WO2007031573A1 - Dispositif d'injection de fluide en couches successives dans un lit fluidifie rotatif et procedes utilisant ce dispositif - Google Patents
Dispositif d'injection de fluide en couches successives dans un lit fluidifie rotatif et procedes utilisant ce dispositif Download PDFInfo
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- WO2007031573A1 WO2007031573A1 PCT/EP2006/066404 EP2006066404W WO2007031573A1 WO 2007031573 A1 WO2007031573 A1 WO 2007031573A1 EP 2006066404 W EP2006066404 W EP 2006066404W WO 2007031573 A1 WO2007031573 A1 WO 2007031573A1
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Classifications
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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
- B01J8/1881—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving downwards while fluidised
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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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/14—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moving in free vortex flow apparatus
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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
- B01J8/36—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 through which there is an essentially horizontal flow of 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
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- B01J2219/0004—Processes in series
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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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/18—Details relating to the spatial orientation of the reactor
- B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
Definitions
- the present invention relates to a fluid injection device, in successive layers, in a fluidized bed
- Rotary within a fixed circular reaction chamber, and processes for catalytic polymerization, drying, impregnation, coating or other treatments of solid particles suspended in the rotating fluidized bed, or cracking, dehydrogenation or other catalytic conversion of fluids using this device.
- the centripetal pressure exerted by the fluid which radially passes through the fluidized bed can be substantially higher and therefore j 5 flow rate and speed difference with that of the solid particles can be substantially higher, which improves the contact between the fluid and the solid particles and substantially increases the volume of fluid that can pass through the fluidized bed and thus also its ability to cool, heat and / or dry the solid particles .
- the density and the rotation speed of the fluidized bed are large. The latter will decrease rapidly if the kinetic moment of rotation is not maintained using rotary mechanical means, with the problems related to the presence of mobile equipment inside a reactor, and / or by the injection of fluid, at high speed, in the direction of rotation of the fluidized bed.
- the specific mass of the fluid is much smaller than that of the solid particles, the amount of fluid that must be injected to transfer to the solid particles the required kinetic momentum is very large and it can prevent the formation
- the present invention relates to a rotating fluidized bed apparatus comprising a circular reaction chamber, a device for supplying one or more fluids, arranged around the circular wall of said circular reaction chamber, a device evacuation of said fluid or fluids, a device for feeding solid particles to one side of said circular reaction chamber and a device for discharging said solid particles on the opposite side of said circular reaction chamber, characterized in what:
- the said device for discharging the fluid or fluids comprises a central chimney extending longitudinally or penetrating inside the said reaction chamber, the wall of the said central chimney comprising at least one discharge opening allowing to evacuate centrally, by said central chimney, the fluid or said fluids of said circular reaction chamber;
- the said device for supplying the fluid (s) comprises fluid injectors distributed around the
- Said centrifugal force is, on average, at least equal to three times the force of gravity, said solid particles thus forming a rotating fluidized bed which rotates around and at a certain distance from said central chimney sliding along the said one of the said circular wall and being supported by the said layers or said fluids which cross the said fluidized ha before being removed centrally by the said discharge opening of the said central chimney and the centripetal force is compensated by said centrifugal force acting on said solid particles.
- mjectors distributed around the circular wall of a circular reaction chamber, inject one or more fluids, along the circular wall, into successive layers, in order to form a succession of layers of fluid which superimposed by rotating rapidly inside the reaction chamber, around a central chimney that penetrates or crosses along its central axis and which is provided with one or more discharge openings through which the fluid can be evacuated centrally.
- the circular reaction chamber is traversed by a stream of solid particles which are fed from one of its sides and discharged from the opposite side and which are driven by the fluid in a fast rotational movement whose centrifugal force makes it possible to concentrate them before their exit from the circular reaction chamber, in a dense rotary fluidized ht, which is at least partially supported by the centripetal pressure of these successive layers of fluid which run along the circular wall and which act as fluid cushions, reducing the friction of the solid particles against this wall.
- the fluid is supplied by a supply device which may comprise a fluid supply chamber surrounding the circular reaction chamber, the pressure difference, preferably greater than the average pressure due to the centrifugal force of the rotary fluidized bed against the circular wall, between the feed device and the central chimney and the flow rate of the fluid or fluids for supporting and rotating the fluidized ht at a speed generating a substantial average centrifugal force, preferably greater than three times the force of gravity .
- a supply device which may comprise a fluid supply chamber surrounding the circular reaction chamber, the pressure difference, preferably greater than the average pressure due to the centrifugal force of the rotary fluidized bed against the circular wall, between the feed device and the central chimney and the flow rate of the fluid or fluids for supporting and rotating the fluidized ht at a speed generating a substantial average centrifugal force, preferably greater than three times the force of gravity .
- each annular slice of the reaction chamber there is at least one injector of fluid every 90 °, ie 4, and preferably at least seven, the most preferred being at least 11 and therefore the number of successive layers of fluid is high, or the distance between these mjectors is small, preferably less than mean radius of the circular chamber, to limit the amount and concentration of solid particles that come into contact with this circular wall after having passed through the layer of fluid that has been injected by the injector upstream, before reaching the layer of fluid injected by the injector located downstream.
- the profile of the mjectors be designed so as to be able to inject the fluid at a sufficient speed, preferably at least twice the desired rotation speed for the solid particles in the fluidized bed, and in thin layers, with a thickness at the moment of their injection, preferably less than one twentieth of the mean radius of the reaction chamber, in a direction forming an acute angle, preferably less than 30 °, with the circular wall, and that the planes of the outlet openings of the Fluid injectors form, with the side of the circular wall situated downstream, preferably angles of between 60 ° and 120 °, so that the thrust of the fluid or fluids at the time of their exit from the mjectors is more tangential than radial or centripetal.
- the circular wall may be cylindrical, but it may also have different radii of curvature or be flat between the fluid mjectors. In the latter case the circular wall is polygonal and its sides located on either side of the mjectors form an angle all the closer to 180 ° as the number of injectors is high.
- no cross-section of the central chimney comprises more than one fluid discharge opening, and that these openings are narrow, arranged longitudinally, preferably of an average width of less than half the average distance between the central chimney and the circular wall and that the sum of the sections of the discharge openings is preferably less than twice the sum of the sections of the outlet openings of the fluid mjectors, which itself is preferably lower than the half of the mean longitudinal section of the circular reaction chamber, and that the planes of these discharge openings form with the wall of the central chimney an angle of preferably between 60 and 120 °, this wall gradually diverging from the circular wall of the reaction chamber, from its side downstream of the discharge openings to the opposite side, thus taking the ap appearance of a spiral.
- the present invention may comprise at least one deflector, wing-shaped, longitudinally passing through the reaction chamber, near the wall of the central chimney, having its leading edge upstream of the evacuation opening or openings of the fluid and its trailing edge downstream of these fluid discharge openings, in order to reintroduce into the reaction chamber the solid particles, generally the finest, which have entered the space between the baffle and the wall of the central fireplace.
- the inlet section of this space is preferably larger than the sum of the sections of the exhaust openings and the distance between the trailing edge and the wall of the central stack is preferably less than half the distance between this edge and the circular wall.
- This deflector may be hollow and provided with fluid injectors arranged along its trailing edge, in order to inject at high speed, a layer of fluid, approximately parallel, preferably more or less 30 °, at the wall of the central chimney, downstream of the discharge openings, to prevent these solid particles to go up along the wall of the central chimney downstream of the discharge opening.
- the present invention may comprise at least one control transverse ring, which is placed close to the exit of the solid particles, whose outer edge runs along and is fixed to the circular wall and whose inner edge surrounds and is at an average distance from the central chimney, preferably greater than a quarter of the mean distance between the central chimney and the circular wall, in order to allow the solid particles to pass from one side of the fluidized bed to the other without being too close to the evacuation openings of the central fireplace.
- This regulation ring makes it possible to prevent or slow down the transfer of the solid particles situated upstream of this ring downstream, as long as the fluidized bed has not reached the desired thickness upstream.
- This ring may comprise a passage along the circular wall, to allow a minimum passage sufficient to gradually empty the circular reaction chamber when the supply of solid particles is stopped.
- the present invention may comprise a set of helical coils, whose outer edges run along and are fixed to the circular wall and whose inner edges surround and are at an average distance from the central chimney, preferably greater than one quarter of the average distance between the central chimney and the circular wall, in order to allow the solid particles which move longitudinally in one direction, as they run along these helical turns, to move in the other direction in the space between these helical coils and the central chimney without getting too close to the openings of the central chimney.
- These helical coils which can form a continuous or discontinuous helical helix or be fragmented into a set of vanes, allow the solid particles to be passed from one side to the other of the circular reaction chamber many times over.
- the axis of rotation of the fluidized bed can be horizontal, inclined or vertical. If it is ho ⁇ zontal or inclined less than 45 °, preferably less than 30 °, the average velocity of the solid particles, their concentration and the pressure they exert on the thin layers of fluid are higher in the bottom of the reaction chamber. It is therefore preferable to divide the outer distribution chamber into several longitudinal sectors by longitudinal separation walls in order to be able to differentiate the fluid injection pressure in the different fluid mjectors as a function of their position in the reaction chamber.
- separation rings surrounding the central chimney at a distance therefrom, preferably at least one third of the mean distance between the circular wall and the central chimney to allow the solid particles to pass into this space without being too close to the exhaust opening of the central chimney, can be fixed against the circular wall to prevent the rapid fall of the solid particles.
- the pressure exerted by these solid particles against the upper surface of these separation rings will slow them down not only in their fall, but also in their rotational movement. This can be compensated, if necessary, if these rings are hollow and provided with fluid mjectors for injecting a fluid in thin layers along their upper surface in the direction of rotation of the solid particles.
- these separation rings can be replaced by helical coils, which can also be hollow and which can form a continuous or discontinuous helical helix or be fragmented into fins, fixed against the circular wall, the orientation of the slope coils or fins driving up the solid particles, which rotate rapidly along the circular wall, and the average distance between the inner edge of the turns and the central chimney, preferably greater than a quarter of the mean distance between the wall circular and the central chimney, allowing solid particles, which are mounted along the upper surface of these turns, to fall into this space without too close to the exhaust opening of the central chimney.
- This makes it possible to feed the solid particles into the bottom of the circular reaction chamber and to evacuate them at the top.
- Similar devices are described in Applications Nos. 2004/0186 and 2004/0612 of Belgian patents, filed on April 14 and December 12, 2004 in the name of the same inventor.
- the central chimney may pass only one side of the circular reaction chamber, preferably the upper side if the axis of rotation of the fluidized bed is vertical or inclined, and terminate before reaching the side. opposite. Its cross section may gradually decrease and its end located in the circular reaction chamber may be open or closed.
- the distribution chamber can be divided into successive annular sections by transverse annular separation walls in order to be able to differentiate the quality and the quantity of the fluids which are fed into the different sections and which cross the corresponding section of the fluidized bed. rotary and these fluids can be recycled in the same sections or in other sections, if the central chimney is also divided into successive sections, connected to tubes passing inside the central chimney and to separate these fluids separately .
- a plurality of circular reaction chambers can be put in series by connecting the solid particle outlet of a chamber to the inlet of the solid particles of the next chamber, and the solid particles can be recycled after being regenerated. if they are catalytic, by a suitable device after having spent a longer or shorter time, as needed, in the circular chamber or chambers of reaction.
- a suitable device is described in the patent application No. 2004/0612 of a Belgian patent, filed on December 12, 2004 in the name of the same inventor.
- the present invention makes it possible to pass through a dense rotary fluidized bed, with good separation between the solid particles and the fluid, by a very large amount of fluid and to rotate it rapidly to obtain a high centrifugal force, without the use of rotating mechanical means inside the reactor, even if the density of the fluid is low. It allows easy recycling, after appropriate treatment, fluid and / or solid particles, whose residence time can be adapted to the needs. It is particularly advantageous for processes which require a very good contact between the fluid and the solid particles, such as fast drying of solid particles in a compact reactor, and / or a large heat transfer capacity for controlling the temperature.
- FIG. 1 shows the schematic longitudinal section, in the plane of the axes (x) and (z), the axis (x) coinciding with the axis of rotation of the fluidized bed (00 ') and the axis (z), directed upwards, coinciding with the vertical, of a cylindrical reactor comprising three concentric walls, the outer wall (1), the central wall, called the circular wall (2) and the central wall (3), called the wall of the central chimney, the space between the outer wall and the wall central being closed by two annular side walls (4.1) and (4.2).
- the space (5) between the outer wall and the circular wall is the supply chamber of the fluid or fluids
- the space (6) between the circular wall and the central wall is the circular reaction chamber
- the space to the interior of the central wall is the central chimney (7).
- Tubes (8) are used to introduce the fluid or fluids, symbolized by the arrows (9) through the outer wall (1) or the annular side walls (4.1) and (4.2), inside the chamber supply (5) and tubes (10) to evacuate the fluid or fluids, symbolized by the arrows (11), of the central chimney (7).
- the tangential component of their speed is much greater than the radial component, but it is not visible because it is perpendicular to the plane of the figure.
- a conduit (16) is used to introduce solid particles, symbolized by small circles (17), through the side wall (4.1).
- the solid particles are driven by the fluid in a rotational movement and the centrifugal force holds them along the circular wall (2) where they form an approximately cylindrical surface fluidized bed (18).
- a conduit (19) discharges the solid particles (17) through the opposite annular sidewall (4.2).
- Annular walls (20) can divide the distribution chamber (5) into annular sections, (A), (B) and (C) in order to feed different qualities and / or at different pressures the fluid or fluids.
- the tubes (10) for discharging the fluid or fluids can penetrate inside the central chimney (3) which widens at its two ends, thus forming a kind of cyclone.
- the solid particles, which have been able to penetrate inside the central chimney and which turn rapidly, are concentrated along the conical walls (24), and are evacuated by the tubes (25) and possibly recycled.
- the fluidized bed can be divided by a regulating ring (26) optionally provided with one or more passages (27) against the circular wall allowing the solid particles to pass from one side to the other. If the feed rate of the solid particles (17) through the conduit (16) is higher than the transfer rate of the solid particles through the passages (27), the thickness (28) of the fluidized bed upstream of the The control ring (26) will increase until it is sufficient for the particles to overflow through the center of this ring to pass to the other side. And if the output rate of the solid particles through the conduit (19) is greater than the feed rate, the thickness (29) of the fluidized bed downstream of the regulating ring (26) will decrease until that the rarefaction of the solid particles automatically adjusts the output flow rate with the input flow rate of these particles.
- This device makes it possible to keep the volume of the fluidized bed upstream of the control ring (26), preferably located near the outlet (19), approximately constant if the feed rate of the solid particles is sufficiently high.
- the passages (27) also make it possible to evacuate all the solid particles from the circular reaction chamber when the feeding of the solid particles is stopped.
- the outlet (14) is preferably in the bottom of the reactor because the velocity and the concentration of the particles is maximum, and therefore the thickness of the fluidized ha is minimum, which reduces their probability of being driven into the central chimney (7).
- the thickness or width (31) of the reaction chamber is minimum downstream of the discharge opening (14) and it is maximum (32) upstream.
- the circular wall (2) is cylindrical in this illustration, and therefore its radius (33) is constant, while the radius of curvature of the wall of the central chimney (3) is variable. It is minimum (34) upstream of the outlet (14) and maximum (35) in downstream.
- the width (36) of the discharge opening (14) can be maximum in the middle of the reaction chamber and minimum near the annular side walls (4.1) and (4.2) so that the cross section of the central chimney is more raised at its ends, to facilitate the evacuation of the fluid (11). It should be noted that this width (36) is preferably zero against these walls, to prevent the solid particles slowed by these walls are driven into the central chimney.
- the reactor can be slightly inclined to increase the flow of particles to their outlet and thus reduce their residence time inside the reaction chamber.
- the surface of the fluidized bed is slightly tapered as a function of the amount of inclination and the ratio of the gravitational force to the centrifugal force.
- FIG. 2 shows the schematic cross-section along the plane of the axes (y) and (z) of the reactor of FIG. 1, in which the annular distribution chamber (5) is replaced by four distribution chambers (5.1). ) to (5.4), each connected to an injector or set of fluid injectors (12). This arrangement may be preferred when the number of injectors is low.
- the radius of curvature (35) of the wall (3) of the central chimney is smaller (34) on its part upstream of the discharge opening (14), giving it the appearance of a spiral, and that the width (31) of the circular chamber is preferably smaller downstream than upstream (32), because the flow rate of the fluid rotating around the chimney increases as it gets closer the exhaust opening (14).
- the surface (37) schematizes the section of a zone of turbulence generated by the possible inversion of the flow of the fluid, shown schematically by the arrows (38), downstream of the outlet (14) of the central chimney.
- This turbulence can cause the evacuation of solid particles, usually the finest, through the discharge opening (14).
- the injectors preferably a prime number, and / or that the distance between the injectors is not everywhere identical. It is also preferable to give the injectors and the circular wall a shape that minimizes the centripetal thrust of the fluid and promote its tangential thrust.
- the planes of the outlet openings of the injectors are almost identical with the planes parallel to the circular surface which is cylindrical, which favors the centripetal thrust due to the pressure of the fluid on the solid particles even if the angle fluid injection is small.
- FIG. 3 shows the schematic cross section of the zone around a fluid injector, illustrating how a small modification of the circular wall (2.2) downstream of a fluid injector (12), which becomes flat and tangential.
- in (B) at the extension of the circular wall (2.3), changes the orientation of the plane of its outlet, which therefore forms an angle (40) of about 90 ° with the plane wall (2.2).
- the thrust generated by the high pressure of the fluid (13.1) on the upstream side of its outlet, in (A), is therefore more directed tangentially to the circular wall.
- the solid particles highly concentrated, symbolized by small circles (17), form a compact assembly that slides along the circular wall (2.1) in the direction (41.1) upstream of the injector (12.1). Their encounter with the flow line (42.1) of the fluid (13), at the outlet of the injector, progressively deviate and accelerate along the flow line (41.2) and therefore their concentration gradually decreases, allowing a increasing fraction of the fluid to penetrate into this set of less and less compact solid particles by following the fluid flow line (42.2) which penetrates more and more (42.3) in the fluidized bed by deviating from the wall (2.3).
- the pressure of the fluid in the space (43) between the wall (2.2) and the flow line (41.2) of the solid particles must be sufficient to prevent the solid particles from clogging the outlet of the fluid and thus to deflect them according to this flow line (41.2).
- This illustration shows how the solid particles braked by the curved wall of the reaction chamber and, encountering the obstacle constituted by the injection of a jet of fluid, can form a compact assembly which substantially slows the normal sliding of these particles. solid particles and how the arrangement and orientation of the nozzle outlet opening and the fluid injection direction can minimize this braking and the centripetal pressure exerted by the fluid on the solid particles upstream of its outlet.
- the feed chamber is preferably delimited by a cylindrical wall (1) surrounding the circular wall (2) and is divided into longitudinal sectors of (5.1) to (5.4), by longitudinal walls (49), to allow to supply the different fluid injectors (12) at different pressures.
- the circular wall is flat between two injectors (12). It is therefore polygonal.
- the fluid is injected parallel to this surface, according to the diagram described in FIG. 5, in order to facilitate the sliding of the solid particles along the latter and to reduce their concentration upstream of the injection slots and thus to reduce the resistance. to advancement.
- the turbulence zone (37) which can develop along the leading edge (54) of the deflector (50) can cause solid particles in this space (53).
- the distance (51) being preferably greater than the thickness (36) of the discharge opening (14), the speed of the fluid (52), which accelerates these solid particles, increases gradually and the centrifugal force pushes them along the curved inner wall (55) of the hollow baffle (50).
- the trailing edge (56) of the deflector located at the distance (57) from the wall of the central chimney (3), is provided with one or more fluid injectors for injecting a thin layer of fluid at high speed. (58) more or less parallel at least 30 ° to the wall of the central chimney (3), producing a suction effect which returns to the reaction chamber (6) beyond the discharge opening (14). ), the solid particles that run along the inner wall (55) of the deflector. However, a turbulence zone (59.1) may develop between the fluid layer (58) and the wall of the central chimney (3) and generate a flow reversal that returns a portion of these particles to the outlet (14). .
- the pressure drop in the space (53) is small and therefore that the quantity of solid particles that the fluid stream (52) must accelerate is small and that the distance (57) is small, preferably less than half the distance (60) between the trailing edge and the circular wall.
- Another turbulence zone (59.2) may develop between the fluid jet (58) and the circular wall and cause a reversal of the fluid flow which increases the resistance to rotation of the fluidized bed upstream of this zone.
- the injection of the mmce layer of fluid (58) is parallel or slightly directed towards the wall of the central chimney (3).
- Figure 5 shows an enlargement of the area around the two mjectors (12.1) and (12.2).
- the solid particles form a barrier, which acts as a more or less permeable deflector depending on their concentration, and they confine the fluid between the flow line (42.2) and the polygonal wall (2.2) and the medium which keeps a high average speed, because it is confined in a narrow space, loses energy and therefore pressure as it transfers it to the solid particles along the flow line (41.3), accelerating them and thus decreasing their concentration. and their permeability increases, allowing the flow line (42.3) to move away from the wall (2.2) and thus the fluid, which has lost a lot of its energy, to slow down.
- the flow line (41.4) of the solid particles finished along the wall (2.2), along which they slide, slow down and their concentration increases before reaching the next injector (12.2). And so on ..
- the concentration of the flow of solid particles upstream of the mjectors is even greater than the distance between the fluid mjectors (12.1) and (12.2) is large and therefore that their number is small, and if the surface of the plane wall (2.2) was curved like the walls (2.1) and (2.3) in Figure 3, it would exert on the flows of solid particles (41.1) and (41.4) an additional pressure which would slow them down and which would increase thus their concentration and resistance to the rotation of the fluidized ht.
- the angle of deflection (66) between two mjectors is smaller the higher the number of mjectors, which dims the deflection of the solid particle streams (41.2) and (41.3) and therefore the pressure exerted on them.
- the angle (40) formed by the plane of the outlet of the injector (12.1) and the polygonal circular wall (2.2) is about 90 °, which makes it possible to inject the fluid (13.1) in a direction substantially parallel to this wall (2.2) and amsi to increase the amount of tangential cmetic momentum transferred to the solid particles.
- the circular reaction chamber can be connected in series with other similar chambers, the outlet (19) of the solid particles of the upstream chamber being connected to the inlet (16) of the next chamber.
- These circular reaction chambers may be side by side, in the extension of one another or superimposed. They can be mclmées or vertical.
- FIG. 6 shows the schematic longitudinal section, in the plane of the axes (x) and (z), the axis of (z) being vertical and coinciding with the axis of rotation (OO 1 ) of the fluidized beds, of the connection two sections of superimposed circular chambers. Since the surfaces (18) of the fluidized beds are conical, the fluidized beds of the reaction chambers (6) are subdivided into annular sections by separation rings (80) which support the portion of the fluidized bed directly above them. These are hollow and connected to the fluid distribution chambers (5) through openings (81) so that they can be injected by injectors (82) more or less parallel to the plane of the axes (x) and (y) and perpendicularly. at the axis of rotation (OO 1 ), fluids, symbolized by the arrows (83), in thin layers, which support and rotate the solid particles which rest on the upper part of the separation rings (80).
- the separation ring (85) at the bottom of the reaction chambers is extended to the wall of the central chimney (3), while the other separation rings (80) have a wide central opening, preferably greater than quarter of the average distance between the circular wall and the central chimney, to allow the solid particles to pass while remaining at a distance from the wall of the central chimney (3) not to be driven into the central chimney by the discharge opening (14).
- a stream of solid particles (90) flows from the bottom of the upper reaction circular chamber through the transfer conduit (91) which passes through the separation ring (85) and enters (92) into the upper portion of the lower chamber.
- the fluid flows (11) are evacuated from the central chimneys (7) by one or more conduits (93).
- the separation rings (80) can be replaced by helical turns.
- the solid particles which run along the circular wall and a helical turn will rise if the slope of the turn is in the ascending direction.
- it is possible to transfer the solid particles from the lower chamber to the upper chamber if the lower part of the transfer duct (91) is located along the circular wall where the pressure is highest and the upper part this duct (91) is located against the central chimney where the pressure is the lowest. Particles that are not transferred or removed from the top of the circular reaction chamber may fall back into the central space between the inner edge of the turns and the central stack.
- the helical coils may also be hollow and fed with fluid which is injected along their upper surface into the circular reaction chamber. They can form a continuous or discontinuous helical helix or be fragmented into a fraction of turns, similar to fixed fins, oriented in the ascending direction.
- FIG. 7 shows a diagram adapted to the drying of solid particles introduced by the tube (16) on one side of one of the two circular reaction chambers placed in series and exiting through the tube (19) placed at the end opposite of the second chamber, the transfer of these particles from one reactor to another is via the transfer conduit (91).
- the fresh and dry gas (100) is introduced through the tube (8.1) supplying the annular section (F) of the feed chamber located on the outlet side (19) of the solid particles. It is heated in contact with the hot solid particles that it cools while completing drying before their exit through the tube (19). This gas is then sucked by the compressor (101.1) through the outlet tube (11.1). It is recycled through the treatment units (102.1) and (102.2), for example heat exchangers and / or condensers, through the tubes (8.2) and (8.3) in the annular sections (E) and (D). .
- the solid particles may be catalysts that catalyze the chemical transformation of the fluid that passes through the fluidized bed.
- the fluid is progressively transformed. It is in contact during its first passage in the reactor with a used catalyst which can be regenerated and recycled by suitable devices, and during its last passage with a fresh or regenerated catalyst and the treatment units of (102.1) to ( 102.5) can also be used to evacuate an undesirable component, for example by absorption or condensation.
- FIG. 8 shows the diagram of the schematic longitudinal section of a reactor similar to that of FIG. 1, but whose axis of rotation of the fluidized bed is vertical or strongly inclined and whose central stack (7) ends at a some distance above the lower side (4.2).
- the bottom of the central chimney can be closed, as shown in Figure 8, or opened.
- the solid particles that enter the central chimney can be removed from the bottom during stops, but during operation, vortices can cause the solid particles that accumulate in the bottom of the circular reaction chamber. .
- This configuration can be advantageous when the amount of fluid to be evacuated is not too high.
- the surface (18) of the fluidized bed is conical, very slightly conical in this scheme, which assumes a very high centrifugal force, the fluid (13) must pass through a greater thickness of the fluidized bed in the lower part of the chamber. reaction and therefore his residence time is higher.
- the circular chamber (2) may also be conical to reduce this difference and / or the amount of fluid injected into the lower part of the circular reaction chamber may be increased, for example by increasing the number and / or the section of the fluid mjectors and / or the pressure in the annular section (C) of the distribution chamber.
- FIG. 8 also includes, by way of illustration, the diagram of an ejector fluid supply system for recycling a fraction of this fluid without the use of a compressor.
- This scheme is useful when the fluid needs to be recycled once or twice and the use of compressors is difficult, for example because of the corrosivity of the fluid or very high temperatures, for example for the dehydrogenation of the fluid.
- the feed fluid (100), possibly preheated, is injected under pressure into an ejector (105), to be injected (106) at a very high speed into the outlet tube (10.1) of the fluid to be recycled (11.1) in order to entraining it in a treatment unit (102), for example an oven, and recycling it into the reactor through the tubes (8), before being evacuated (11.2) through the tube (10.2) to treatment units .
- a treatment unit for example an oven
- FIG. 9 shows the diagram of the longitudinal section of a reactor similar to that of FIG. 1, comprising at each end of the central stack a centrifugal compressor, (108.1) and (108.2), symbolized by the propellers (109.1) and (109.2), which are driven by a common motor (110) through the drive shaft (111) which passes through the central chimney.
- the fresh fluid (112) is fed by the tube (8.1) located on the side of the outlet (19) of the solid particles, possibly passing through a processing unit (113), such as for example a moisture condenser.
- Fluid streams may be recycled in the same annular sections, for example to polymerize the catalyst particles suspended in mixtures of active fluids containing the monomer or monomers and may have compositions and / or temperatures different from one section to the next. other to obtain multimodal polymers and / or broad molecular distribution.
- Figure 10 illustrates a diagram that can be used for this type of application.
- the feed chamber and the central chimney are divided into four sections, respectively from (A) to (D) and (A 0 ) to (D 0 ), by the transverse walls of (20.1) to (20.3) and (115.1) to (115.3). These can be extended by the annular transverse walls of (116.1) to
- the fluids are gases, it is possible to spray fine droplets (120) of a liquid on at least a portion of the surface of the fluidized bed by one or more tubes (121) passing through the central stack.
- the fluid after being slowed down by the solid particles, the fluid must maintain an average tangential velocity sufficient to avoid significant reflux. For example it must perform an average of more than a half turn before exiting the reaction chamber in the diagrams described above which contain only one outlet opening (14) per section and where the fluid is injected more or less uniformly along the circular wall.
- Ke which may be greater than 1 when the fluid which has just been injected is confined between a "wall" of solid particles and the circular wall making it possible to convert a fraction of its kinetic energy and / or its pressure into kinetic momentum, is a variable coefficient of transfer efficiency of the tangential kinetic moment of the fluid towards the particles
- m, Vi and Vt are respectively the averages of the specific mass
- the injection and tangential velocity of the fluid Ei is the sum of the thicknesses (widths) of the outlet openings of the injectors passing through the annular slice
- Cc and M are the average concentration and the specific mass of the solid particles
- E and R are the average thickness (width) and the radius of the reaction chamber and
- Kf is a variable coefficient of friction representing the% of the kinetic moment that the solid particles must receive per unit time to reach and maintain the average rotation speed Vp.
- Equation (2) allows to write:
- the estimated average tangential velocity of the solid particles and that of the gas varies from about 4.6 to 4 m / s and from 5.5 to 5 m / s respectively and the coefficient X and the product of Cc * Kf / Ke vary only from 0.9 to 1 and from 7% to 8% / s, when the concentration of the solid particles is progressively increased by 10 to 30%, confirming that the efficiency of the kinetic momentum transfer from the fluid to the solid particles improves when the concentration of the solid particles, and thus the "walls" of solid particles channeling the fluid, increases.
- the losses of solid particles by the central chimney appear and increase rapidly when the average concentration of the solid particles approaches 28% and the coefficient X is close to 1.
- the fluid rotates about 5 times faster by completing on average more than 2 revolutions around the central chimney before entering and the centrifugal force is about 25 times higher.
- This therefore makes it possible to increase the concentration of the solid particles and / or to reduce the injection speed of the fluid and / or to increase the diameter of the reaction chamber while keeping a very good separation of the fluid and the solid particles.
- the performance can also be improved if the coefficient of friction, Kf, is smaller and if the coefficient of kinetic momentum transfer efficiency, Ke, is greater, which can be obtained by increasing the number of fluid mjectors. and improving the profile of the mjectors and the circular chamber.
- the fluid is a slightly lighter fluid than the solid particles, its number of revolutions, rotational speed, and centrifugal force increase further, which allows for an acceptable separation of fluid and solid particles, even if the critical velocity Vc is much smaller because of the small difference in specific masses.
- the device of the present invention can be applied to industrial processes of catalytic polymerization, drying, impregnation, coating, roasting or other treatments of solid particles suspended in a fluidized bed or cracking, dehydrogenation or other catalytic transformations of fluids or fluid mixtures passing through a fluidized bed.
- the cylindrical reaction chamber illustrated in FIG. 8 may have, for information only, 1 m in diameter, 4.5 m in length and 0.23 m in thickness (width), which gives it a volume of approximately 2.5 m 3 .
- the fluid (100) consisting of preheated cracking gas at high temperature, a specific gravity, at the injection temperature and pressure, of about 5 kg / m 3 , is injected at high speed.
- the catalyst powder which is fed by the tube (16) is driven by the fluid at an average rotation speed, Vp, approximately 13 m / s, giving a centrifugal force of 35 times the weight, generating a pressure on the cylindrical wall of approximately 30 000 Pa and allowing the fluid to pass through the fluidized bed at a speed of more than 2 m / s.
- the catalyst powder is discharged through the tube (19) and can be easily recycled after regeneration, with a cycle time ranging from a few minutes to many hours.
- the drying of grains of agricultural origin can be done according to the diagram of FIG. 9.
- the reaction chamber or drying chamber can have the same dimensions as those of the example above.
- the fresh air (112) is introduced by the tube (8.1), possibly through a moisture condenser (113), to pass through the end of the reaction chamber located on the grain outlet side (19) in order to heat up by cooling them and completing their drying.
- This air (11.1) is then sucked by the compressor or centrifugal fan (108.1) through the pipe (10.1) and recycled to the reactor via the pipe (8.2) after being further heated in the heater (102).
- this air (11.2) is sucked by the compressor or centrifugal fan (108.2) through the pipe (10.2) and recycled into the reactor via the pipe (8.3) after having been reheated by the heater ( 102). After being recycled again a few times, this moisture-laden and grain-cooled air, which is fed through the pipe (16) and has been reheated, is discharged at (114).
- the pressure in the reactor is lower than the atmospheric pressure, which is favorable for drying and mechanical means can easily transfer the dried grains for storage at atmospheric pressure.
- the air can be injected into the drying chamber at the same rate of 23 m 3 / s of the above example, or about 100 tons per hour. If it is recycled 5 to 10 times, this gives a fresh air quantity of 10 to 20 tons per hour and a contact time with the grains of about 5 to 10 times 0.1 seconds.
- the quantity of grains in the drying chamber can be about 500 kg, which gives an average residence time of 90 seconds for the drying of 20 tons per hour, which may be sufficient given the high speed and the low air pressure and the possibility of working at higher temperatures thanks to the short residence time and the cooling of the grains before leaving the reactor.
- This assembly can be made compact and easily transportable, which shows the advantage of being able to pass through a dense fluidized bed by a very large amount of fluid at high speed through the centrifugal force.
- the copolymerization of ethylene and octene is possible in the gas phase only if the pressure in the reactor is low, at most a few times the atmospheric pressure, because the partial pressure of the octene is limited to about 0, 2 atmospheres at 70 ° C. At these pressures, the amount of calories produced by these highly exothermic reactions can be removed only by using little active catalysts or by diluting the active gas mixture with a macif gas to slow down the rate of reaction, which increases the cost of the installation, or by passing through the fluidized bed by such a quantity of gas that it requires a rotating fluidized bed, for example according to the diagram described in FIG.
- the octene can be sprayed into fine droplets (120) in the reaction chamber through the tube (121) which passes through the central stack and / or fed in the gaseous form together with the fresh ethylene (119) and the fluid recycled by one or more of the tubes of (8.1) to (8.4).
- the cylindrical reaction chamber may, for example, have a diameter of 1.6 m; 10 m long and 0.32 m thick, comprising 29 injection slots 0.005 m thick, allowing the injection of approximately 50 m 3 / s of active fluids, if the injection speed of fluid is 35 m / s. If the pressure is about 3 times the atmospheric pressure, which allows a concentration of about 20% by weight of octene, the flow of recycled active fluids is about 700 tons per hour, which allows to evacuate the polymerization heat of about 10 to 20 tons per hour of polymer.
- the amount of polymer in the reaction chamber having a volume of about 12 m 3 is about 3 tons, giving a residence time of the polymer particles in the reaction chamber of 10 to 15 minutes, allows the use of very active catalysts.
- the rotational speed of the polymer particles can be about 11 m / s, which gives a centrifugal force of about 16 times the gravity, which allows to pass through the fluidized bed with a radial velocity of more than 1.5 m / s in about 0.2 seconds.
- This reactor can be put in series, for example following another reactor that can work at much higher pressures without comonomer or with lighter comonomers, in order to obtain multimodal polymers. It also makes it possible to progressively vary the composition and / or the temperature of the fluid passing through the rotating fluidized bed.
- IMPREGNATION OR COATING OF SOLID PARTICLES The scheme of FIG. 10 can also be used for the impregnation or coating of solid particles.
- the impregnating or coating fluid may be sprayed as fine droplets (120) into the portion of the reaction chamber which is located on the solid particle supply side by the tube (16).
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
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Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
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US12/066,609 US20080269432A1 (en) | 2005-09-15 | 2006-09-15 | Device For Injecting Successive Layers Of Fluid In A Circulating Fluidised Bed And Methods Using Same |
CA2644367A CA2644367C (fr) | 2005-09-15 | 2006-09-15 | Dispositif d'injection de fluide en couches successives dans un lit fluidifie rotatif et procedes utilisant ce dispositif |
JP2008530542A JP2009507633A (ja) | 2005-09-15 | 2006-09-15 | 一連の流体層を回転流動床中に注入するための装置と、この装置を用いた方法 |
EP06793555A EP1924348A1 (fr) | 2005-09-15 | 2006-09-15 | Dispositif d'injection de fluide en couches successives dans un lit fluidifie rotatif et procedes utilisant ce dispositif |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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BE2005/0443 | 2005-09-15 | ||
BE2005/0443A BE1016766A5 (fr) | 2005-09-15 | 2005-09-15 | Dispositif d'injection de fluide en couches successives dans un lit fluidifie rotatif et procedes utilisant ce dispositif. |
Publications (1)
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WO2007031573A1 true WO2007031573A1 (fr) | 2007-03-22 |
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PCT/EP2006/066404 WO2007031573A1 (fr) | 2005-09-15 | 2006-09-15 | Dispositif d'injection de fluide en couches successives dans un lit fluidifie rotatif et procedes utilisant ce dispositif |
Country Status (8)
Country | Link |
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US (1) | US20080269432A1 (fr) |
EP (1) | EP1924348A1 (fr) |
JP (1) | JP2009507633A (fr) |
KR (1) | KR20080045210A (fr) |
CN (1) | CN101309745A (fr) |
BE (1) | BE1016766A5 (fr) |
CA (1) | CA2644367C (fr) |
WO (1) | WO2007031573A1 (fr) |
Cited By (9)
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WO2007122211A1 (fr) * | 2006-04-21 | 2007-11-01 | Total Petrochemicals Research Feluy | Dispositif et procede d'injection de fluide dans un lit fluidifie rotatif |
EP1967261A1 (fr) * | 2007-03-02 | 2008-09-10 | Total Petrochemicals Research Feluy | Dispositif et procédé d'injection de fluide dans un lit fluidifié rotatif. |
WO2008107404A1 (fr) * | 2007-03-02 | 2008-09-12 | Total Petrochemicals Research Feluy | Dispositif et procede d'injection de fluide dans un lit fluidite rotatif |
WO2009141372A1 (fr) * | 2008-05-23 | 2009-11-26 | Total Petrochemicals Research Feluy | Procédé de transformation thermique et/ou catalytique de fluides réactifs traversant différents volumes longitudinaux de réaction d'un lit fluidifié rotatif |
WO2010022232A2 (fr) * | 2008-08-20 | 2010-02-25 | Tiax Llc | Réacteurs chimiques |
US20120039755A1 (en) * | 2007-03-06 | 2012-02-16 | Univation Technologies, Llc | Methods and Devices for Polymerization |
WO2019023038A1 (fr) | 2017-07-28 | 2019-01-31 | Uop Llc | Procédés de mise en contact de fluides dans une cuve à courant descendant |
EP3658271A4 (fr) * | 2017-07-28 | 2021-01-20 | Uop Llc | Procédés et appareil de mise en contact de fluide dans un réservoir à écoulement descendant |
EP3658273A4 (fr) * | 2017-07-28 | 2021-01-20 | Uop Llc | Procédés et appareil de mise en contact de fluide dans un réservoir à écoulement descendant |
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KR20070087101A (ko) | 2004-12-15 | 2007-08-27 | 브로끄빌 악셀 드 | 회전 유동층 장치 및 이 장치의 사용 방법 |
BE1017234A3 (fr) * | 2006-07-25 | 2008-05-06 | Broqueville Axel De | Dispositif d'evacuation d'un fluide avec refoulement centrifuge. |
KR101029185B1 (ko) * | 2008-10-08 | 2011-04-12 | 한국수자원공사 | 회전류를 이용한 무동력 혼화장치 |
ITMI20082183A1 (it) * | 2008-12-10 | 2010-06-11 | Martini S P A De | Apparecchiatura a flusso vorticoso per realizzare un' interazione tra un fluido ed un solido e processo di interazione fluido-solido impiegante la stessa |
EP2701851B1 (fr) * | 2011-04-29 | 2024-04-24 | Becton Dickinson and Company | Système fluidique d'immobilisation et de collecte de particules en continu et leur procédé d'utilisation |
CN107952401B (zh) | 2016-10-17 | 2020-02-04 | 北京华石联合能源科技发展有限公司 | 一种悬浮床加氢冷壁反应器 |
CA3062449A1 (fr) * | 2017-05-01 | 2018-11-08 | Universite Catholique De Louvain | Dispositif de traitement de particules dans un lit fluidise rotatif |
US10486127B2 (en) * | 2017-07-28 | 2019-11-26 | Uop Llc | Methods and apparatus for fluid contacting in a downflow vessel |
CN109059298B (zh) * | 2018-07-05 | 2020-11-03 | 中国矿业大学 | 流体自混匀装置 |
CN108993325B (zh) * | 2018-08-28 | 2020-12-01 | 福州大学 | 一种旋转催化床及其使用方法 |
US20220134300A1 (en) * | 2019-02-13 | 2022-05-05 | Sabic Global Technologies B.V. | Three-dimensional annular rotating fluidized bed fluid-solids contactor |
KR102283250B1 (ko) * | 2020-12-24 | 2021-07-29 | (주)인벤티지랩 | 용매 제거 장치 및 이를 이용한 미소구체 제조 방법 |
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US20120039755A1 (en) * | 2007-03-06 | 2012-02-16 | Univation Technologies, Llc | Methods and Devices for Polymerization |
US8192690B2 (en) * | 2007-03-06 | 2012-06-05 | Univation Technologies, Llc | Methods and devices for polymerization |
WO2009141372A1 (fr) * | 2008-05-23 | 2009-11-26 | Total Petrochemicals Research Feluy | Procédé de transformation thermique et/ou catalytique de fluides réactifs traversant différents volumes longitudinaux de réaction d'un lit fluidifié rotatif |
EP2127738A1 (fr) * | 2008-05-23 | 2009-12-02 | Total Petrochemicals Research Feluy | Procédé de transformation thermique et/ou catalytique de fluides réactifs traversant différents volumes longitudinaux de réaction d'un lit fluidifié rotatif. |
WO2010022232A3 (fr) * | 2008-08-20 | 2010-05-27 | Tiax Llc | Réacteurs chimiques |
US7906016B2 (en) | 2008-08-20 | 2011-03-15 | Tiax Llc | Chemical reactors |
WO2010022232A2 (fr) * | 2008-08-20 | 2010-02-25 | Tiax Llc | Réacteurs chimiques |
WO2019023038A1 (fr) | 2017-07-28 | 2019-01-31 | Uop Llc | Procédés de mise en contact de fluides dans une cuve à courant descendant |
EP3658267A4 (fr) * | 2017-07-28 | 2021-01-20 | Uop Llc | Procédés de mise en contact de fluides dans une cuve à courant descendant |
EP3658271A4 (fr) * | 2017-07-28 | 2021-01-20 | Uop Llc | Procédés et appareil de mise en contact de fluide dans un réservoir à écoulement descendant |
EP3658273A4 (fr) * | 2017-07-28 | 2021-01-20 | Uop Llc | Procédés et appareil de mise en contact de fluide dans un réservoir à écoulement descendant |
Also Published As
Publication number | Publication date |
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KR20080045210A (ko) | 2008-05-22 |
CA2644367A1 (fr) | 2007-03-22 |
US20080269432A1 (en) | 2008-10-30 |
EP1924348A1 (fr) | 2008-05-28 |
BE1016766A5 (fr) | 2007-06-05 |
CA2644367C (fr) | 2013-06-04 |
CN101309745A (zh) | 2008-11-19 |
JP2009507633A (ja) | 2009-02-26 |
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