PROCESS AND DEVICE FOR THE SEPARATION OF A CATALYST USING A CYCLONE IN A FCC PROCESS BACKGROUND OF THE INVENTION The present invention relates to the separation of particles of catalytic materials from gaseous materials in a fluid catalytic disintegration (FCC) process. Cyclonic methods for separating solids from gases are well known, and are commonly used in the hydrocarbon processing industry, in which catalyst particles come into contact with gaseous reactants, to effect chemical conversion of gas stream components, or changes physical particles that come in contact with the gas streams. The FCC process presents a familiar example of a process that uses gas streams to come into contact with a finely divided stream of catalyst particles, make contact between gas and particles, and benefit from efficient separation of vapor catalyst particles. of products . Filtration methods or additional downstream separation devices are necessary to remove catalyst particles that the FCC unit can not recover. The catalyst not recovered from the FCC process represents a double loss. It is necessary to replace the catalyst, which represents a material cost, and the lost catalyst can cause erosion in the equipment that is downstream. Accordingly, methods for efficiently separating catalyst particle materials from gaseous fluids in an FCC process are very useful. The discharge of the gaseous fluids from the FCC reaction unit initiates the separation of solid catalyst particles. The most common method for separating solid particles from a gas stream uses centripetal separation. The most well-known centripetal separators impart a tangential velocity to gases containing solid particles, which forces the solid particles to move away from the gases, which are lighter, to extract the gases upwards, and collect the solids downwards. . Patent US-A-5, 584, 985 Bl discloses the initial rapid separation of the discharge from the reaction conduit, by discharging the feed and catalyst particles from a riser to a separation vessel through an arched extension and tubular, to impart a helical movement to the gases and catalyst particles. The helical and swirling movement of the materials in the separation vessel effect an initial separation of the catalyst particles from the gases. The swirling movement of the mixture continues, while rising to the gas recovery conduit. At the end of the gas recovery conduit, cyclones extract the mixture to further separate the catalyst particles from the gases. This arrangement is known as the Vortex Separation System ÜOP (VSSSM). Cyclones generally comprise a tangential inlet to the outside of a cylindrical vessel forming an outer wall of the cyclone. The cyclone inlet and the inner surface of the outer wall cooperate to create a spiral or vortex flow path of gaseous materials and catalyst in the cyclone. The centripetal acceleration on the outside of the vortex causes the catalyst particles to migrate out of the barrel, while the gaseous materials enter the interior of the vortex, eventually discharging through an upper outlet. The catalyst particles, which are heavier, accumulate in the side wall of the cyclone barrel, and finally fall to the bottom of the cyclone and exit through an outlet and a recovery conduit, to be recycled through the FCC device. Providing cyclones in a container requires a separation between cyclones, to allow adequate access for installation and maintenance purposes. The separation between cyclones becomes an important consideration when installing more cyclones in a container.
Accordingly, it is an object of the present invention to improve the efficiency of the process of separating solid vapor particles in an FCC unit. It is another object of the present invention to further improve the efficiency of separation in an FCC unit using a VSSSM with one or more cyclones. A further object of the present invention is to ensure an adequate separation between cyclones in a container containing them. SOMRRIO DE LA INVENCIÓN It has been found that orienting the angular direction of a swirling motion in an initial separation vessel as a VSSSMf to direct it out of the cyclone increases the separation efficiency. To achieve this, the direction of the swirl in the container may be opposite to the angular direction of a swirling motion in a downstream cyclone. The same objective can be achieved with the same direction of the vortex in both the container and the cyclone, as long as the entrance of the cyclone intersects tangentially with the container, so that the particles of the container enter the cyclone in a path parallel to the Center line of cyclone entrance. If the swirling movements in the VSSSM and the cyclones coincide and the entrance of the cyclone does not receive the mixture tangentially, less contact occurs between the mixture entering the cyclone and the interior surface of the exterior wall imparting the swirling motion to the mixture. . Instead, the mixture tends toward a center of the cyclone that contains the inlet to the steam outlet duct. As a result, part of the mixture entering the cyclone can leave the cyclone before receiving a swirling movement of the outer wall, and consequently leaving the cyclone with a minimum additional separation of the solid particles of the gaseous vapors. By directing the flow of the container in a direction parallel to the outside of the center line of the cyclone inlet, the outer wall of the cyclone is more likely to impart a swirling motion to the mixture before it comes into contact with the center of the cyclone. Therefore, a greater separation efficiency is obtained. To co-direct the swirl angle in the container and the cyclone, the entrance of the cyclone requires a tangential connection with the container in order to obtain the desired direction for the entry of the mixture into the cyclone. By counter-directing the vortex movements in the cyclone and container, a radial or tangential orientation of the cyclone relative to the container can achieve the desired direction of entry of the mixture into the cyclone. To counter-steer the swirl movements, a VSSSM orients an extension for swirling so that the opening at the end of the swirling extension is angularly oriented toward the wall of the cyclone inlet that is contiguous to the curved wall of the cyclone. In this manner, the outlet of the VSSSM of the swirling extension directs the mixture in the direction of the outer wall of the cyclone or the adjoining surface of the cyclone inlet. With the counter-directed swirl movement, more efficiency is obtained by tangentially configuring the entrance of the cyclone with one side upstream of the vortex of the cyclone and the vortex VSSSM, and the opposite side of the entrance of the cyclone that is current below the vortices of the cyclone. cyclone and the VSSSM. Accordingly, in one embodiment, the present invention is a process for the fluid catalytic disintegration of a hydrocarbon feedstock. The process passes a feed charge of hydrocarbons and solid catalyst particles to a reaction conduit to produce a mixture of solid catalyst particles and gaseous fluids. Inducing the mixture of catalyst particles and gaseous fluids to swirl in an angular direction within a separation vessel decreases the concentration of catalyst particles, and increases the concentration of gaseous fluids in the mixture. The container tangentially empties the mixture from the container to at least one cyclone through a cyclone inlet having an upstream side and a downstream side relative to the angular direction of the vortex in the container. In accordance with the present invention, the angular direction of the vortex tangentially empties the mixture to the entrance of the cyclone, in such a direction that a tangent to the container projecting from an intersection point of the upstream cyclone inlet with the container projects parallel to the entrance of the cyclone. cyclone, or away from the center of the cyclone. An eddy movement can be induced to the mixture in an angular direction in the cyclone opposite to the angular direction in the container, or it can be swirled in the same direction in the cyclone or container, although tangentially entering the cyclone. In another embodiment, the present invention is a device for the fluid catalytic disintegration of a hydrocarbon feedstock. The device comprises a reaction conduit for contacting a hydrocarbon feedstock with solid catalyst particles and thus producing a mixture of solid catalyst particles and gaseous fluids. The reaction conduit has a vortex outlet configured to induce a vortex movement of solid catalyst particles and gaseous fluids in a first angular direction in the container. A cyclone in communication with the swirl outlet has an eddy-inducing outer wall that is curved to induce a swirling movement of solid catalyst particles and gaseous fluids in a second angular direction and a cyclone inlet tangentially extending from the outer wall through a tangential wall. The entrance of the cyclone intersects with the container such that the first direction of the swirling movement drains the mixture to the cyclone in a direction parallel to, or toward, the tangential wall of the cyclone inlet. The reaction conduit may have a curved, tubular, swirling extension that can be connected to the reaction conduit, and the swirling extension has a curved outer wall, whereby the swirling extension of the curving movement is curved in a angular orientation opposite to the angular orientation in which the outer wall of the cyclone is curved. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic cross-sectional view of an FCC unit. Figure 2 is a cross-section of Figure 1, taken on segment A-A. Figure 3 is a cross section of Figure 1, taken on segment B-B. Figure 4 is a partial view of Figure 2, showing the flow path of the material particles when the swirling movements are equal.
Figure 5 is an alternative cross section of Figure 1, taken on segment B-B. Figure 6 is a partial view of Figure 2, showing the flow path of the material particles when the swirling movements are opposite. Figure 7 is another alternative cross section of segment A-A in Figure 1. DESCRIPTION OF THE PREFERRED MODALITY Figure 1 is the illustration of an FCC unit that will be the basis for illustrating various modalities. Two alternative cross sections are taken on segment AA of Figure 1, which are Figures 2 and 7. Also, two alternative cross sections are taken on segment BB, which are Figures 4 and 6. The FCC unit includes an arrangement of separation in a reactor vessel 10. A conduit in the form of reactor elevator 12 extends upwards, through a lower portion of the reactor vessel 10 in a typical FCC arrangement. The central duct or reactor riser 12 preferably has a vertical orientation within the reactor vessel 10 and may extend upwardly through the bottom of the reactor vessel, or downwardly from the top of the reactor vessel. The reactor riser 12 terminates in a separating vessel 11 in a swirling movement outlet in the form of a swirling movement extension 14. The swirling movement extension 14 is a curved tube whose axis of curvature is parallel to the swirl elevator. reactor 12. (See Figure 4). The swirling motion extension 14 also has one end connected to the reactor riser 12 and another open end comprising a discharge opening 16. The swirling extension 14 discharges a fluid mixture through the discharge opening 16. gaseous comprising disintegrated product and solid catalyst particles. The tangential discharge of gases and catalyst from the discharge opening 16 produces a helical swirl movement with respect to the interior of the separation vessel 11. The centripetal acceleration associated with the helical movement causes the catalyst particles, which are heavier, to go the outer portions of the separation vessel 11. The catalyst particles from the discharge openings 16 are collected at the bottom of the separation vessel 11 to form a dense bed of catalyst 17. The gases, having a lower density than the particles solid catalytic converters, change direction more easily, and initiate an upward spiral, where gases ultimately move towards a gas recovery conduit 18 through an inlet 20. Gases entering a gas recovery conduit 18 through an inlet 20 will generally contain a light charge of catalytic particles dor. The inlet 20 recovers gases from the discharge openings 16, in addition to extracting gases in a suction section 27. The loading of catalyst particles in the gases entering the gas recovery conduit 18 is generally less than 16 kg / m3, and typically less than 2 kg / m3. The swirling movement imparted by the swirling motion extension 14 continues in the same angular direction through the gas recovery conduit 18. The gas recovery conduit 18 passes the separated gases to the cyclones 22 which effect an additional extraction of catalyst particles gas material in the gas recovery conduit 18. The cyclones 22 create a swirling motion within the cyclones to establish a vortex separating solids from gases. A product gas stream, relatively free of catalyst particles, exits the cyclones 22 through the steam outlets 24 and the outlet pipes 49. The product stream then exits the reactor vessel 10 through the outlet 25. catalyst recovered by the cyclones 22 exit the bottom of the cyclone through the hoppers 19 and recuperators 23, and pass to a lower portion of the reactor vessel 10, where it forms a dense catalyst bed 28 outside the separation vessel 11. The catalyst solids in the dense catalyst bed 28 enter an extractor section 27 through the windows 26. catalyst solids pass down through the extractor section 27. An extraction fluid, which is typically steam, enters a lower portion of the extractor section 27 through at least one distributor 29. The countercurrent contact of the catalyst with the Extraction fluid through a series of extraction gates 21 displaces gases product of the catalyst by continuing down through the separation vessel 11. The extruded catalyst from the extractor section 27 passes through a conduit 31 to a catalyst regenerator 37 which regenerates the catalyst by high-temperature contact with an oxygen-containing gas, by oxidizing coke deposits in the catalyst surface. After regeneration, the catalyst particles enter the bottom of the reactor riser 12 through a duct 33 where a fluidizing gas from a distributor 35 pneumatically transports the catalyst particles upwards through the riser 12. According to the mixture of catalyst and carrier gas continues its ascent by the riser 12, the nozzle 40 injects feed charge to the catalyst, which contact vaporizes the feed charge to provide additional gases exiting through the discharge openings 16 in the previously described manner. Figure 2 illustrates cyclones 22 in greater detail by a cross-sectional view taken on segment AA in Figure 1. Each cyclone 22 comprises a radial inlet of cyclone 30 and a barrel chamber 32. A steam outlet 24 disposed in the center of the barrel chamber 32 provides an outlet for the product gases together with only small amounts of cyclone material particles 22, The hopper 19 provides a discharge of material particles from the cyclone 22 to the dense catalyst bed 28, as described with respect to Figure 1. The radial entry of cyclone 30 is defined by a long and straight side wall 34 that provides a tangential wall of the cyclone inlet. The side wall 34 preferably has a continuous gradual transition 34a which provides a continuous curve to the outer wall 38. In a steep transition 36a, a short and straight side wall 36 intersects at an acute angle with the curved outer wall 38 defining the chamber barrel 32 of the cyclone 22. The radial entry of cyclone 30 to the cyclones 22 exits radially from the gas recovery conduit 18. The radial outlet of the gas recovery conduit 18 to the cyclone 22 is generally characterized by a "C" of middle line laterally bisecting the radial entrance of cyclone 30, which exits where the gas recovery conduit 18 essentially intersects the center of section of the gas recovery conduit 18. In operation, a mixture of gases and particulate material exits the gas conduit. gas recovery 18 towards the cyclone radial inlet 30 of the cyclone 22. The long straight side wall 34 and the curved outer wall 38 provide a surface c Ongoing it imparts a swirling motion to the mixture entering the cyclone 22 to generate the vortex that separates the material particles from the gases. Figure 3 shows the orientation of the curvature of the swirling extension 114. A mixture containing particles of material and gaseous fluids ascending through the reactor riser 12 leaves the reactor riser 12 through the extension of swirling movement 114 towards the discharge opening 16, forming a swirling movement in an angular direction clockwise. As the mixture leaves the separation vessel 11 and is transported through the gas recovery conduit 18, the mixture will retain the same swirling movement in an angular direction clockwise. Figure 4 shows how the material particles 50 that exit radially from the gas recovery conduit 18 enter the cyclone 22. In Figure 4 only one cyclone is shown, for simplicity purposes. A swirling movement in the clockwise direction WD "of the mixture containing particles of material 50 in the gas recovery conduit 18 is generated by the swirling motion extension 14 having the curvature orientation shown in Figure 3. The curvature orientation of the swirling motion extension 14 is the angular direction defining from the entrance to the exit, the straight side wall 34, the gradual transition 34a and the curved outer wall 38 impart to movement in swirl in clockwise angular direction WE "to the mixture in the cyclone 22. When the swirling motion extension 114 has the same curvature orientation as the curvature orientation of the cyclones 22, they impart the same swirling movement in angular direction clockwise "D" in the gas recovery conduit 18 and "in the cyclone 22, as in the prior art. 50 of materials entering the cyclone have a tendency to approach the vapor outlet 24 instead of following the interior surface of the curved outer wall 38 to generate the desired swirl movement. Accordingly, it is thought that part of the material particles 50 exit through the vapor outlet 24 before being incorporated into a vortex that separates the particles of material 50 from the gases, thereby decreasing the efficiency to separate gas from the particles. of material. The tangent line J in Figure 4 more completely defines the undesired direction of the mixing flow that characterizes the prior art. The tangent line J projects on a tangent to the container wall of the gas recovery conduit 18 which starts at the point L, where the side wall 34 intersects the conduit 18. Regarding the direction of the swirl in the conduit 18, the side wall 34 forms the upstream side of the entrance of the cyclone 30. The configuration described in Figure 4 projects the tangent line J towards the center of the cyclone 22, which coincides with the steam outlet 24, to effect the objects of the present invention, Figure 4 also shows another arrangement of the container wall 34 to 34 '. Moving the side wall 34 to the position 34 'changes the point of intersection upstream L to the point L', so that the wall 3 'defines a tangent from the point of intersection L', and although it is not shown, the change of the entrance 30 gives the cyclone entrance 30 a central line parallel to the line 34 '. In this way, a tangent drawn on the line 34 'does not project towards the center of the cyclone at 22, but is now parallel to the center line of the entrance of the cyclone, so that the path of the incoming mixture is parallel to the entrance of cyclo. The object of the present invention can also be achieved by reversing the direction of the vortex in the container. Figure 5 shows a curvature orientation of the extension of movement in swirls 14 contrary to that of the extension of movement in swirls in Figure 4, and contrary to the curvature orientation of the cyclone 22 in accordance with one embodiment of the present invention. The same reference number designates elements common to Figures 3 and 5. The discharge openings 16 in Figure 5 are oriented in opposition to the discharge openings 16 in Figure 3. Accordingly, the orientation of the curvature of the extension of movement in swirls 14 is contrary to the orientation of the curvature of cyclone 22. Figure 5 shows four swirling movement extensions 14. It can be used more or less extension of movement in swirls. Figure 6 shows the interaction between the angular directions of the swirling movements in the gas recovery conduit 18 and the cyclone 22. The mixture exiting the discharge openings 16 in the swirling extension 14 in Figure 5 will acquire a swirling movement in an angular direction opposite to the clockwise direction "F". The mixture will continue to swirl in a counter-clockwise motion as the mixture rises through the gas recovery conduit 18. However, the swirling movement in the cyclones 22 shown in Figure 2 will have an angular direction clockwise "E". As the mixture containing particles of material 50 enters the cyclone radial inlet 30 of the cyclone 22, the angular momentum of the sidewall mixture 34 instead of the center of the barrel chamber 32. Consequently, the long and straight side wall 34 and the curved outer wall 38 can impart a swirling movement with angular direction clockwise "E" to a larger mixing portion, thereby incorporating more of the mixture into the vortex separating the particles of material 50 from the gases The particles of material 50, heavier, swirl in the curved outer wall 38 of the cyclone 22, where they eventually fall into the hopper 19 to enter the recuperator 23 and finally be incorporated into the dense catalyst bed 28. The fact that the extension of movement in swirls 14 swirl the mixture in a direction opposite to the angular direction clockwise, and cyclones swirl the mixture in an angular direction clockwise is not a limiting factor, since that the opposite relationships between the angular directions of the swirling movements from the extent of movement in swirls 14 and the cyclones 22 is a useful way of preventing the particles from embedding themselves in central portions of the cyclone. Examining again the trajectory of the particle flow on a tangent, Figure 5 shows a tangent line M projecting tangentially from the conduit 18 and originating from the point N, where the side wall 36, which is now the upstream wall of the cyclone inlet 30, intersects with the conduit 18. The end of the tangent line M projects towards the outside portion of the inlet 30, against the side wall 34, and away from the center of the cyclone 22. Accordingly, the end of the tangent line M moves away from the center of the cyclone 22. Figure 7 shows yet another embodiment of the present invention, which provides an essentially tangential exit towards the cyclones from the gas recovery conduit 18, and in which the movement in a swirl with angular direction opposite to the clockwise direction "F" of the mixture in the gas recovery conduit 18 is contrary to the swirling movement in the angular direction in the direction of the "H" clock induced in cyclones. Figure 7 is taken as an alternative cross section of Figure 1 taken on segment A-A. The reference number for each element in Figure 7 related to an entry whose configuration is different from the corresponding element in Figure 2 will be designated by adding 200 to the reference number in Figure 2. Other elements common to Figures 2 and 7 will retain the same reference number. The section in segment BB of Figure 1 which corresponds to the embodiment illustrated in Figure 7 is illustrated in Figure 5. The extension of movement in swirls 14 imparts a swirling movement of angular direction contrary to clockwise "F" to the mixture containing particles of material 50 discharged from the reactor elevator 12. This angular direction counter to the clockwise "F" of the swirling movement continues as the mixture is transported through the gas recovery conduit 18. The The mixture exits the gas recovery conduit 18 through the inlets of the cyclones 230 which are essentially tangential to the gas recovery conduit 18. The mixture enters each cyclone 22 through a tangential entrance of the cyclone 230 defined by the wall. long and straight lateral 234 and the short and straight side wall 236. A "I" line, coplanar or collinear with the short and straight side wall 236 is essentially tangential to the perf cross section of the gas recovery conduit 18. The short and straight side wall 236 may be slightly spaced inwards from the tangent to facilitate being welded to the gas recovery conduit 18. This arrangement allows the installation of more cyclones 22 in the reactor vessel 10, and with greater separation between each of the cyclones 22. The long and straight side wall 234 is contiguous and has a continuous gradual transition 234a with a curved outer wall 238 that defines the barrel chamber 232 of the cyclone 22. The short side wall and straight 236 has a sharp abrupt transition 236a with curved outer wall 238. A mixture with a higher concentration of material particles 50 than that which enters cyclone 22 exits down through hopper 19r as a mixture with higher concentration of gaseous fluids that that which enters the cyclone 22 exits upwardly through the steam outlet 24. The long straight side wall 234 and the curved outer wall 238 cooperate to impart a swirling motion to the mixture entering cyclone 22 , which establishes a vortex that separates the particles of material 50 from the gases. In this embodiment, the swirling movement with angular direction opposite to the clockwise direction "F" imparted by the extension of movement in swirls 14 from the reactor elevator 12 is contrary to the angular direction opposite to the clockwise "H" of the movement In a swirl imparted by the cyclones 22. Accordingly, the particles of material 50 in the mixture are more likely to meet first with the long straight side wall 234 or the curved outer wall 238, and are subject to the vortex motion of the vortex , which first meets the center of the cyclone 22 and is discharged from the cyclone with gases through the steam outlet 24. Consequently, and since it is more probable that greater proportions of the mixture are subject to the swirling movement to tend towards the center of the cyclone, a greater separation efficiency is obtained. This arrangement also provides opposing angular directions of swirling movement in the gas recovery conduit 18 and cyclones 22, as previously accepted, by modifying the orientation of the cyclones 22 instead of the swirling extensions 114. EXAMPLE I Computed flow dynamics (CFD) models were calculated using a FLÜENT program to study separation efficiencies for three sets of conditions. The following were assumed for the three sets of conditions: a minimum catalyst size of 40 microns, a density of gas of 2.75 kg / m3, a gas velocity of 0.02 cp, a speed of the mixture leaving each swirling extension of 20.8 m / sec, a pressure of 299 kPa and a temperature of 549 ° C. The first set of conditions involved a model where the radial entry of cyclones 30 to the cyclones 22 was disposed with respect to the gas recovery conduit 18 as shown in Figure 2, and the swirling movement extensions 114 were arranged as shown in Figure 3. This model focused on the case where the angular direction of the swirling movement imparted by the swirling motion extensions was equal to the angular direction of the swirling movement imparted by the cyclones 22 as shown in FIG. Figure 4. The CFD model indicated that in this model, 21% of the mixture that entered the cyclone moved towards the center of the cyclone instead of moving towards the periphery of the cyclone to join the vortex and thus further separate the gases from the cyclones. solids, which represented a loss of efficiency. A second set of conditions had the same cyclone configuration shown in Figure 2 and used in the previous model. However, swirl movement extensions 14 were oriented as shown in Figure 5, so that the angular direction of the swirling movement generated by each swirling motion extension 14 was opposite to the angular direction of swirling movement generated by cyclones 22 as shown in Figure 6. The model indicated that only 10% of the mixture entering the cyclone moved towards the center of the cyclone, where the steam outlet is arranged, without moving towards the vortex for its further separation. EXAMPLE II A model reactor vessel with five cyclones was made. The entrances to the cyclones comprised a long wall with a continuous and gradual transition to the curved outer wall defining the cyclone barrel, and a short and straight side wall with a steep and sharp transition to the curved outer wall. The long and straight side wall was disposed essentially tangential to the gas recovery conduit that transports the mixture from a reactor elevator to the cyclones. In an attempt to prevent the mixture from entering the cyclone without passing through the vortex in the cyclone, the cyclone inlet was built relatively long, 45.7 km. The separation between cyclones, at their maximum separation distance, was 10.7 cm. In another model, five cyclones were installed in a reactor vessel similar to the previous model, with the exception that the length of the short and straight side wall was only 32.0 cm, and that the short and straight side wall was arranged essentially tangentially. to the gas recovery conduit, as shown in Figure 7. Accordingly, the orientation of the curvature of the cyclones in the second model was opposite to the orientation of the curvature of the cyclones in the first model. However, in the second model, the space between cyclones at its maximum separation distance was 45.7 cm. Therefore, when reversing the orientation of cyclones, the separation between cyclones increases by almost 300%. Accordingly, the second model provides more flexibility to arrange a given number of cyclones in a reactor vessel, in addition to reversing an orientation of the curvature of the cyclones to oppose the orientation of the curvature of the extension of movement in eddies in an exit of a reactor duct, to increase the efficiency of the separation. The first set of conditions involved a model where the radial inlet of cyclones 30 to cyclones 22 was disposed relative to gas recovery conduit 18, as shown in Figure 2, and swirling extensions 114 were arranged as in Figure 3. This model investigated a case where each extension of movement in eddies imparted the same angular direction as the cyclones 22 shown in Figure 4 and the lateral wall cyclone entry corresponded to that indicated by the number 34. The CFD model indicated that in this model, 21% of the mixture that entered the cyclone moved towards the center of the cyclone instead of moving towards the periphery of the cyclone to join the vortex and further separate the gases from the solids, which represented a loss in efficiency. A second set of conditions had the same cyclone configuration shown in Figure 2 and used in the previous model. However, swirl movement extensions 14 were oriented as shown in Figure 5, so that the angular direction of the swirling movement generated by each swirling motion extension 14 was opposite to the angular direction of swirling movement generated by cyclones 22 as shown in Figure 6. The model indicated that only 10% of the mixture entering the cyclone moved towards the center of the cyclone, where the steam outlet is arranged, without moving towards the vortex for its further separation.