• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    This invention relates to an apparatus and method for rapidly separating particulate solids from a mixed-phase solids-gas stream which may be at velocities up to 150 ft./ sec. and at hight temperature. Specifically, the device is designed for incorporation at the discharge of solid-gas reacting systems having low residence time requirements and carried out in tubular type reactors (13). Separation is effected by projecting solids by centrifugal force against a bed of solids as the gas phase makes a 180° directional change (15), said solids changing direction only 90° relative to the incoming stream (14).
    公开号:SU1085499A3
    申请号:SU813255244
    申请日:1981-03-05
    公开日:1984-04-07
    发明作者:Джон Гартсайд Роберт；Николас Воебке Герман
    申请人:Стоун Энд Вебстер Инджиниринг Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    2. The separator according to claim 1, about the fact that the chamber is made with a height of at least D |, H width (0.75-1.25) D | and the gas outlet is located between the inlet for the mixed flow and the outlet for the solid particles at a distance from the inlet not exceeding 4D, between their vertical axes, where D. is the internal diameter of the inlet for the mixed flow.
    3. The separator according to claim 2, wherein the gas outlet is set relative to the inlet for the mixed flow at a distance (1.5-2.5) D; between their vertical axes.
    4. Separator on PP. 2 and 3, differing in that the height of the camera is 2D, -.
    5. A separator according to claim 4, characterized in that the width of the chamber is (0.9-1.1) 0.
    6. A separator according to claim 2, characterized in that the outlet for the solid particles is made of two parts: the first, collinear with the chamber and the second perpendicular to the first.
    7. A sealer according to claim 6, characterized in that it is provided with a means for restricting flow, located inside the collinear part of the outlet for solid particles.
    .eight. The separator according to claim 7, wherein the means for restricting flow is made in the form of an aperture.
    9. The separator of claim 7, wherein the means for restricting flow is performed in the form of a venturi.
    10. Separator according to claims 1 and 2, which are equipped with an overflow device located across the chamber under or at the bottom of the gas bed and in front of the outlet for solid particles.
    11. Separator on the PP. 1 and 2, characterized in that it is provided with means for giving a definite shape to the channel for the mixed flow, located after the chamber, wired with a circular cross section.
    12. Separator according to claim 11, wherein the means for shaping the mixed flow channel is defined
    in the form of a ceramic lining, located on the walls of the chamber.
    13. The separator according to claim 11, which is tactile in that the means for imparting a certain shape to the channel for the mixed flow are made in the form of a partition mounted
    in the chamber.
    14. Separator according to claim ,, 12, which is equipped with a lining made of an erosion-resistant material and located on the walls of the chamber.
    15. Separator, on PP. 1,2,5 and 6, characterized in that it is provided with a lining made of a thermally insulating material and located on the walls of the chamber.
    16. Separator according to claim 14, wherein it is provided with a heat insulating lining located between the walls of the chamber and an erosion-resistant lining.
    17. Separator on PP. 1,2,6 and 7, from. characterized in that the length of the portion of the chamber after the gas outlet is equal to or less than 5D-.
    18. Separator on PP. 1,2 and 8, which is equivalent to the fact that it is made with passages for the repair
    and cleaning works located on one 1-shek of both ends of the chamber.
    19. A system for separating solid particles, characterized in that it is equipped with a chamber for separating solid particles from gas, a secondary separator, separation of solid particles and gas, a pipeline connecting the gas outlet in the chamber to the secondary separator, a container for removing solid particles, a pipe connecting the container and the chamber and the means for adjusting the pressure.
    20. The separation system according to claim 19, wherein it is provided with a means of rapid cooling, located in the pipeline connecting the outlet for the gas in the chamber
    with secondary separator.
    21. A separation system according to claim 20, wherein the means for quenching is designed as a nozzle for the injection of a cooling fluid.
    22. The separation system according to claim 19, wherein the capacity for the removal of solid particles
    Executed in the form of a stripping tank.
    23. The separation system according to claim 19, wherein the secondary separator is implemented as a cyclone.
    24. A separation system according to claim 19, wherein the pressure control means is embodied in the form of a control valve installed at the outlet end of the pipeline connecting the container and the chamber.
    25. The separation system according to claim 1, wherein the pressure control means is embodied in the form of a pressure control valve mounted on the container for the removal of solid particles.
    The invention relates to devices and systems for separating solids from gas and may be used in the chemical, metallurgical and other industries. A separator is known which contains a curved pipeline, and the separation of solid particles and gas is carried out with a turn from 180 to. The centrifugal force directs heavier solids to the outer wall of the pipeline, while allowing gases to build up on the inner wall for later removal through the outlet. The disadvantage of the device is that it separates the gas from the solids by changing the direction of gas movement the place of its separation, and in this case solids continue to move linearly to the outlet of the separator. Since solids do not change direction of motion at the separation point, significant amounts of gas flow past the point of gas removal to the solids outlet. A separator for separating solid particles and gas containing a chamber for separating solid particles from gas is known. as well as the gas outlet and the solids outlet, while the inlet is normally located with respect to the flow direction, the solids outlet is located at the bottom of the chamber and the gas outlet is at an angle to the direction otok C2J. However, the well-known 5 system is characterized by insufficiently effective separation of particles from gas. The aim of the invention is the rapid separation of fine solid particles from a mixed stream with minimal erosion. This goal is achieved in that in the separator for separating solid particles and gas, there is a chamber for separating solid particles from gas, provided with an inlet for a mixed stream, an outlet for gas and an outlet for solid particles, the outlet for solid particles being located at the bottom of the chamber, and the gas outlet is at an angle of 180 ° to the flow direction, the chamber is made with rectangular or slightly curved longitudinal walls, and the outlet for solid particles is located on the opposite side of the chamber relative to the inlet for the mixed flow. The camera is complete with a height, at least DJ-, and width (0.751, 25) D. and the gas outlet is located between the inlet for the mixed flow and the outlet for the solid particles at a distance from the inlet, not exceeding, between their vertical axes, where D. is the inner diameter of the inlet for the mixed flow. The gas outlet is set relative to the inlet for the mixed flow at a distance (1.5-2.5) 0 between their vertical axes. The height of the camera is 2D, -. The width of the camera is (0.9-1.1) 0-. The solids outlet is made of two parts: the first, the collie is not varied with the camera, and the second, perpendicular to the first. The separator is equipped with flow restriction means located inside the collinear part of the outlet for solid particles. The flow restriction means is designed as a hole or as a venturi. The separator is provided with a variable device located across the chamber under or in the gas outlet and in front of the solid particle outlet. The separator is equipped with a means for shaping a certain-shaped channel for the mixed flow, located after the chamber, which has a circular cross-section. The means for imparting a certain shape to the channel for the mixed flow is made in the form of a ceramic lining located on the walls of the chamber, or in the form of a partition mounted in the chamber. The separator is equipped with a lining made of erosion-resistant or thermally insulating material located on the walls of the chamber. The separator is equipped with a thermal insulation dey lining located between the walls of the chamber and an erosion-resistant lining. The length of the portion of the chamber located after the gas outlet is equal to or less than L 5D. The separator is made with passages for repair and cleaning works located at one or both ends of the chamber. The system for separating solid particles is equipped with a chamber for separating solid particles from gas, a secondary separator for separating solid particles and gas, a pipeline connecting the gas outlet in the chamber to the secondary separator, a container for removing solid particles, a pipeline connecting the container and the chamber, and by pressure, pressure control. The system is equipped with a means of rapid cooling, a pipe located in the pipes connecting the gas outlet in the chamber with the secondary separator. The means for rapid cooling is designed as a nozzle for the injection of coolant. Eat: the bone for the removal of solid parts is made in the form of a stripping tank. The secondary separator is made in the form of a cyclone. The means for controlling the pressure is implemented in the form of a control valve installed at the outlet end of the pipeline connecting the container and the chamber, or in the form of a pressure control valve mounted on the container for the removal of solid particles. Fig, 1 shows a diagram of the separator, the section; FIG. 2 is a section A-A in FIG. Fig. 3 shows an embodiment of a chamber with rectangular walls; Fig. 4 is a diagram of a variant of a separator of a non-overflow device; Fig. 5 is a diagram of a variant of a separator with an overflow device and an elongated separating chamber of Fig. 6 is a diagram of a variant of a separator with stepped an outlet for solid particles that is filled in two parts: the first, collinear with the chamber, and the second, perpendicular to the first one in FIG. 7 is a diagram of the separation option: a torus with a stepless output; Fig. 8 is a diagram of a variant of a separator with flow restriction means in the form of a Venturi tube; Fig. 9 is a diagram of a variant of the separator of Fig. 8 for use in a lifting type reactor; in fig. 10 is a schematic of a solid particle separation system. The separator 1 is provided with a shell 2 and comprises a chamber 3 for separating solid particles from a gas, having an inlet 4 for introducing a mixed phase stream, an outlet 5 for the gas phase and an outlet 6 for the solid phase (particles). The outlet 4 and the outlet 6 of the solid phase are located at the opposite ends of the chamber 3, while the outlet 5 for the gas is located in the place between them. Passages 7 and 8 for repair and cleaning work can be provided at either end of chamber 3, Shell 2 of the separator and passages 7 and 8 for peMOHia are lined with erosion resistant liners 9-11, which may be necessary if solid particles come with large speeds, the lining 12, which provides thermal insulation, can be placed between the sheath 2 and the lining 9 and between the passages for repair and their corresponding erosion resistant linings in the event that the separator is to be used for operation at high temperatures tours. Thus, a process temperature in excess of 870 ° C is not an obstacle to the use of this device.
    For greater strength and to facilitate construction, the separator shell 2 is made of cylindrical sections, such as, for example, pipe 13. The longitudinal side walls 14 and 15 should be rectangular or slightly rounded. The shape of the flow channel is determined by adjusting the lining thickness for walls 14 and 15. Overflow devices, bulkheads, inserts, or other means can also be used. The casing 2 of the separator can be made in the form of a rectangular shaped pipe (FIG. 3). Since sheath 2 has rectangular walls 14 and 15, it is not necessary to adjust the width of the flow channel by varying the thickness of the lining. Liners 9 and 12 can be added to provide resistance to erosion and thermal exposure, respectively.
    The separator works as follows.
    The inlet stream containing the mixed phase enters input 4 and then turns 90 ° from inlet 4. The output of the gas phase 5 is located in such a way that the gas phase at the exit from the separator completes the change of its direction by 180 °.
    The centrifugal force pushes the solid particles in the direction of the wall 16 opposite the inlet 4 of the chamber 3, while a part of the gas with less momentum flows in the vapor space of chamber 3. The solid particles hit the wall 16 and accumulate to a static layer of solid particles 17, which takes the form of a surface corresponding to a curvilinear arc with an angle of approximately 90. The solid particles falling, and not on this layer, move along the curvilinear surface of the layer to exit 6 for a solid which is arranged in such a way that the particles go down under the force of gravity. The shape of the surface of layer 17 is determined by the geometry of the particular separator and the input flow parameters, such as speed, mass flow rate, bulk density, and particle size. Since the force applied to the incoming particles acts more on the static layer 17 than on the surface of the separator 1, the erosion will be minimal.
    The efficiency of the separator, determined by the degree of removal of solid particles from the gas phase exiting through the outlet 5, does not vary significantly at high input velocities (up to 45.7 m / s), and separator 1 can work in a wide density distribution diluted phases.
    The separator's efficiency also depends on its geometry, and the flow channel must be rectangular, and on the ratio between chamber height H and the sharpness of the U-shaped bend of the gas stream.
    For a given height of chamber H, the efficiency of the separator increases as the length of the flow channel and, consequently, the residence time of the mixture in the separator decreases. If the inner diameter of the inlet 4 has a value D, then the distance CL between the central axes of the inlet
    Drive 5 must be less than 4D. , in 4 and as the most optimal
    that time, the distance between said central axial lines is in the range of (1.5-2.5) 0, -. At a distance less than 1.5D, a better separation occurs, but difficulties will arise in the manufacture of such a device, which makes this option less attractive in many respects, since it is necessary to manufacture the separator as a one-piece cast structure due to the fact that that the inlet 4 and the outlet 5 are so close to each other that welding of the structure will be impossible.
    The height of the flow chamber H should be equal to or 5 cm, depending on which of the dimensions is larger. Practice shows that if H is less than or 5 cm, then the inlet push stream acquires a tendency to perturb the layer of solid particles, as a result of which solid particles re-enter the gas stream exiting through outlet 5. If H is twice as large as D. This results in even greater separation efficiency. A further increase in the value of H will simply lead to an increase in the residence time of the mixture in the chamber without actually increasing its efficiency. The width W of the current channel is (0.75-1.25) D, and the most optimal value is (0.9-1.1) D. Output 5 can have any internal diameter. However, at high temperatures, erosion can start due to solid particles trapped in the gas stream. In the separator, an overflow device 18 is located across the flow channel, located at a place located at the outlet of the gas or directly below it, in order to ensure the presence of a positive column of solid particles before exit 6 for solid particles. Installing the overflow device (or equivalent limitation) in this place creates a more stable layer, resulting in reduced turbulence and erosion. In addition, the overflow device 18 provides for the creation of a layer that has the shape of a crescent-shaped curvilinear arc encompassing the corner. A little over 90, an arc of this shape deflects the gas flow in the gas outlet direction and thereby creates an i-shaped trajectory of the gas flow. Without the overflow device 18, the arc 19 would cover an angle of less than or equal to 90 °, and would approach asymptomatically to exit 6 (FIG. 4). Although this is not going to be worse or effective. Neither gas losses, the presence of a stream whose shape corresponds to arc 19, leads to an increase in the residence time of particles in the chamber and, more importantly, creates a significant potential for erosion in sections 20-2. A variant of a separator having an outlet chamber in the longitudinal direction. Here, the horizontal distance L between the gas outlet 5 and the overflow 1m by the device 18 is increased in order to ensure the formation of the SAY, which has a large extent. L is chosen to be less than or equal to 5D. Although the shape of the flow contour does not reach the U-shaped view, a crescent-shaped arch is obtained, which limits the potential for erosion in section 22. The separator embodiments are used in cases where the concentration of solids in the input flow is low. The separator variant also has minimal pressure loss and can be used when the inflow rate is low. A variant of a separator having a stepped outlet for solid particles is possible, section 23 of which is collinear with the flow channel, and section 24 is located in such a way that the flow in it moves under the action of gravity. The step output exit replaces the overflow device 18. As the solid particles accumulate in the limited collinear part 23, the pressure loss is higher. This option is thus less optimal when the inlet stream has a low speed and cannot develop a force of sufficient magnitude to push the solids through the outlet. However, since the channel for the flow of solid particles is limited, better dielectric is provided and gas losses are minimal. A variant of the separator is possible in which the outlet for solid particles is made stepless (Fig. 7). Although no overflow device is used here, the output restricts the flow of solids, which helps the formation of a layer. Here, an increased distance between the gas outlet and the solid particle outlet can also be used. Possible version of the separator, made with a Venturi tube (Fig.8). The Venturi tube 25, having dimensions DI (diameter at the tube inlet), D y (diameter of the throat of the Venturi tube), 8 (the angle at the apex of the cone formed between the projections of the converging walls of the Venturi tube) is placed on the collinear section 23 of the exit for to provide greatly improved solid deaeration. A variant of a Venturi tube separator is possible for use in a lifting type reactor (Fig. 9). Here, the inlet 4 and the outlet are oriented in such a manner as to allow this device to be used with a lifting type reactor, solids are pressed against the upper wall and the layer thus formed is held in place by a suitable flow force, and the gas portion follows .U-shaped torii paths. However, in the absence of a constraint, an asymptotic layer will be formed at the outlet for the solid particles. The use of an overflow device for setting the height of the bed will be inefficient, and it will deflect solid particles towards the gas outlet. Installing the venturi 25 in the collinear section 23 is most effective in order to improve the deaeration of the solid particles. Example 1. The distance L from the gas outlet to the overflow device is zero. The inlet stream is made up of air entering at a speed of 2.407 and aluminosilicate. It is supplied at a speed of 23.58 kg / min, the bulk density of which was 112 t, 3 kg / m, and the average particle size reached 100 microns. The vapor density is 0.96 kg / m, and the operation is carried out at ambient temperature and at atmospheric pressure. The velocity of the flow entering through the inlet with a diameter of 5.06 cm was 20 m / s, while the velocity of the gas at the outlet was 26.1 m / s, and it came out through a hole with a diameter of 4.5 cm. The positive seal formed solid matter at the outlet of solid particles prevented the capture of gas into the stream of solids leaving the separator. The solids layer was stabilized by placing a flow-overflow device across the flow channel. The observed separation efficiency was 89.1%, and it was carried out with the gas-phase residence time in the device for approximately 0.008 s. Efficiency was defined as the percentage of solids removed from the inlet stream. Example 2. A mixture of gas and solid particles, used in example 1, was processed in a variant of the separator (figure 5). In this example, the size L is 5.06 cm, all other dimensions are the same as in Example 1. By increasing the size of the separation chamber in the longitudinal direction, the shape of the gas flow began to deviate from the U-shape. As a result, the residence time has become longer and an increase in turbulence has been noted. The separation efficiency was 70.8%. Example 3. A separator similar to that used in Example 2 was tested at an inlet stream consisting of air entering at a rate of 2.407 and aluminosilicate entering at a speed of 4.6 kg / min, which ensured a flow density of 19 kg / m ,those. approximately two times more than in example 2. The separation efficiency was greater and equal to 83.8%. Example 4. The separator variant used in example 1 was tested at the inlet flow rate indicated for example 3. A slight increase was noted efficiency up to 91.3%. Example 5. A separator (Fig. 1) was tested under the conditions of Example 1. The distance CL between the axial lines of the gas inlet and outlet was 15 cm, i.e. almost three times the input diameter. This size is outside the preferred range of CL values, which is (1.50-2.5) D, the dwelling Brem in the separator has increased to 0.01 s, the separation efficiency is 73: , 0%. Example 6. A separator was tested in which the size of the device was increased in comparison with the previous examples nine times with respect to the flow area. The treatment of air entering at a speed of 1.359, and aluminosilicate, flowing at a speed of 299.37 kg / min through an inlet opening with a diameter of 15.5 cm and exiting through an opening with a diameter of 10.12 cm, at 82.2 ° C and pressure 0.843 kg / cm . The corresponding speeds were 12.19 and 27.43 m / s, and the flux density was 22 kg / m. The distance CL between the inlet and outlet axes for the gas was 28 cm, or 1.83 times the input diameter. The distance L was zero. The layer was stabilized with an overflow device with a height of 5.85 cm, while gas losses were prevented by the presence of positive compaction of solids. Solids were collected in a closed vessel. The pressure difference was the result of a positive flow of gas from the collection vessel to the separator. This volume was approximately .0.26. The apparent separation efficiency was 90.0%, and the residence time of the gas phase in the device was approximately 0.02 s. Example 7 A separator used in Example 6 was tested with identical inlet flow of gas and solid particles. However, a tank for collecting solids was in communication with the atmosphere, and the pressure difference was controlled so that 9% of the feed gas (or 1.18) exited through the opening for separating solids at a speed of 1.09 m / s. The efficiency of the separator in the presence of this positive leakage through an outlet for solid particles has increased, up to 98.1%. EXAMPLE 8 A separator variant (Fig. 7) was tested as a unit having an entrance diameter of 5.06 cm and an outlet for a gas with a diameter of 2.54 cm. The outlet for solid particles had a diameter of 5.06 cm and was located 25.4 cm away from the gas outlet. Overflow device not applied. The inlet stream consisted of air and spent catalyst used in the process of a greedy catalytic cracking feed at a rate of 52.6 kg / m, having a bulk density of 720.83 kg / m3 and an average particle size of 50 microns. This provided a flux density of 19.22 kg / m. The inlet gas velocity was 19.4 m / s, while the outlet gas velocity was 79.3 m / s. As in Example 7, a positive counterflow of the displaced gas from the collecting tank to the separator was provided. 912 This flow was moving at a speed of 0.396 m / s. The work was carried out at the terapet of the surrounding pilot and at atmospheric pressure. The separation efficiency was 95.0%. The separation system consists of the primary separator 1, the secondary separator 26 and the stripping tank 27. The outlet for the gas of the primary separator 1 is connected to the secondary separator 26 by means of a pipe (line) 28, while the stripper 27 is likewise connected to the outlet particulate matter. A pressure control means is used to regulate the gas flow entering the stripping tank. The system works as follows. The solids and gas enter the tube reactor 29 through lines 30 and 31, respectively. The streams extending from the reactor are sent directly to separator 1, where the separation is made into streams containing the gas phase and the phase of solids. The gas phase is removed via line 28 while the solid phase is sent to tank 27 for stripping through line 32. Depending on the type of process and. the degree of separation, the rapid cooling of the gas. Inside the line 28 can be carried out by injecting the material from line 33 to cool. Usually, the resulting product gas contains residual solids and is sent to the secondary separator 26, which is a conventional cyclone. The cooling material must be introduced in line 28 in such a way that: to prevent the possibility of the back flow of this material into the separator. Residual solids are removed from E-26 through line 34 at that time, as virtually no gas solids are contained; as a product, is removed from the top through line 35. Solids from lines 32 and 34 are freed from gas pollution in the tank 27. The steam from the steam containing the fluidized bed uses steam or other neutralizing fluid gas flowing through lines 36. Pairs of. The stripping vessels are removed along line 37 and. if necessary or for economic reasons, they are sent to purification units located downstream of the flow. Stripped solids discharged from tank 27 through line 38 are sent to regenerator 39, and this uses pressurized transport gas from line 40. Exhaust gases from regenerator 39 are removed through line 41. After regeneration, the solids are recycled to the reactor 29 through line 30. Separator 1 must ensure that, for a short time, solids are separated from the stream leaving the reactor, in order to prevent degradation of the product and to ensure optimal yield and selectivity of the required products. who in. Separator 1 operates in taco mode, which eliminates or at least substantially reduces the amount of gas entering the tank 27 for stripping, since this part of the gaseous product will significantly improve its properties if it stays in close contact with solid phase. This is accomplished by applying a positive seal that is provided between the separator 1 and the tank 27 for stripping. Separator 1 operates so that erosion is minimized despite the high temperatures and high speeds that are inherent to these. The inner diameter of the outlet 6 of the separator should be chosen 914 so that the pressure difference between the tank .27 for stripping and the separator 1 is of such a size that a static column of solid forms in the line 32 coming from the outlet for solid particles. This static column of solids in line 32 forms a positive seal that prevents the gases from entering the stripping tank 27. The magnitude of the pressure difference between the stripping tank 27 and the separator t is determined by the magnitude of the force required to move the solid particles as a volume flow to exit 6 for solids and a column of solid particles in line 32. As the pressure difference increases, the total flow the gas in the stripping tank 27 is reduced. Solid particles with a gravitational moment overcome this pressure difference while the gas exits through outlet 5 for gas. By adjusting the pressure in the stripping tank 27, the amount of gas entering the installation can be controlled. The means for regulating the pressure may include a check or flap valve 42 installed at the outlet of line 32, or a device 43 for controlling pressures on the tank 27. The pressure can also be adjusted by selecting the size of the outlet 6 and line 32 so as to obtain the hydraulic force acting on the system to create a gas stream in the direction of the steamers.
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    权利要求:
    Claims (25)
    [1]
    1. A separator for separating solid particles and gas, comprising a chamber for separating solid particles from gas, made with an inlet for a mixed flow, an outlet for gas and an outlet for solid particles, the outlet for solid particles being located at the bottom of the chamber, and the outlet for gas under angle of 180 ° to the flow direction, characterized in that, in order to quickly separate small solid particles from the mixed stream with minimal erosion, the chamber is made with rectangular or slightly curved longitudinal walls, and the exit for solid particles is located "g in p otivopolozhnoy of the camera with respect to the mixed input stream.
    6bSh0G ' go ns
    [2]
    2. The separator pop.1, characterized in that the chamber is made with a height of at least D ^, h width (0.75-1.25) Dj, and the gas outlet is located between the inlet for the mixed stream and the outlet for solid particles at a distance from the inlet not exceeding 4D ^ between their vertical axes, where is the internal diameter of the inlet for the mixed flow.
    [3]
    3. The separator according to claim 2, wherein the gas outlet is set relative to the inlet for the mixed flow at a distance of (1.5-2.5) D; between their vertical axes.
    [4]
    4. The separator according to paragraphs. 2 and 3, characterized in that the height of the camera is equal to 2D, ·.
    [5]
    5. The separator according to claim 4, characterized in that the width of the chamber is equal to (0.9-1.1) Dj.
    [6]
    6. The separator according to claim 2, characterized in that the output for solid particles is made of two parts: the first, collinear with the camera, and the second perpendicular to the first.
    [7]
    7. The searator according to claim 6, characterized in that it is provided with a flow restriction means located inside the collinear part of the outlet for solid particles.
    .
    [8]
    8. The separator according to claim 7, wherein the flow restriction means is made in the form of an opening.
    [9]
    9. The separator according to claim 7, characterized in that the flow restriction means is in the form of a venturi.
    [10]
    10. The separator according to claims 1 and 2, characterized in that it is equipped with an overflow device located across the chamber under or in the outlet: an ode for gas and in front of the outlet for solid particles.
    [11]
    11. The separator according to paragraphs. 1 and 2, characterized in that it is provided with means for giving a certain shape to the channel for mixed. flow, located after the camera, made with a circular cross section.
    [12]
    12. The separator according to claim 11, wherein the means for shaping the mixed flow channel is made in the form of a ceramic lining located on the walls of the chamber.
    [13]
    13. The separator according to claim 11, wherein the means for shaping the mixed flow channel is in the form of a partition installed in the chamber.
    [14]
    14. The separator according to claim 12, characterized in that it is provided with a lining made of erosion-resistant material and located on the walls of the chamber.
    [15]
    15. Separator. 1,2,5 and 6, characterized in that it is equipped with a lining made of heat-insulating material and located on the walls of the chamber.
    [16]
    16. The separator according to claim 14, characterized in that it is provided with a thermally insulating lining located between the walls of the chamber and an erosion-resistant lining.
    [17]
    17. The separator according to paragraphs. 1,2,6 and 7, characterized in that the length of the part of the chamber located after the exit for gas is equal to or less than 5D ·.
    [18]
    18. The separator according to paragraphs. 1,2 and 8, characterized in that it is made with passages for repair and cleaning works located at one or both ends of the chamber.
    [19]
    19. A system for separating solid particles, characterized in that it is equipped with a chamber for separating solid particles from gas, a secondary separator for separating solid particles and gas, a pipe connecting the gas outlet in the chamber with a secondary separator, a container for discharging solid particles, the pipeline connecting the tank and the chamber, and means for regulating the pressure.
    [20]
    20. The separation system according to claim 19, characterized in that it is provided with means of quenching located in the pipeline connecting the gas outlet in the chamber to the secondary separator.
    [21]
    21. The separation system according to claim 20, characterized in that the means for quenching is made in the form of a nozzle for injecting coolant.
    [22]
    22. The branch system in g :. 19, characterized in that the tank for outputting solid particles is made in the form of tanks for steaming.
    [23]
    23. The separation system according to claim 19, characterized in that the secondary separator is made in the form of a cyclone.
    [24]
    24. The separation system according to claim 19, characterized in that the means for regulating the pressure is made in the form of a control valve installed at the output end of the pipeline connecting the tank and the chamber.
    [25]
    25. The separation system according to claim 19, characterized in that the means for regulating the pressure is made in the form of a pressure regulating valve mounted on a container for outputting solid particles.
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    KR20010072426A|2001-07-31|Method and assembly for separating solids from gaseous phase
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    JP4178496B2|2008-11-12|Separation and stripping equipment and its use for fluidized bed catalytic cracking
    US2402845A|1946-06-25|Multiple stage cyclonic separator
    US6146597A|2000-11-14|Separation device
    EP1583847B1|2008-10-08|Method and plant for the heat treatment of sulfidic ores using annular fluidized bed
    US4278550A|1981-07-14|Fluid separator
    US4756886A|1988-07-12|Rough cut solids separator
    US20060177357A1|2006-08-10|Riser termination device
    US4279624A|1981-07-21|Downflow separator method and apparatus
    JP4247503B2|2009-04-02|Direct rotary separator of gas mixed particles and its use in fluidized bed thermal cracking or catalytic cracking
    US4552645A|1985-11-12|Process for cracking heavy hydrocarbon to produce olefins and liquid hydrocarbon fuels
    US5518695A|1996-05-21|Vented riser with compact multiple cyclone arrangement
    US5976355A|1999-11-02|Low residence time catalytic cracking process
    US4556541A|1985-12-03|Low residence time solid-gas separation device and system
    US4871147A|1989-10-03|Apparatus for the pyrometallurgical processing of fine-grained solids
    CA1171800A|1984-07-31|Low residence time solid-gas separation device andsystem
    US5328592A|1994-07-12|FCC reactor with tube sheet separation
    US4544480A|1985-10-01|Low residence time solid-gas separation process
    KR830001384B1|1983-07-21|Solid-gas separator with short residence time
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    同族专利:
    公开号 | 公开日
    EP0023769A1|1981-02-11|
    IN154591B|1984-11-17|
    MX150892A|1984-08-09|
    ES495691A0|1981-10-01|
    ES8105578A1|1981-06-16|
    ZA804043B|1981-06-24|
    IL60521D0|1980-09-16|
    IL60521A|1984-03-30|
    ES8107039A1|1981-10-01|
    FI76498B|1988-07-29|
    ES495692A0|1981-10-01|
    WO1981000059A1|1981-01-22|
    SG22885G|1985-09-13|
    YU42345B|1988-08-31|
    YU174480A|1983-10-31|
    MX161010A|1990-06-29|
    US4288235A|1981-09-08|
    PT71489A|1980-08-01|
    ES493120A0|1981-06-16|
    CA1151084A|1983-08-02|
    FI802137A|1981-01-07|
    BR8008739A|1981-04-28|
    AR224014A1|1981-10-15|
    MY8600098A|1986-12-31|
    FI76498C|1988-11-10|
    AT10588T|1984-12-15|
    MA18899A1|1981-04-01|
    JPS6018447B2|1985-05-10|
    EP0023769B1|1984-12-05|
    ES8107040A1|1981-10-01|
    JPS56500878A|1981-07-02|
    DE3069746D1|1985-01-17|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2514960C2|2008-07-31|2014-05-10|Тиссенкрупп Уде Гмбх|Device and method for dust degassing|US1469702A|1923-10-02|Air-cleaning attachment eor automobile carburetors |
    DE532653C|1927-11-18|1931-09-02|Carl Foerderreuther Dr Ing|Dust collector|
    US2328325A|1940-06-29|1943-08-31|Standard Oil Co|Powdered catalyst recovery|
    US2439811A|1941-05-21|1948-04-20|Kellogg M W Co|Catalytic conversion of hydrocarbons|
    US2641335A|1946-01-12|1953-06-09|Union Oil Co|Gas-solid separator|
    CH284789A|1949-05-28|1952-08-15|Waagner Biro Ag|Gas cleaning process with the aid of a primary dust separator and dust separator for carrying out the process.|
    US2698224A|1951-12-18|1954-12-28|Phillips Petroleum Co|Catalyst backflow prevention device|
    FR1088435A|1952-12-04|1955-03-07|Standard Oil Dev Co|Separation of entrained particles in fluids|
    US2737479A|1953-07-27|1956-03-06|Exxon Research Engineering Co|Staged separation and stabilization of oil conversion products and apparatus therefor|
    US2878891A|1953-10-05|1959-03-24|Exxon Research Engineering Co|Loop separator for gases and solids|
    US2947577A|1957-01-15|1960-08-02|Shell Oil Co|Disengaging solids from a lift gas|
    DE1170320B|1957-08-19|1964-05-14|Buehler Ag Geb|Flat separator for pneumatic conveyor systems|
    US3056248A|1959-07-22|1962-10-02|Metallgesellschaft Ag|Separating apparatus|
    US3247651A|1962-11-27|1966-04-26|Exxon Research Engineering Co|Inertia-type solids de-entrainment device|
    AT238115B|1962-11-28|1965-01-25|Wibau Gmbh|Device for the production of a grain-compatible filler as a proportion of the solid components in the preparation of bituminous mixed material, in particular for purposes of road construction|
    US3443368A|1966-07-26|1969-05-13|Shell Oil Co|Tubular centrifugal separators|
    DE2221726A1|1972-05-04|1973-11-15|Karl Dipl-Ing Beckenbach|Dust sepn from gas - esp coarse particles from lime kiln flue gas|
    US4219407A|1978-01-20|1980-08-26|Mobil Oil Corporation|Fluid cracking process and the method for separating a suspension discharged from a riser cracking zone|
    US4163650A|1978-07-24|1979-08-07|Tepco, Incorporated|Portable electronic precipitator|US4433984A|1979-07-06|1984-02-28|Stone & Webster Engineering Corp.|Low residence time solid-gas separation device and system|
    US4348364A|1979-07-06|1982-09-07|Stone & Webster Engineering Corp.|Thermal regenerative cracking apparatus and separation system therefor|
    US4556541A|1980-07-03|1985-12-03|Stone & Webster Engineering Corporation|Low residence time solid-gas separation device and system|
    US5045176A|1981-05-13|1991-09-03|Ashland Oil, Inc.|Carbometallic oil conversion with ballistic separation|
    SE437943B|1983-08-16|1985-03-25|Stal Laval Turbin Ab|SET TO OK A CYCLE'S SEPARATION DEGREE AND CYCLE DISPENSER FOR IMPLEMENTATION OF THE SET|
    JPS6189645U|1984-11-16|1986-06-11|
    US4756886A|1986-04-10|1988-07-12|Stone & Webster Engineering Corporation|Rough cut solids separator|
    US5098672A|1987-08-11|1992-03-24|Stone & Webster Engineering Corp.|Particulate solids cracking apparatus and process|
    US4814067A|1987-08-11|1989-03-21|Stone & Webster Engineering Corporation|Particulate solids cracking apparatus and process|
    US5167795A|1988-01-28|1992-12-01|Stone & Webster Engineering Corp.|Process for the production of olefins and aromatics|
    EP0381870B1|1989-02-08|1993-05-12|Stone & Webster Engineering Corporation|Process for the production of olefins|
    US5391289A|1990-09-04|1995-02-21|Chevron Research And Technology Company|FCC process with rapid separation of products|
    US5259855A|1991-09-09|1993-11-09|Stone & Webster Engineering Corp.|Apparatus for separating fluidized cracking catalysts from hydrocarbon vapor|
    ES2073240T3|1991-09-09|1995-08-01|Stone & Webster Eng Corp|PROCEDURE AND APPARATUS FOR SEPARATING FLUIDIZED CRACHY CATALYSTS FROM VAPORIZED HYDROCARBONS.|
    US5314610A|1992-05-29|1994-05-24|Abb Lummus Crest Inc.|Staged catalytic cracking process|
    AT399824B|1993-11-17|1995-07-25|Scheuch Alois Gmbh|METHOD AND DEVICE FOR DUST SEPARATION|
    US5389239A|1993-11-22|1995-02-14|Texaco Inc.|Control method for direct-coupled FCC riser cyclone|
    AU729703B2|1996-06-10|2001-02-08|Supergold Holdings Pty Ltd|Top stuffing box|
    FI114289B|2000-04-07|2004-09-30|Foster Wheeler Energia Oy|Device for separating particles from hot gases|
    US6692552B2|2001-03-20|2004-02-17|Stone & Webster Process Technology, Inc.|Riser termination device|
    US7591939B2|2004-06-22|2009-09-22|Stone & Webster Process Technology, Inc.|Integrated desulfurization and FCC process|
    US7429363B2|2005-02-08|2008-09-30|Stone & Webster Process Technology, Inc.|Riser termination device|
    WO2009019070A1|2007-08-07|2009-02-12|Polysius Ag|Device and method for performing chemical and/or physical reactions between a solid material and a gas and plant for producing cement|
    AT505750B1|2007-12-21|2009-04-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR THE SOLUBLE DEPOSITION OF SOLID PARTICLES FROM SOLID-LOADED GASES|
    US8383051B2|2009-07-22|2013-02-26|Stone & Webster Process Technology, Inc.|Separating and stripping apparatus for external FCC risers|
    US8177887B2|2010-02-27|2012-05-15|Hewlett-Packard Development Company, L.P.|Aerosol particle collection|
    CN103939072B|2014-05-07|2018-08-14|邓晓亮|Liquid oxygen strong stimulation igniting air drives Pintsch process mixed phase gas recombination technology of reservoir sweep|
    CN107288599A|2016-03-30|2017-10-24|中国石油化工股份有限公司|Administer the stifled tune method of steam stimulation wells|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/055,148|US4288235A|1979-07-06|1979-07-06|Low residence time solid-gas separation device and system|
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