WO2023110590A1 - Cyclone pour une installation et un procede de combustion en boucle chimique muni d'une conduite d'arrivee a parois inclinees et injection de gaz - Google Patents
Cyclone pour une installation et un procede de combustion en boucle chimique muni d'une conduite d'arrivee a parois inclinees et injection de gaz Download PDFInfo
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- WO2023110590A1 WO2023110590A1 PCT/EP2022/084843 EP2022084843W WO2023110590A1 WO 2023110590 A1 WO2023110590 A1 WO 2023110590A1 EP 2022084843 W EP2022084843 W EP 2022084843W WO 2023110590 A1 WO2023110590 A1 WO 2023110590A1
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- WIPO (PCT)
- Prior art keywords
- cyclone
- particles
- gas
- inlet pipe
- reactor
- Prior art date
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/02—Construction of inlets by which the vortex flow is generated, e.g. tangential admission, the fluid flow being forced to follow a downward path by spirally wound bulkheads, or with slightly downwardly-directed tangential admission
- B04C5/04—Tangential inlets
-
- 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
-
- 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
- C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
-
- 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
- C10J3/466—Entrained flow processes
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
- B04C2009/008—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks with injection or suction of gas or liquid into the cyclone
-
- 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
-
- 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
- C10J2300/094—Char
-
- 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
-
- 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
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1637—Char combustion
-
- 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Definitions
- the present invention relates to the field of gas/solid separation, and more specifically to the field of cyclones, in the context of the chemical loop combustion of hydrocarbon feedstocks to produce energy, synthesis gas and/or hydrogen.
- the present invention deals with the problem of the accumulation of solid particles in processes involving transport of particles through particle transport lines, such as chemical loop redox processes, typically chemical looping combustion (“CLC” for “Chemical Looping Combustion”), implementing multiphase circulating beds comprising a reactive solid in contact with one or more generally gaseous fluid phases.
- chemical loop redox processes typically chemical looping combustion (“CLC” for “Chemical Looping Combustion”)
- CLC chemical looping combustion
- multiphase circulating beds comprising a reactive solid in contact with one or more generally gaseous fluid phases.
- the particles can agglomerate which risks leading to clogging and partial or total blockage of the transmission line; the particles can accumulate temporarily and then be suddenly mobilized again in bunches, which then creates pressure fluctuations and fluctuations in the flow rate of solid transported.
- reaction zone In multiphase circulating bed processes using a reactive solid in contact with one or more gaseous fluid phases, such as CLC processes, a reaction zone is conventionally implemented, generally formed by a substantially vertical reactor with an ascending fluid phase, and a phase separation zone (solid/gas) generally with a substantially vertical axis, formed by a cyclone using centrifugal force to separate the solid particles from the gas phase.
- phase separation zone solid/gas
- gas/solid separators are well known to those skilled in the art.
- transition transport zone typically a pipe
- the length and inclination of which are conditioned by the relative locations of the reaction zone and the zone. of seperation.
- transition zones in which the gas/solid mixture circulates, are substantially horizontal to respect the tangential arrival of the flow in the cyclone. This therefore results in a change of direction, whereby the deceleration of the solid promotes the deposition of particles at the bottom of the pipe, which can generate the phenomena described above.
- the solid standing at high temperature which can be oxygen carrier or ash, can produce a clump of particles that grows larger as other solid particles pass. This agglomeration can in extreme cases block a large part of the cyclone inlet and compromise the pressure balance.
- the present invention aims to overcome the problems of the prior art mentioned above, and thus has the general objective of reducing the deposition of solid particles at the inlet of a cyclone of a CLC installation of a hydrocarbon charge, but also to possibly carry out chemical reactions within the cyclone, as well as to improve the efficiency of the cyclone.
- a cyclone for a chemical loop redox installation of a hydrocarbon feedstock implementing at at least one reactor operating in a circulating fluidized bed comprising:
- an inlet pipe for a gaseous mixture comprising solid particles coming from a reactor of the installation comprising at one end an inlet opening of rectangular section and at its other end an outlet opening of rectangular section,
- a cylindrical-conical chamber comprising a cylindrical upper portion surmounting an inverted frustoconical lower portion, the cylindrical upper portion comprising the outlet opening of the inlet pipe;
- the inlet pipe comprises at least one injection nozzle an auxiliary gas disposed on the flat bottom wall.
- the cross-sectional area of the inlet opening is equal to the cross-sectional area of the outlet opening.
- the angle a has an absolute value between a' and a'+45°, preferably between a'+10° and a'+20°, a' being l the angle of repose of the particles, and preferably the angle a has an absolute value between 15° and 60°.
- the angle p is determined so that the cross-sectional area of the inlet opening is equal to the cross-sectional area of the outlet opening, and preferably the angle P has an absolute value between 5° and 70°.
- the cyclone comprises between 1 and 10 nozzles/m 2 of the flat bottom wall, preferably between 2 and 5 nozzles/m 2 of the flat bottom wall, distributed evenly over the surface of the flat bottom wall.
- the cross-sectional area of the outlet opening is such that the superficial velocity UgS of the gas of the gaseous mixture leaving said inlet pipe and entering the cyclone chamber is between 5 m/s and 35 m/s.
- said at least one nozzle is configured so as to form a jet having an angle comprised between 0° and 90°, and preferably between 0° and 45°, with respect to the horizontal axis (X) in the vertical plane (XZ).
- said at least one nozzle is configured so that the speed of the gas at the outlet of said nozzle is between 5 m/s and 100 m/s, preferably between 20 m/s and 40 m/s.
- the present invention proposes a plant for the chemical loop combustion of a hydrocarbon feedstock implementing a solid oxygen carrier in the form of particles, comprising at least:
- an oxidation reactor operating in a fluidized bed to oxidize the particles of the reduced oxygen-carrying solid originating from the reduction reactor (300) by bringing them into contact with an oxidizing gas;
- a cyclone positioned downstream of said reduction reactor and/or downstream of said oxidation reactor so as to receive a gaseous mixture comprising solid particles originating from the reduction reactor or from the oxidation reactor.
- the cyclone is positioned downstream of the oxidation reactor, and said oxidation reactor comprises in its upper part the inlet opening of the inlet pipe of the cyclone of so as to send the gaseous mixture comprising particles of the oxygen carrier from said oxidation reactor into the inlet pipe of the cyclone.
- the present invention proposes a process for the chemical loop combustion of a hydrocarbon charge, implementing a cyclone according to the invention or an installation according to the invention, in which:
- the particles of the oxygen carrier having remained in the reduction reactor are oxidized by bringing them into contact with an oxidizing gas within an oxidation reactor operated in a fluidized bed by means of an oxidizing gas, preferably air, before returning them to the reduction reactor;
- an auxiliary gas is injected through at least one nozzle arranged on the inclined lower wall of the inlet pipe of the cyclone so as to disperse the solid particles;
- a gas/solid separation is carried out within said cyclone to form a gas flow depleted in particles extracted by the outlet pipe at the top of the upper cylindrical portion of said cyclone and to form a flow of solid particles evacuated by the evacuation pipe at the bottom of the inverted tapered lower portion of said cyclone.
- the gaseous mixture comprising solid particles sent to the inlet pipe of the cyclone comes directly from the oxidation reactor, and the auxiliary gas is identical to the oxidizing gas of the oxidation reactor, and preferably air, and is injected at a flow rate of between 0.1% and 30% of the flow rate of oxidizing gas used in the oxidation reactor.
- the gaseous mixture comprising solid particles sent to the inlet pipe of the cyclone comes from the reduction reactor, and the auxiliary gas is dioxygen to further carry out a reduction of species residual unburnt contained in the gas mixture, or the auxiliary gas is ammonia to further effect a non-catalytic reduction of NOx contained in the gas mixture.
- the auxiliary gas is injected through said at least one nozzle at a speed of between 5 m/s and 100 m/s, preferably between 20 m/s and 40 m/s , and forms a jet having an angle between 0° and 90°, and preferably between 0° and 45°, relative to the axis (X) in the vertical plane (XZ).
- the superficial gas velocity of the gaseous mixture at the inlet of said inlet pipe is equal to the superficial gas velocity of the gaseous mixture at the outlet of said inlet pipe, and is between 5 m/s and 35 m/s.
- Figure 1 is a schematic sectional view of a cyclone according to one embodiment of the invention and its operation.
- Figure 2 illustrates the same cyclone as that shown in Figure 1, in a top view.
- FIG. 3 is a block diagram of the implementation of a CLC method.
- FIG. 4 illustrates an example of a cyclone according to the invention, according to a sectional diagram (A), according to a top view (B), and according to a perspective view (C).
- Figure 5 illustrates simulation results of the cyclone in operation shown in Figure 4 (B), and of a conventional cyclone comprising an inlet in the form of a horizontal duct (A), and in particular illustrates the deposition of solid particles on the inner surface of the bottom wall of the cyclone inlet.
- FIG. 6 illustrates simulation results of the cyclone according to an embodiment of the invention in operation shown in FIG. 4 (B), and of a conventional cyclone comprising an inlet in the form of a horizontal duct (A), and in particular illustrates the quantity of solid particles according to their residence time in the entry of the cyclones.
- the object of the invention is to provide a cyclone for the gas/solid separation in a chemical loop combustion installation of a hydrocarbon charge, and more broadly in a chemical loop oxidation-reduction installation, implementing circulating fluidized bed reactors.
- the cyclone according to the invention comprises a specific inlet pipe making it possible to reduce the deposit of solid particles at the inlet of the cyclone, to possibly carry out chemical reactions within the cyclone, as well as to improve the efficiency of the cyclone, especially the particulate collection efficiency.
- CLC installations generally comprise two separate reactors: a reduction reactor (or combustion reactor) and an oxidation reactor (or air reactor).
- the reduction of an oxygen-bearing solid takes place by means of a fuel, or more generally of a reducing gas, liquid or solid.
- the reduction reactor effluents mainly contain CO2 and water, allowing easy CO2 capture.
- the restoration of the oxygen-carrying solid to its oxidized state by contact with air or any other oxidizing gas makes it possible to correlatively generate a hot effluent, an energy vector, comprising the reoxidized oxygen carrier , and an oxygen-depleted gas stream, typically a stream of nitrogen lean or devoid of oxygen in the case where air is used.
- CLC chemical loop oxidation-reduction installations/processes
- CLR chemical loop oxidation-reduction installations/processes
- CLOU chemical loop oxidation-reduction installations/processes
- redox active mass or in an abbreviated manner “active mass”, “oxygen carrier material”, “oxygen carrier solid” or “oxygen carrier” are equivalent.
- the redox mass is said to be active in relation to its reactive capacities, in the sense that it is capable of playing its role of oxygen carrier in the CLC process by capturing and releasing oxygen.
- oxidation and reduction are used in relation to the respectively oxidized or reduced state of the oxygen carrier.
- the oxidation reactor also called air reactor, is the one in which the oxygen carrier is oxidized and the reduction reactor, also called fuel reactor or combustion reactor, is the reactor in which the oxygen carrier is reduced.
- the reactors operate in a fluidized bed and the oxygen carrier circulates between the oxidation reactor and the reduction reactor. Circulating fluidized bed technology is used to allow the continuous passage of the oxygen carrier from its oxidized state in the oxidation reactor to its reduced state in the reduction reactor.
- section is generally meant a straight section, unless otherwise specified.
- axis (X) which is a horizontal axis, parallel to the side wall 27 of the cyclone inlet pipe.
- plane (XY) which is a horizontal plane
- plane (XZ) which is a vertical plane, orthogonal to the plane (XY).
- the terms “essentially” or “substantially” correspond to an approximation of ⁇ 5%, preferably ⁇ 1%.
- an element covering substantially an entire surface corresponds to an element covering at least 95% of said surface.
- a new cyclone is proposed for gas/solid separation, suitable for CLC installations and processes.
- This type of cyclone has good separation efficiency, and can advantageously allow chemical reactions to be carried out within the cyclone.
- Figures 1 and 2 illustrate, schematically and in a non-limiting manner, an embodiment of the cyclone according to the invention.
- FIG. 4 also illustrates an example of a cyclone according to the embodiment illustrated in FIGS. 1 and 2, serving to illustrate certain performances of the cyclone according to the invention, as described in more detail in the “example” part.
- the cyclone according to the invention comprises:
- an inlet pipe 21 for a gaseous mixture 2 comprising solid particles coming from a reactor 100 of a CLC installation said inlet pipe 21 comprising at one end an inlet opening O of rectangular section So and at its other end an outlet opening S of rectangular section Ss,
- cylindrical-conical chamber 22 comprising a cylindrical upper portion 22a surmounting an inverted frustoconical lower portion 22b (in other words the narrowest portion of the truncated cone is in the lower part), the cylindrical upper portion 22a comprising the outlet opening S of the inlet pipe;
- An evacuation pipe 24 for a flow of solid particles 4 positioned at the bottom of the inverted tapered lower portion 22b.
- the inlet pipe 21 is delimited by:
- the inlet pipe 21 comprises at least one injection nozzle 29 for an auxiliary gas arranged on the flat lower wall.
- the cyclone according to the invention is of the flow reversal type with a tangential inlet (“tangential-inlet reverse-flow cyclone”).
- tangential-inlet reverse-flow cyclone the gaseous mixture containing solid particles enters at the top of the cyclone and sees itself imposing a centrifugal movement due to its tangential entry. The particles are propelled towards the wall of the cyclone by centrifugal force and then fall along the wall due to gravity.
- the gas flow stripped of the particles which are evacuated at the bottom of the frustoconical section, is reversed to form an internal vortex which exits through an axial duct at the top of the cyclone.
- the outlet pipe 23 is preferably arranged in the axis of the cyclone chamber, and may comprise an internal cylindrical part over a height h, generally called "vortex finder" in English, as is typical in a flow reversal cyclone.
- the gaseous mixture 2 comprising solid particles typically comes from a reactor 100 of a CLC installation comprising an ascending gas/solid multiphase flow 1. This ascending flow changes direction once it has entered the inlet pipe 21 through the opening inlet O, and is referred to as the gas mixture 2 comprising solid particles entering the inlet pipe in the present description.
- the specific inlet of the cyclone according to the invention characterized by its particular geometry and the injection nozzle or nozzles 29 of auxiliary gas, makes it possible to limit the deposit of solid particles in the inlet pipe of the cyclone.
- the downward inclination of the lower wall 26 of the inlet pipe 21 (angle a) promotes the flow and the re-acceleration of the solid particles towards the outlet opening S of the inlet pipe 21, in the direction of the cyclone chamber, and the injection nozzle or nozzles 29 make it possible to inject an auxiliary gas so as to disperse the solid particles.
- the auxiliary gas injected makes it possible to redirect the solid particles which fall on the lower wall 26 towards the main gas flow in the inlet pipe 21, and to destroy the agglomerates of particles, if necessary.
- the specific inlet of the cyclone according to the invention can also make it possible to carry out chemical reactions within the cyclone.
- an oxidizing gas for example the same oxidizing gas as that used in the air reactor to reoxidizing the oxygen carrier particles, eg air, or another oxidizing gas, to complete the oxidation of the oxygen carrier particles.
- auxiliary gas auxiliary gas
- the specific inlet of the cyclone according to the invention characterized by its particular geometry and the injection nozzle(s) 29 of auxiliary gas, also makes it possible to provide a cyclone with good separation efficiency.
- the deposit of solid particles is reduced in the inlet pipe 21, thanks to the injection of auxiliary gas by the injection nozzle(s) 29 and the specific geometry of the inlet pipe 21, in particular the inclined bottom wall 26, which makes it possible not to obstruct the inlet of the cyclone and not to disturb the operation of the cyclone, the gas/solid separation thus being able to take place correctly.
- the dispersion of the solid particles in the main gas flow allows their entrainment in the chamber 22 of the cyclone, and thereby a better gas/solid separation than in the event of stagnation and agglomeration of these same particles on the lower wall. 26 of conduct.
- the inclination of an angle P of the side wall 28 of the inlet pipe 21 makes it possible to preferentially direct the particles towards the wall at the entrance to the cyclone chamber, which makes it possible to improve the collection efficiency of the cyclone, by minimizing on the one hand the distance to be traveled for the particles to the wall of the cyclone chamber, but also by favoring the winding of the gas in the cyclone which limits the re-entrainment of particles towards exit 23 in the entry zone of the cyclone.
- the UgO gas velocity at the inlet opening O of the inlet pipe 21 depends on the physical properties of the solid particles circulating and on the design of the cyclone.
- the area of the section Ss of the outlet opening S is such that the superficial gas velocity UgS of the gaseous mixture leaving said inlet pipe 21 and entering the cyclone chamber is between 5 m/ s and 35 m/s, and more preferably between 15 m/s and 25 m/s, to have good separation performance.
- the section of the inlet pipe 21, in particular the section So of the inlet opening O and that Ss of the outlet opening S of the inlet pipe, is understood as a straight section. This is clearly shown in Figure 2. It is in particular orthogonal to the flat outer surface T1 of the inlet pipe 21.
- the area of the section So of the inlet opening O of the inlet pipe 21 is equal to the area of the section Ss of the outlet opening S of said inlet pipe 21.
- the superficial velocity of the UgO gas of the gas mixture 2 entering said inlet pipe is equal to the superficial velocity of the UgS gas leaving said pipe.
- the area of the section of the inlet pipe is constant from the inlet opening O to the outlet opening S of the inlet pipe 21, guaranteeing a constant superficial gas velocity along of the incoming line.
- the superficial velocity of the UgO gas at the inlet opening of the inlet pipe is preferably equal to the superficial velocity of the UgS gas at the outlet opening of the inlet pipe , it is not beyond the scope of the invention if UgO is less than UgS, in particular if UgO is between 0.5 and 1 times UgS, or even between 0.75 and 1 times UgS.
- the flat bottom wall 26 is inclined relative to the horizontal flat top wall 25 by an angle a defined in a vertical plane (XZ), and so that the dimension along the vertical axis (Z) of the opening outlet S of the inlet pipe is less than the dimension along the axis (Z) of the inlet opening O, as clearly visible in FIG. 1. Due to this angle a, the lower wall plane 26 is inclined downwards with respect to the horizontal axis (X), from the inlet opening O towards the outlet opening S arranged in the part of the inlet pipe 21.
- the angle a has an absolute value between a' and a'+45°, preferably between a'+10° and a'+20°, a' being the angle of repose of the particles.
- the angle of repose or slope of the particles is traditionally defined as the angle between the slope of the pile of untamped powder and the horizontal direction and can be determined with different methods. For example, this angle can be measured by pouring the powder through a funnel, which makes it possible to form a small pile of product characterized by a slope with respect to the horizontal surface.
- the angle of repose can also be measured by sliding a solid on an inclined plate, the angle of repose then being measured as the angle at which the solid material begins to slide, or by using a rotating cylinder to determine the angle that allows the solid to flow. These last two methods are preferably used to determine the angle of repose because they involve the motion of the solid.
- the angle a can have an absolute value comprised between 5° and 80°, preferably between 15° and 60°, more preferably between 15° and 45°, and even more preferably between 20° and 45°.
- the inclination of the lower wall of the inlet pipe reduces the saltation velocity of the particles, and consequently the accumulation of the particles.
- the flat inner side wall 28 is inclined relative to the flat outer side wall 27 by an angle P defined in the horizontal plane (XY), and so that the dimension along the axis (Y) (i.e. the width) of the outlet opening S of the inlet pipe is less than the dimension along the axis (Y) (i.e. the width) of the inlet opening O, as clearly visible in figure 2.
- the angle P is determined so that the area of the section So of the entrance opening O is equal to the area of the section Ss of the exit opening S.
- the angle P is determined so that the area of the section So of the entrance opening O is equal to the area of the section Ss of the exit opening S.
- the angle P can have an absolute value between 5° and 70°, preferably between 10° and 50°.
- the injection nozzle(s) make it possible to inject the auxiliary gas so as to disperse the solid particles and reinforce the limitation of the deposit of solid particles in the inlet pipe.
- the presence of such a gas can also make it possible, depending on its nature, and the temperature and pressure conditions operated in the cyclone, to carry out chemical reactions in the cyclone. These reactions are described in detail later in connection with the description of the CLC plant and process.
- the number of nozzles for injecting the injection auxiliary gas depends on the total flow rate of injected auxiliary gas.
- the cyclone has a nozzle density of between 1 and 10 nozzles per square meter, and preferably between 2 and 5 nozzles per square meter.
- the reference surface for the density of the nozzles is that of the flat lower wall 26 of the inlet pipe 21.
- the nozzles can for example be distributed in a regular manner along a central longitudinal axis of the lower wall of the supply pipe. arrival 21, from the inlet opening O to the outlet opening S. They are preferably distributed evenly over the lower flat surface, for example along of an axis or of several secant axes, for example at the intersections of secant axes according to a square, rectangular, triangular etc. pattern.
- the cyclone according to the invention comprises an inlet pipe comprising three equidistant injection nozzles, distributed over the lower wall of the inlet pipe 21, along the central longitudinal axis of said lower wall, as shown in Figure 4.
- the nozzle or nozzles are preferably configured so as to form a jet having an angle between 0° and 90°, preferably greater than 0° and less than 90°, and more preferably between 0° (and preferably greater than 0°) and 45°, with respect to the horizontal axis (X) in the vertical plane (XZ).
- the jet formed is thus preferably directed along the axis of the flow of the gaseous mixture in the pipe, so as not to disturb the flow going towards the body of the cyclone too much.
- the nozzle or nozzles are configured so that the speed of the gas at the outlet of said nozzle is between 5 m/s and 100 m/s, preferably between 20 m/s and 40 m/s, to avoid only solid particles enter the nozzle, to obtain a good dispersion of the solid particles and break up any agglomerates.
- the cyclone is advantageously implemented in a CLC installation, and typically operated under the pressure and temperature conditions of a CLC process as detailed below. It is thus preferably formed of materials adapted to the high temperatures encountered in CLC, typically between 800° C. and 1000° C., or even between 600° C. and 1400° C., for example, and without being limiting, high temperature steels , such as those of the Hastelloy®, Incoloy®, Inconel® or Manaurite® type, or conventional steels, for example of the stainless steel or carbon steel type combined with refractory materials or combined with cooling means such as tubes in which circulating a heat transfer fluid.
- high temperature steels such as those of the Hastelloy®, Incoloy®, Inconel® or Manaurite® type, or conventional steels, for example of the stainless steel or carbon steel type combined with refractory materials or combined with cooling means such as tubes in which circulating a heat transfer fluid.
- the cyclone is well suited to the gas/solid separation of gaseous mixtures comprising solid particles whose mean particle diameter is between 20 ⁇ m and 1000 ⁇ m.
- the cyclone is well suited to the gas/solid separation of gaseous mixtures comprising a load of solid particles preferably between 0.1 and 50 w/w (weight of solid particles relative to the weight of gas).
- the cyclone according to the invention can have a total height of a few meters (height of the cylindrical-conical chamber), for example 5 meters, a diameter of the cylindrical upper part (“ barrel") of the cylindrical-conical chamber of the order of one meter, for example 1 meter, and include an inlet pipe with a rectangular opening of sub-metric or metric order, for example 0.6 meter x 0, 2 meters, and a few meters long, for example 2.5 meters.
- a cyclone having the examples of given values cited makes it possible, for example, to treat 0.9 kg/s of gas and a flow rate of the solid of 30 kg/s.
- FIG. 3 is a diagram representing the general principle of operation of chemical loop combustion. It is in no way limiting of the cyclone according to the invention which can be used in the installation and the CLC method of the invention.
- a reduced oxygen carrier 8 is brought into contact with a flow of an oxidizing gas 5, typically air, in a reaction zone 100 previously defined as the oxidation reactor (or air reactor). This results in a depleted air flow 3 and a flow of re-oxidized particles 4.
- the flow of oxidized oxygen carrier particles 4 is transferred to the reduction zone 300 previously defined as the combustion reactor (or reduction).
- the flow of particles 4 is brought into contact with a fuel 5, which is a hydrocarbon charge. This results in a combustion effluent 7 and a flow of particles of reduced oxygen carrier 8.
- the hydrocarbon charge 6 is brought into co-current contact with the oxygen carrier in the form of particles to carry out the combustion of said charge by reduction of the oxygen carrier.
- the oxygen carrier M x O y M representing a metal, is reduced to the state M x O y -2 n -m/2, by the intermediary of the hydrocarbon charge C n H m , which is correlatively oxidized to CO2 and H2O, according to reaction (1) below, or optionally to a CO + H 2 mixture depending on the proportions used.
- Total combustion of the hydrocarbon charge is generally targeted.
- the combustion of the charge in contact with the oxygen carrier is carried out at a temperature generally between 600°C and 1400°C, preferably between 800°C and 1000°C.
- the contact time varies according to the type of combustible charge used. It typically varies between 1 second and 20 minutes, for example preferably between 1 minute and 10 minutes, and more preferably between 1 minute and 8 minutes for a solid or liquid load, and for example preferably from 1 to 20 seconds for a load carbonated.
- a mixture comprising the gases resulting from the combustion and the particles of the oxygen carrier is evacuated at the top of the reduction zone 300.
- Gas/solid separation means such as a cyclone, make it possible to separate the combustion gases 7 of the solid particles of the oxygen carrier in their most reduced state 8.
- a solid/solid separation device making it possible to separating the particles of unburnt particles from the particles of the oxygen carrier can be implemented at the outlet of the combustion reactor.
- This type of separator can be associated with one or more gas/solid separators arranged downstream of the solid/solid separator, and for example with a cyclone according to the invention.
- the particles of the oxygen carrier having stayed in the combustion reactor, and separated from the combustion gases, are sent to the oxidation zone 100 to be re-oxidized.
- the unburnt particles can be recycled to the reduction reactor 300.
- the oxygen carrier is restored to its oxidized state M x O y in contact with an oxidizing gas 5, typically air or steam, and preferably air, according to reaction (2) below, before returning to the reduction reactor 300, and after having been separated from the oxygen-depleted gas 3, typically so-called "depleted" air, evacuated at the top of the reactor of oxidation 100.
- an oxidizing gas 5 typically air or steam, and preferably air, according to reaction (2) below
- n and m respectively represent the number of carbon and hydrogen atoms reacted with the oxygen carrier in the combustion reactor.
- the temperature in the oxidation reactor is generally between 600°C and 1400°C, preferably between 800°C and 1000°C.
- the oxygen carrier passing alternately from its oxidized form to its reduced form and vice versa, describes an oxidation-reduction cycle.
- the hydrocarbon feedstocks (or fuels) treated can be solid, gaseous or liquid hydrocarbon feedstocks, and preferably solid or gaseous feedstocks.
- the solid fillers can be chosen from among coal, coke, pet-coke, biomass, bituminous sands and household waste.
- the gaseous feeds are preferably composed essentially of methane, for example natural gas or a biogas.
- the liquid fillers can be chosen from oil, bitumen, diesel, gasoline.
- the hydrocarbon feedstock treated is a solid or gaseous feedstock, as stated above.
- the oxygen carrier may be composed of metal oxides, such as for example oxides of Fe, Ti, Ni, Cu, Mn, Co, V, alone or as a mixture, which may come from ores (for example ilmenite or pyrolusite) or be synthetic (for example copper oxide particles supported on CuO/Al 2 O 3 alumina or nickel oxide particles supported on NiO/ALC alumina), with or without a binder, and has the properties oxidation-reduction required and the characteristics necessary for the implementation of fluidization.
- the oxygen storage capacity of the oxygen carrier is advantageously comprised, depending on the type of material, between 0.5% and 15% by weight.
- the quantity of oxygen actually transferred by the metal oxide is between 0.5% and 3% by weight, which makes it possible to use only a fraction of the total oxygen transfer capacity, ideally less than 30% of it in order to limit the risks of mechanical aging or particle agglomeration.
- the use of only a fraction of the oxygen transport capacity also has the advantage that the fluidized bed acts as a thermal ballast and thus smooths the temperature variations on the path of the oxygen carrier.
- the oxygen carrier is in the form of fluidizable particles, belonging to groups A, B, C or D of the Geldart classification, preferably to groups A, B, or D, alone or in combination.
- the particles of the oxygen carrier belong to group B of the Geldart classification.
- the particles of group B used have a particle size such that more than 90% of the particles have a size of between 100 ⁇ m and 500 ⁇ m, preferably between 150 ⁇ m and 300 ⁇ m.
- the particles of the oxygen carrier which may be metal oxides, synthetic or natural minerals, supported or not, have a density of between 1000 kg/m 3 and 5000 kg/m 3 and preferentially between 1200 kg/m 3 and 4000 kg/m 3 .
- nickel oxide particles supported on alumina generally have a grain density of between 2500 kg/m 3 and 3500 kg/m 3 depending on the porosity of the support and the the nickel oxide content, typically approximately 3200 kg/m 3 .
- Ilmenite, an ore combining titanium and iron (iron oxide and titanium) has a density of 4700 kg/m 3 .
- the oxygen carrier can undergo an activation phase so as to increase its reactive capacities, which can consist of a temperature rise phase, preferably progressive, and preferably under an oxidizing atmosphere (for example under air).
- Oxidation and combustion reactors operate in fluidized beds. They each comprise at least one fluidization gas injection system.
- the fluidization gas can be CO 2 , which can be CO 2 produced during combustion and recycled, or steam.
- the fluidizing gas is an oxidizing gas, preferably air.
- the oxidation reactor 100 preferably comprises a transported fluidized bed.
- the gas velocity gas phase of the bed
- the gas velocity is between 2 m/s and 15 m/s, and preferably between 3 m/s and 10 m/s.
- such an oxidation reactor can have a diameter comprised between 1 m and 6 m for a height comprised between 10 m and 30 m.
- the oxidation reactor is thus configured to receive the particles of the oxygen carrier having stayed in the combustion reactor, to oxidize said particles within the transported bed, and to return them to said combustion reactor.
- Combustion reactor 300 can be configured to include a dense fluidized bed.
- the superficial velocity of the gas in the dense fluidized bed of the reactor which is also referred to here as the superficial velocity of the operational gas Ug, is between 0.1 m/s and 3 m/s, preferably between 0.3 m/s and 2 m/s.
- the combustion reactor 300 can have a diameter DR comprised between 1 m and 10 m.
- the combustion reactor preferably has a height H R to diameter DR ratio of between 0.5 and 8, preferably between 1 and 5, even more preferably between 2 and 4. The same applies for the ratio of the height of the dense fluidized bed in the reactor to the diameter of the reactor.
- dense fluidized bed is meant a bubbling bed (bubbling regime also called bubble regime or bubbling bed) or a turbulent bed (turbulent regime).
- the volume fraction of solid in such a dense fluidized bed is generally between 0.20 and 0.50.
- a sufficiently long contact time of the feedstock with the particles of the oxygen carrier is generally necessary to tend towards total combustion, and involves a first phase of gasification of the solid feedstock, followed by combustion of the gasified charge.
- Both phases can be carried out in the dense fluidized bed of the combustion reactor.
- the first phase can be carried out in the dense fluidized bed of the combustion reactor, and the second phase can be carried out in another combustion zone, for example within the same reactor in a zone overcoming the dense bed and operating in a dilute fluidized bed or in a separate reactor receiving the gasified charge and bringing it into contact with the oxygen carrier, in a dense or dilute fluidized bed.
- dilute fluidized bed is meant a transported bed.
- the volume fraction of solid is generally less than 0.20.
- Combustion reactor 300 can thus be configured to include a dilute fluidized bed.
- a reactor or part of “riser” type reactor forming a substantially elongated and vertical conduit, and operating in a dilute fluidized bed, may be sufficient to carry out the combustion of the charge, and to transport the particles.
- the speed is preferably greater than 3 m/s and less than 30 m/s, more preferably between 5 and 15 m/s, so as to facilitate the transport of all the particles while minimizing pressure drops so as to optimize the energy efficiency of the process.
- the geometry of the reactors can be parallelepipedic, typically a rectangular parallelepiped, cylindrical or any other three-dimensional geometry preferably comprising a symmetry of revolution.
- Cylindrical refers to a cylinder of revolution.
- the combustion reactor is cylindrical or has the shape of a rectangular parallelepiped.
- the diameter DR of the reactor must be understood as an equivalent diameter, defined as the diameter of the circle inscribed in the section of the reactor.
- the materials used to make the reactors and their constituent elements can be chosen from refractory materials, for example of the refractory concrete, refractory brick or ceramic type, high temperature steels, for example of the Hastelloy®, Incoloy®, Inconel® or Manaurite® type, or conventional steels, for example of the stainless steel or carbon steel type combined with refractory materials or combined with cooling means such as tubes in which a heat transfer fluid circulates.
- the present invention thus relates to a CLC installation which comprises at least:
- a reduction reactor 300 operating in a fluidized bed to carry out the combustion of the hydrocarbon charge in contact with the particles of the oxygen-carrying solid;
- an oxidation reactor 100 operating in a fluidized bed, to oxidize the particles of the reduced oxygen-carrying solid coming from the reduction reactor 300, by bringing them into contact with an oxidizing gas;
- a cyclone according to the invention positioned downstream of the reduction reactor 300 and/or downstream of the oxidation reactor 100 so as to receive a gaseous mixture comprising solid particles originating from the reduction reactor 300 or the oxidation reactor 100.
- the cyclone is positioned downstream of the oxidation reactor 100, and is connected directly, ie without any other enclosure or intermediate device, to said oxidation reactor 100 so as to receive, via the pipe of arrival 21, a gaseous mixture comprising particles of the oxygen carrier from said oxidation reactor 100.
- the oxidation reactor 100 comprises, in its upper part, the inlet opening of the inlet pipe of the cyclone, so as to directly send a gaseous mixture comprising particles of the oxygen carrier from the oxidation reactor 100 into the inlet pipe of said cyclone.
- Such a configuration has the particular advantage that the auxiliary gas injected into the inlet pipe of the cyclone, if of the same nature as the same oxidizing gas as used in the oxidation reactor, eg air, makes it possible to continue the oxidation reaction of the oxygen carrier, in particular facilitated due to the greater concentration of the oxygen carrier in the inlet pipe of the cyclone than in the oxidation reactor 100.
- This has the effect of improving the degree progress of the reactions (oxidation of the carrier), and has substantially the same effect as adding this flow of gas to the oxidation reactor upstream, without having to significantly increase its size to respect the same conditions of fluidization.
- this injection of auxiliary gas into the inlet pipe of the cyclone is in fact carried out at a lower pressure than the injection of oxidizing gas into the oxidation reactor upstream, and therefore makes it possible to save energy. energy compared to a configuration where the flow of auxiliary gas would be introduced into the oxidation reactor upstream.
- the present invention can also be advantageously implemented in the context of the transformation of an existing CLC unit ("revamping"), without modifying the oxidation reactor upstream of the cyclone which is designed to operate with a certain flow rate. gas. In this case, the injection of auxiliary oxidizing gas into the inlet pipe of the cyclone makes it possible to increase the oxidation capacity of the unit.
- the cyclone is positioned downstream of the combustion reactor 300, and receives a gaseous mixture comprising particles of the oxygen carrier from the reduction reactor 300.
- the reduction reactor 300 can comprise, in its upper part, the inlet opening of the inlet pipe of the cyclone, so as to send (directly) the gaseous mixture into the inlet pipe of said cyclone.
- the installation can comprise a solid/solid separator as already mentioned above, and in this case the cyclone according to the invention can be positioned downstream of the solid/solid separator.
- Said solid/solid separator can then comprise, in its upper part, the inlet opening of the cyclone inlet pipe, so as to send (directly) the gaseous mixture from the solid/solid separator into the supply pipe. arrival of said cyclone.
- the solid/solid separator may comprise an outlet pipe for the gas stream comprising the lightest particles which comprises the inlet opening of the cyclone inlet pipe.
- the solid/solid separator is used to effect a separation between particles of unburned matter and particles of the oxygen carrier based on the physical properties of different size and density of the particles.
- the particles of the oxygen carrier, described above generally have a size and a density much greater than those of the particles of unburned matter, and also than that of the fly ash from the combustion reactor.
- the solid/solid separator can thus be used to carry out a separation between, on the one hand, particles of unburned matter and, on the other hand, particles of the oxygen carrier having a density greater than or equal to 1000 kg/m 3 , of preferably greater than or equal to 1200 kg/m 3 , more preferably greater than or equal to 2500 kg/m 3 .
- more than 90% of the oxygen carrier particles have a size between 100 ⁇ m and 500 ⁇ m, preferably between 150 ⁇ m and 300 ⁇ m.
- the size of the particles of unburned matter is less than 100 ⁇ m and that the majority of said particles has a size of between 20 and 50 ⁇ m.
- the density of these unburnt particles is generally between 1000 and 1500 kg/m 3 .
- Other particles such as fly ash, to be distinguished from unburnt particles, and resulting from the combustion of the solid charge, can also circulate with the rest of the particles and are characterized by a particle size and a lower density than the oxygen carrier particles (ie less than 100 ⁇ m) and often also weaker than the unburnt particles.
- the ashes are incombustible elements resulting from the total combustion of the solid fuel particles and for which the residence time in the combustion reactor has been sufficient.
- the ashes are essentially mineral in nature. They typically comprise the following compounds: SiO 2 , Al 2 O 3 , Fe 2 O 3 , CaO, MgO, TiO 2 , K 2 O, Na 2 O, SO 3 , P 2 O 5 . If ashes are present in the process and in particular in the gaseous mixture coming from the combustion reactor, they can be separated and entrained with the particles of unburned matter in the solid/solid separator.
- the present invention also relates to a CLC method implementing the cyclone according to the invention or the CLC installation according to the invention comprising such a cyclone, comprising the following steps:
- - oxidation of the particles of the oxygen carrier having stayed in the reduction reactor 300 is carried out by bringing them into contact with an oxidizing gas within the oxidation reactor 100 operated in a fluidized bed by means of an oxidizing gas, preferably air, before returning them to the reduction reactor 300;
- the gaseous mixture comprising solid particles coming from the reduction reactor 300 or from the oxidation reactor 100 is sent to the inlet pipe of the cyclone;
- the auxiliary gas is injected through at least one nozzle arranged on the inclined lower wall of the inlet pipe of the cyclone so as to disperse the solid particles;
- a gas/solid separation is carried out within the cyclone to form a gaseous flow depleted in particles extracted by the outlet pipe from the cyclone and to form a flow of solid particles evacuated by the outlet pipe from the cyclone.
- the gaseous mixture comprising solid particles sent into the inlet pipe of the cyclone comes directly from the oxidation reactor 100 (i.e. without any other enclosure or intermediate device).
- the solid particles are those of the oxygen carrier.
- the auxiliary gas can be identical to the oxidizing gas of the oxidation reactor, and preferably is air.
- the auxiliary gas can also be oxygen.
- the auxiliary gas is injected at a flow rate of between 0.1% and 30% by volume of the flow rate of oxidizing gas used in the oxidation reactor, or even between 1% and 10% by volume. .
- the gaseous mixture comprising solid particles sent to the inlet pipe of the cyclone comes from the reduction reactor.
- the auxiliary gas can advantageously be dioxygen to convert the residual unburned species or ammonia to reduce, for example, the NOx concentration.
- the auxiliary gas can also be CO 2 , preferably recycled, or steam.
- the auxiliary gas is injected at a flow rate less than or equal to 30% by volume of the flow rate of fluidization gas used in the oxidation reactor, the minimum flow rate being able to be determined by a person skilled in the art. profession so as to carry out the desired chemical reactions, namely the combustion of residual unburnt species or the non-catalytic selective reduction of NOx.
- residual unburned species we mean the gaseous or solid compounds produced during incomplete combustion of the charge, mainly the unburned gaseous compounds, eg CO and/or H 2 , resulting from the conversion of the charge in contact with water (devolatilization/gasification of a solid or liquid feed and reforming of methane, producing CO and H 2 ) or a fraction of the unconverted gaseous hydrocarbon feed, eg CH 4 , or a solid fraction of the hydrocarbon feed not converted in the case of a solid load for example.
- unburned gaseous compounds eg CO and/or H 2
- the auxiliary gas is injected through the nozzle or nozzles at a speed of between 5 m/s and 100 m/s, preferably between 20 m/s and 40 m/s.
- the auxiliary gas injected forms a jet having an angle of between 0° and 90°, and preferably between 0° and 45°, with respect to a horizontal axis (X) in the vertical plane (XZ).
- the superficial gas velocity of the gas mixture at the outlet of the UgS inlet pipe, and entering the cyclone chamber is preferably between 5 m/s and 35 m/s, and more preferably between 15 m/s and 25 m/s, to have good separation performance.
- the superficial gas velocity of the gas mixture at the inlet of the inlet pipe may advantageously be equal to the superficial gas velocity of the gas mixture at the outlet of the inlet pipe.
- the following example aims to show certain performances of the cyclone according to the invention, in particular the limitation of the deposit of solid in the inlet pipe of the cyclone placed at the outlet of an air reactor of a CLC installation, compared to a classic cyclone fitted with a traditional inlet pipe in the form of a horizontal duct.
- This example is based on numerical simulations in CFD (fluid dynamics) by the Barracuda® software (CPFD Software), and models the hydrodynamic aspect, without taking into account the real temperature conditions of a CLC unit (“cold” model). .
- FIG. 4 illustrates the example of cyclone according to the invention tested, according to 3 different schematic views: (A) in section, (B) from above, and (C) in perspective (C).
- the cyclone inlet pipe according to the invention like that of the conventional cyclone, has a rectangular section.
- the cyclone according to the invention comprises, unlike the conventional cyclone, an inlet pipe 21 comprising:
- the injection nozzles are vertical ducts opening into the inlet duct so as to create a jet at 90° relative to the horizontal (X) in the vertical plane (XZ).
- the solid particles of the oxygen carrier have an average diameter of 330 ⁇ m, and a density of 2200 kg/m 3 .
- the mass flux of particles in the air reactor 100 in the form of a riser is 220 kg/m 2 /s.
- the gas used in the air reactor is air, at 26.85° C. (300 K) and 0.1 MPa (1 atm).
- the superficial gas velocity in the inlet pipe 21 is 15m/s.
- the auxiliary gas injected by the three nozzles is air, and its flow rate is equal to 10% of the air flow rate used in the air reactor.
- the injection of air through the nozzles makes it possible to reduce the solid deposit in the inlet pipe and to complete the oxidation reaction in the inlet pipe, before sending the gas and the particles into the cyclone chamber .
- FIG. 5 illustrates the deposit of solid on the internal surface of the lower wall of the inlet pipe of the cyclone according to the invention (B) and of the conventional cyclone (A): in the example of a cyclone according to one embodiment of the invention, in the image (B) on the right, the much lower volume fraction of PVF particles at the level of the lower wall of the inlet pipe than in the case of the conventional cyclone, visible in the image ( A) left.
- FIG. 6 illustrates the quantity of solid particles under the same conditions of gas flow rates and of particles according to their residence time in the inlet pipe of the cyclone according to one embodiment of the invention (B) and of the conventional cyclone (A ): in the example of a cyclone according to the invention, in the image (B) on the right, there are many fewer particles having a residence time greater than 2 seconds within the inlet pipe, compared to the case of the classic cyclone, visible in the image (A) on the left.
- the mean residence time of the particles at the outlet of the cyclone inlet pipe is reduced by 13% in the case of the example of the cyclone according to the invention, which amounts to having on average 44% fewer particles in the inlet pipe of the cyclone.
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- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
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Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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CA3238175A CA3238175A1 (fr) | 2021-12-17 | 2022-12-07 | Cyclone pour une installation et un procede de combustion en boucle chimique muni d'une conduite d'arrivee a parois inclinees et injection de gaz |
CN202280083628.5A CN118510608A (zh) | 2021-12-17 | 2022-12-07 | 设置有具有斜壁和气体注入部的入口导管的用于化学链燃烧设施和方法的旋风分离器 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR2113894A FR3130651B1 (fr) | 2021-12-17 | 2021-12-17 | Cyclone pour une installation et un procede de combustion en boucle chimique muni d’une conduite d’arrivee a parois inclinees et injection de gaz |
FRFR2113894 | 2021-12-17 |
Publications (1)
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WO2023110590A1 true WO2023110590A1 (fr) | 2023-06-22 |
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PCT/EP2022/084843 WO2023110590A1 (fr) | 2021-12-17 | 2022-12-07 | Cyclone pour une installation et un procede de combustion en boucle chimique muni d'une conduite d'arrivee a parois inclinees et injection de gaz |
Country Status (4)
Country | Link |
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CN (1) | CN118510608A (fr) |
CA (1) | CA3238175A1 (fr) |
FR (1) | FR3130651B1 (fr) |
WO (1) | WO2023110590A1 (fr) |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5771844A (en) * | 1996-04-04 | 1998-06-30 | Foster Wheeler Development Corp. | Cyclone separator having increased gas flow capacity |
US20080246655A1 (en) | 2004-12-17 | 2008-10-09 | Jon Olafur Winkel | Spreading Codes for a Satellite Navigation System |
WO2011047848A2 (fr) * | 2009-10-21 | 2011-04-28 | Outotec Oyj | Appareil pour le traitement des solides et/ou des gaz |
US20110146152A1 (en) | 2009-12-21 | 2011-06-23 | Pannalal Vimalchand | Apparatus, Components and Operating Methods for Circulating Fluidized Bed Transport Gasifiers and Reactors |
US20120272825A1 (en) * | 2009-07-23 | 2012-11-01 | Binder + Co Ag | Cyclone having a pure gas line |
-
2021
- 2021-12-17 FR FR2113894A patent/FR3130651B1/fr active Active
-
2022
- 2022-12-07 WO PCT/EP2022/084843 patent/WO2023110590A1/fr active Application Filing
- 2022-12-07 CN CN202280083628.5A patent/CN118510608A/zh active Pending
- 2022-12-07 CA CA3238175A patent/CA3238175A1/fr active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5771844A (en) * | 1996-04-04 | 1998-06-30 | Foster Wheeler Development Corp. | Cyclone separator having increased gas flow capacity |
US20080246655A1 (en) | 2004-12-17 | 2008-10-09 | Jon Olafur Winkel | Spreading Codes for a Satellite Navigation System |
US20120272825A1 (en) * | 2009-07-23 | 2012-11-01 | Binder + Co Ag | Cyclone having a pure gas line |
WO2011047848A2 (fr) * | 2009-10-21 | 2011-04-28 | Outotec Oyj | Appareil pour le traitement des solides et/ou des gaz |
US20110146152A1 (en) | 2009-12-21 | 2011-06-23 | Pannalal Vimalchand | Apparatus, Components and Operating Methods for Circulating Fluidized Bed Transport Gasifiers and Reactors |
Non-Patent Citations (1)
Title |
---|
GAUTHIER ET AL.: "Gas-solid séparation in a uniflow cyclone at high solids loadings: effect of acceleration line", PROCEEDINGS OF THE 3RD INTERNATIONAL CONFÉRENCE ON CIRCULATING FLUIDIZED BEDS, October 1991 (1991-10-01) |
Also Published As
Publication number | Publication date |
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FR3130651B1 (fr) | 2023-12-15 |
CA3238175A1 (fr) | 2023-06-22 |
CN118510608A (zh) | 2024-08-16 |
FR3130651A1 (fr) | 2023-06-23 |
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