to carry out the combustion of the gaseous effluents from the first reaction zone (R1) in the presence of metal oxide particles; a separating zone (S3) separating in a gas-containing mixture, unburnt particles, metal oxide particles, said mixture coming from the second reaction zone (R2), and said zone separation device comprising an enclosure in which the admission of the mixture of particles to be separated is carried out in a dilute phase in which a gas flows at an ascending speed which is imposed; an oxidation zone (R4) of the metal oxide particles for reoxidizing said particles before returning them to the reaction zone (R1).
- R1 operating in a dense fluidized bed and for gasifying the solid charge particles. in the presence
- a dense fluidized bed is understood to mean a fluidized bed in which the gas fraction ⁇ 9 is less than 0.9, preferably less than 0.8.
- Diluted fluidized bed means a fluidized bed in which the volume fraction of the metal oxide particles is less than 10% by volume.
- the reaction zone (R1) is fed with: • solid charge, dry or partially moist, in the form of dry or partially wet particles, with a particle size generally between 100 microns and 10 mm, preferably between 100 and 500 microns.
- the solid filler or fuel is generally selected from coal, coke, petcoke, biomass, oil sands and household waste, and preferably the filler treated is coal.
- Fluidization gas which is generally nitrogen, water vapor and / or recycled CO 2 , and preferably water vapor.
- the gas can participate actively in the gasification of the solid fuel.
- the mean residence time of the solid phase is between 0.25 and 20 minutes, preferably between 2 and 10 minutes.
- the superficial gas velocity is generally between 0.3 and 3 m / s (at the reaction conditions at the outlet of the reaction zone (R1)).
- the concentration of metal oxides in the reaction zone (R1) is at least 10% by volume.
- the temperature is generally between 800 and 1000 ° C., preferably greater than 900 ° C.
- metal oxides are generally contained either in ore particles or in particles resulting from industrial treatments (residues of the iron and steel industry or mining industry, used catalysts of the chemical or refining industry, and may also result from synthetic materials such as, for example, alumina or silica-alumina carriers on which oxidizable metals have been deposited (nickel oxide, for example) .
- the oxygen capacity actually available varies considerably from one oxide to the other , and is generally between 0.1 and 15%, and often between 0.3 and 3% by weight, which makes it particularly advantageous to carry out the combustion in a fluidized bed.
- Oxygen carrier particles are generally much larger in size and density than fly ash and unburnt particles having been in contact with the oxygen carrying particles in the high temperature combustion zone.
- the size of the unburned particles of coal is less than 100 microns and that the majority of the particles have a size of less than 150 microns.
- the density of these particles is generally between 1000 and 1500 kg / m 3 .
- reaction zone (R2) flows the gaseous and solid effluents from the reaction zone (R1), with the exception of a very small fraction of agglomerated ash particles which can be drawn off at the bottom of the reaction zone (R1). reaction zone (R1).
- the passage section of the second reaction zone (R2) is strictly smaller than the passage section of the reaction zone (R1).
- the passage section of the second reaction zone (R2) is at least 25% less than that of the reaction zone (R1) and preferably at least 50%.
- the section change makes it possible to increase the speed between the reaction zones (R1) and (R2) and to ensure the transition between the dense phase and the dilute phase flow.
- the average residence time of the gas in this zone is generally between 1 and 20 seconds, the average residence time of the solids ranging between 2 seconds and 1 minute.
- the reactions are essentially reactions between the gas phase and the solid. These reactions are typically the conversion of CO and H 2 to CO 2 and H 2 O.
- oxygen may be advantageous to inject oxygen into this zone, either in the form of fresh oxygen carrier particles originating from an oxidation zone, or under form of gaseous oxygen. Furthermore, it may also be advantageous to inject a portion of the solid fuel into this second reaction zone, especially if the fuel has a quantity volatile matter. In this way, the gaseous charge in the reaction zone (R1) is limited and consequently the reactor diameter is smaller.
- Certain solid fuels are in fact known to have high volatile contents, for example between 25 and 50%.
- the solid volatiles are devolatilized and can burn rapidly.
- the residue of the nonvolatilized solid fuel (“char") does not have time to react because of the residence time which is too short - and moreover of the short contact time with the oxygen carrier - in this reaction zone. It will be recycled to the reaction zone (R1), after its separation in the separation zone (S3) downstream, the effluent gas from the second reaction zone (R2).
- the second reaction zone (R2) operates in a dilute fluidized bed in which all the solids are transported.
- the residence time of the gaseous phase is generally between 1 and 20 seconds, the flow of solid transported between 25 and 500 kg / s / m 2 , preferably between 60 and 300 kg / s / m 2 .
- the superficial gas velocity is greater than 3 m / s and less than 30 m / s, preferably between 5 and 15 m / s (expressed under conditions), in order to facilitate the transport of all the particles while minimizing pressure drops so as to optimize the energy efficiency of the process.
- the flow is diluted and most of the volume is occupied by the gas.
- the void ratio is generally greater than 90%, or even 95%.
- the particles transported with the gas are of different natures. We distinguish:
- the oxygen carrier particles having yielded at least part of their oxygen during their passage through the reaction zone (R1) or in the second reaction zone (R2);
- the gaseous effluents are sent to the separation zone (S3).
- the separation zone (S3) thus makes it possible to separate the heavy particles from the light particles in the gas mixture coming from the combustion zone (R2).
- the heavy particles consist essentially of the particles of metal oxides to be recycled and the light particles of unburnt particles to be recycled to the reaction zone (R1) and possibly fly ash.
- the superficial velocity of the gas flow is greater than the final decay velocity of the unburned fuel particles to allow their entrainment with the gas.
- rapid separation is meant a separation taking place in less than 1 minute and preferably in less than 20 seconds, this time corresponding to the residence time of the light particles in the dilute phase of the separator.
- the dilute phase generally has a solid content generally less than 5%, or even less than 1% (vol.).
- the separation zone comprises at least one chamber with an intake pipe (8) of said mixture, an evacuation pipe (13) located in the lower part of the enclosure and an outlet pipe (10) located in the upper part of the device, the intake and exhaust / outlet parameters being chosen to create in the chamber a dense phase in the lower part and a diluted phase in the upper part, and wherein said intake pipe opens into the diluted phase.
- the separation is carried out in the dilute phase of the separator so as to obtain the best possible separation efficiency.
- the separation efficiency can be defined by the formula:
- X amount of unburnt particles entrained with the gas / total amount of unburnt particles in the mixture of particles entering the separator.
- a separation efficiency generally greater than 70%, or even greater than 80%, can be obtained.
- the capture rate in C0 2 of the process is defined by the ratio of amount of C0 2 emitted at the combustion zone / total amount of C0 2. issued in the CLC loop.
- the capture rate may be greater than 90%.
- the fact of obtaining a separation efficiency of 80% allows a progress of the gasification reactions in a range of 50 to 70% in the reaction zone (R1) depending on the recycling and the content of the reaction. volatile matter of the charge.
- the gas flow rate imposed is induced entirely by the gaseous effluent containing the particles from the second reaction zone (R2) but it is also possible to adjust the speed by complementary injection of a gas from from an external source, which can also contribute to the fluidization of a dense phase accumulating the sedimented particles.
- the superficial gas velocity in the dilute phase of the separation zone is set at a value generally between 30 and 300% of the mean terminal rate of drop of the oxygen carrier particles, preferably between 50 and 150%, and more preferably between 75 and 125%.
- p s is the density of the particles (kg / m 3 )
- p g is the density of the gas (kg / m 3 )
- the gas stream containing the lighter particles is sent to one or more separation cyclones gas-solid (S5, S6), At the outlet of the cyclone (s), the gaseous flow contains only a particle content generally between 100 mg / m 3 and 1 g / m 3 . Subsequent treatments are possible, such as ultimate dust removal, water condensation, heat recovery, deSOx, deNOx, etc.
- oxygen carrier particles withdrawn directly into the lower part of the separation zone (S3) are sent to an oxidation reaction zone (R4), composed of one or more beds fluidized in parallel or in series supplied with air or with an oxidizing gas such as air or water vapor.
- R4 oxidation reaction zone
- the oxidation zone (R4) operates in a fluidized bed at a temperature generally of between 700 and 1200 ° C., preferably between 950 and 1100 ° C., depending on the flow rate of the metal oxides between the combustion zone and the zone. oxidation and the oxygen transfer capacity of the material.
- Figure 2 shows the main elements of Figure 1 by specifying them.
- a fluidizing gas is introduced by specific means which are perforated plates (24) disposed downstream of a wind box (25) fed by a pipe (2).
- These plates are inclined at an angle generally between 30 and 70 ° relative to the horizontal and leave in the central part a free space to the flow of the particles, which allows to withdraw through the distributor (25) a part of the sedimenting particles in this zone and consist mostly of agglomerated ash.
- the cross section of the reaction zone (R1) is substantially constant and the average superficial velocity in this zone is generally between 0.3 and 3 m / s.
- the degree of vacuum within the reaction zone (R1) is less than 0.9 and preferably between 0.5 and 0.8.
- a cone (4 ') makes it possible to evacuate the gaseous effluents and the particles entrained towards the second reaction zone (R2), consisting of an elongated reactor in which the gases have a higher surface velocity than in the first reaction zone.
- a stream of oxygen carrier particles from an oxidation zone is introduced via a pipe (6).
- this pipe makes it possible to introduce the particles in the axial direction of the second reaction zone.
- Their flow in the pipe (6) is of the fluidized type, preferably in the dense phase. In some cases, it may be advantageous to introduce the particles into the second reaction zone (R2) with a diluted type flow.
- the carrier gas is then selected to favor the conversion of the gas from the reaction zone (R1) and may advantageously contain oxygen.
- the gas containing particles is directed into the dilute phase of the separation zone (S3) through the opening (8 ') located at the top of this second reaction zone (R2 ).
- the velocity is slowed down due to the increase of the separation zone (S3) to allow sedimentation of the heavier particles in the lower part of this zone ( S3) and entrainment of the lightest particles in the upper part of the separation zone.
- a pipe (10) conveys the gas stream containing the lightest particles - mainly unburnt particles and possibly fly ash - and a minor fraction of carrier particles. oxygen to the two stages of gas-solid separation cyclones (S5, S6), which recover almost all the particles contained in the gas stream of the pipe (10) and which are then recycled to the reaction zone (R1 ) respectively by the lines (19) and (26).
- the heavier particles within the fluidized dense phase settle in the annular space between the outer walls of the second reaction zone (R2) and the inner walls of the separation zone (S3). Part of the heavier particles is recycled to the reaction zone (R1) via a pipe (11), the other part being drawn off by a pipe (15) to be sent to the oxidation zone (R4).
- the entrained particles are extracted by a pipe (18) and the untrained particles are extracted by a pipe (20) and directed to an enclosure (F7) containing a fluidized bed allowing a separation more pushing the light particles (ash) remaining among unburnt particles which are then recycled via a pipe (26) to the reaction zone (R1).
- the fluidization is provided by a gas supplied by a pipe (21) and distributed by a distributor (22), the fluidization gas being extracted from the enclosure (F7) with the fly ash particles by a pipe (23).
- the device (F7) can also be located on the line (19) at the output of (S5).
- FIG. 3 shows a type of connection between the second reaction zone (R2) and the separation zone (S3) consisting of a diverging cone (35) at an angle advantageously between 6 and 30 °.
- the minimum speed of the gas leaving the cone (35) is greater than 3 m / s and preferably greater than 5 m / s, so as to achieve satisfactory transport conditions at the outlet of the second reaction zone (R2). In this way, a good distribution of the gas mixture containing particles is ensured over the entire cross section of the separation zone (S3). Thus, the total height of the separation zone (S3) can be limited.
- FIG. 4 shows an insert (36) in the form of a divergent cone that facilitates the distribution of the gaseous mixture containing particles over the entire section of the separation zone (S3).
- a coal-type filler is treated according to the process of the invention as described in FIG.
- the load considered is a medium coal having the properties presented in the table below: composition of dry coal
- the return temperature of the oxygen carrier after passage through the oxidation zone (R4) is 1032 ° C. This results in an average temperature in the reaction (R1-R2) and separation (S3) zones of 940 ° C.
- the average residence time of the metal oxide particles in the reactor is 380 s.
- the progress of the carbon gasification reaction by the steam is 69%.
- the coal gasification reaction is endothermic, the thermal energy to maintain the reaction at 940 ° C is provided both by the stream of oxidized solid leaving the air reactor at 1032 ° C (via line (3)) and by the reaction of the synthesis gas resulting from the gasification of the carbon with the oxygen carrier solid.
- This effluent carries with it (via a pipe (4)) a solid phase composed of 465 kg / s of oxidized solid, 103 kg / s of reduced solid, 0.55 kg / s of ash and 1.18 kg / s unconverted coal (taking into account recycled coal). Reactions in the dilute phase reduction reactor (R2)
- the residence time in this reactor is short and set at 4 seconds for solids, it is considered that this time is not sufficient to substantially react the unreacted coal.
- this zone the solid accompanies the gas phase and this makes it possible to reach the gas phase composition at the outlet of this diluted zone, which follows:
- the separator (S3) is dimensioned and operated so as to obtain a gas flow for which the speed is imposed at 0 m / s. In this way, the separation efficiency obtained is 74% (% unburned solids recovered in the pipe (10) / amount of coal introduced into the reactor).
- the resulting C0 2 capture rate is 90.2%.
- a steam booster via line (9) of 0.79 kg / s is used in the fluidization zone (F4).
- the dimensioning criterion is the circulation of gases whose velocity is 0.75 m / s, the vacuum rate of the dense fluidized bed is 65%.
- the dimensioning criterion is the flow of gases whose velocity is 7.5 m / s, the vacuum rate of the dense fluidized bed is 99%.
- the sizing element is the flow of gases in the upper part, above the mouth from the second reaction zone (R2).
- the superficial gas velocity is set at 1.0 m / s above the mouth of (R2), and 0.1 m / s below, i.e. in the fluidization zone (F4).
- the clearance height above the bed is set equal to the diameter.
- the height below the mouth of the second reaction zone (R2) is 4 m.
- the chemical combustion loop is largely exothermic.
- the temperature is set at 130 ° C, the heat recovery is distributed between the solid and the heat recovery on the fumes as follows:
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Abstract
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Priority Applications (7)
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CN201180026991.5A CN102933902B (zh) | 2010-06-02 | 2011-05-24 | 具有包含气固分离区的反应区的化学回路燃烧方法及使用该方法的设备 |
AU2011260162A AU2011260162B2 (en) | 2010-06-02 | 2011-05-24 | Chemical looping combustion process with a reaction zone incorporating a gas/solid separation zone and plant using such a process |
PL11728309T PL2577162T3 (pl) | 2010-06-02 | 2011-05-24 | Sposób spalania w pętli chemicznej z dwiema kolejnymi strefami reakcji i jedną strefą oddzielania i instalacja wykorzystująca taki sposób |
CA2799133A CA2799133C (fr) | 2010-06-02 | 2011-05-24 | Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede |
US13/701,221 US9927118B2 (en) | 2010-06-02 | 2011-05-24 | Chemical looping combustion method with a reaction zone including a gas-solid separation zone and plant using same |
EP11728309.3A EP2577162B1 (fr) | 2010-06-02 | 2011-05-24 | Procédé de combustion en boucle chimique avec deux zones de réaction successives et une zone de séparation et installation utilisant un tel procédé |
ES11728309T ES2748511T3 (es) | 2010-06-02 | 2011-05-24 | Proceso de combustión en bucle químico con dos zonas de reacción sucesivas y una zona de separación e instalación utilizando dicho proceso |
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FR1002325A FR2960940B1 (fr) | 2010-06-02 | 2010-06-02 | Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede |
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EP (1) | EP2577162B1 (fr) |
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FR2850156A1 (fr) | 2003-01-16 | 2004-07-23 | Alstom Switzerland Ltd | Installation de combustion avec recuperation de co2 |
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US7767191B2 (en) * | 2003-12-11 | 2010-08-03 | The Ohio State University | Combustion looping using composite oxygen carriers |
US20070232818A1 (en) * | 2005-11-15 | 2007-10-04 | Domestic Energy Leasing, Llc | Transesterification of oil to form biodiesels |
AT505526B1 (de) * | 2007-08-14 | 2010-09-15 | Univ Wien Tech | Wirbelschichtreaktorsystem |
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FR2936301B1 (fr) * | 2008-09-23 | 2010-09-10 | Inst Francais Du Petrole | Procede et dispositif optimises de combustion par boucle chimique sur des charges hydrocarbonees liquides |
CA2741374A1 (fr) * | 2008-11-04 | 2010-05-14 | Jean-Xavier Morin | Procede d'adaptation a tout type d'oxydes, d'une installation a cycle thermochimique et installation pour la mise en oeuvre de ce procede |
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2010
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2011
- 2011-05-24 US US13/701,221 patent/US9927118B2/en active Active
- 2011-05-24 CN CN201180026991.5A patent/CN102933902B/zh active Active
- 2011-05-24 WO PCT/FR2011/000308 patent/WO2011151535A2/fr active Application Filing
- 2011-05-24 PL PL11728309T patent/PL2577162T3/pl unknown
- 2011-05-24 AU AU2011260162A patent/AU2011260162B2/en not_active Ceased
- 2011-05-24 CA CA2799133A patent/CA2799133C/fr active Active
- 2011-05-24 ES ES11728309T patent/ES2748511T3/es active Active
- 2011-05-24 EP EP11728309.3A patent/EP2577162B1/fr active Active
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FR2850156A1 (fr) | 2003-01-16 | 2004-07-23 | Alstom Switzerland Ltd | Installation de combustion avec recuperation de co2 |
Cited By (15)
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AU2012311411B2 (en) * | 2011-09-20 | 2017-05-25 | IFP Energies Nouvelles | Chemical looping combustion method with removal of ash and fines in the reduction area, and a facility using such a method |
JP2013164235A (ja) * | 2012-02-13 | 2013-08-22 | Tokyo Gas Co Ltd | 窒素製造に適したケミカルループ式燃焼装置とそれを用いた窒素および水素の製造方法 |
WO2017013038A1 (fr) | 2015-07-21 | 2017-01-26 | IFP Energies Nouvelles | Procede et installation clc avec production d'azote de haute purete |
FR3084138A1 (fr) | 2018-07-23 | 2020-01-24 | IFP Energies Nouvelles | Installation clc comportant un separateur solide/solide avec des moyens de dispersion d'un melange gaz-solide |
WO2020020739A1 (fr) | 2018-07-23 | 2020-01-30 | IFP Energies Nouvelles | Installation clc comportant un separateur solide/solide avec des moyens de repartition d'un melange gaz-solide |
US11885488B2 (en) | 2018-07-23 | 2024-01-30 | IFP Energies Nouvelles | CLC facility comprising a solid/solid separator with means for distributing a gas-solid mixture |
FR3086369A1 (fr) | 2018-09-20 | 2020-03-27 | IFP Energies Nouvelles | Dispositif et procede de combustion en boucle chimique avec separateur de particules muni d'une conduite d'admission inclinee |
WO2020058141A1 (fr) | 2018-09-20 | 2020-03-26 | IFP Energies Nouvelles | Dispositif et procede de combustion en boucle chimique avec separateur de particules muni d'une conduite d'admission inclinee |
FR3089828A1 (fr) | 2018-12-17 | 2020-06-19 | IFP Energies Nouvelles | Installation clc comportant un separateur solide/solide integrant une enceinte cyclonique |
FR3089827A1 (fr) | 2018-12-17 | 2020-06-19 | IFP Energies Nouvelles | Réacteur de combustion en boucle chimique à toit plat |
WO2020126704A1 (fr) | 2018-12-17 | 2020-06-25 | IFP Energies Nouvelles | Réacteur de combustion en boucle chimique à toit plat |
WO2020126703A1 (fr) | 2018-12-17 | 2020-06-25 | IFP Energies Nouvelles | Installation clc comportant un separateur solide/solide integrant une enceinte cyclonique |
WO2023001535A1 (fr) | 2021-07-23 | 2023-01-26 | IFP Energies Nouvelles | Procede et installation clc avec recuperation d'oxygene gazeux produit par un porteur d'oxygene |
FR3125441A1 (fr) | 2021-07-23 | 2023-01-27 | IFP Energies Nouvelles | Procédé et installation CLC avec récupération d’oxygène gazeux produit par un porteur d’oxygène |
WO2023110589A1 (fr) | 2021-12-17 | 2023-06-22 | IFP Energies Nouvelles | Installation et procede de combustion en boucle comportant un reacteur air cyclonique |
Also Published As
Publication number | Publication date |
---|---|
FR2960940B1 (fr) | 2015-08-07 |
WO2011151535A3 (fr) | 2012-01-19 |
ES2748511T3 (es) | 2020-03-17 |
CA2799133C (fr) | 2018-04-03 |
AU2011260162A1 (en) | 2013-01-10 |
CN102933902A (zh) | 2013-02-13 |
AU2011260162B2 (en) | 2016-12-01 |
CN102933902B (zh) | 2017-07-14 |
CA2799133A1 (fr) | 2011-12-08 |
FR2960940A1 (fr) | 2011-12-09 |
US9927118B2 (en) | 2018-03-27 |
US20130149650A1 (en) | 2013-06-13 |
EP2577162B1 (fr) | 2019-07-10 |
PL2577162T3 (pl) | 2020-03-31 |
EP2577162A2 (fr) | 2013-04-10 |
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