JP5519982B2 - Two-phase fluid separation apparatus and method - Google Patents

Description

  The present invention relates to a two-phase fluid separation device, and more particularly to a two-phase fluid separation device and method that can freely separate a particle component having a desired particle size from a two-phase fluid.

  Conventionally, many devices for separating each phase of a two-phase fluid (gas-liquid, solid-liquid, solid-gas) permeate the two-phase fluid through the filter membrane, and only the liquid phase or solid phase in the fluid is filtered. Although it was trapped by a membrane, in such a filter membrane method, it is inevitable that the separation efficiency will deteriorate over time due to clogging of the filter, and the maintenance cost associated with cleaning and replacement of the filter There was a problem that would become excessive.

  In this regard, Japanese Patent Laying-Open No. 2005-28242 (Patent Document 1) discloses a filter device that separates solid and liquid using the action of centrifugal force based on the difference in specific gravity (density) in a two-phase fluid. To do. However, this method has a problem that it cannot be applied to the separation of a two-phase fluid that does not have a large difference in specific gravity of each phase.

JP 2005-28242 A

  The present invention has been made in view of the above problems in the prior art, and the present invention freely separates the particle components having a desired particle diameter regardless of the magnitude of the specific gravity difference between the phases of the two-phase fluid. It is an object of the present invention to provide a novel two-phase fluid separation device and method that can be used.

  As a result of intensive investigations on a novel two-phase fluid separation apparatus and method capable of freely separating particle components having a desired particle diameter regardless of the magnitude of the specific gravity difference of each phase of the two-phase fluid, the present inventor When a relative speed is generated between the slit-shaped opening communicating with the fluid discharge side and the two-phase fluid to be separated, in the direction opposite to the long side of the opening, the relative speed is The inventors have found a phenomenon in which particle components having a correlated particle size are separated, and have reached the present invention. Hereinafter, the principle of the two-phase fluid separation method of the present invention will be described with reference to FIG.

FIG. 1 shows a two-dimensional channel composed of a main channel M and a branch channel D. In the two-dimensional channel shown in FIG. 1, a two-phase fluid containing a particle component having a particle diameter d flows down the main channel M from the left to the right, and has a slit-like shape having a width h with respect to the main channel M. A branch channel D is formed, and the longitudinal direction of the slit opening is orthogonal to the flow direction of the two-phase fluid. In this two-dimensional channel, the flow rate of the two-phase fluid flowing through the main channel M is U, the volume concentration of the particle component is α ₀ , the flow rate of the two-phase fluid flowing through the branch channel D is u, and the volume concentration of the particle component is Is α.

  In the two-dimensional flow path shown in FIG. 1, the two-phase fluid layer that flows through the place where the separation distance from the wall surface of the main flow path M is within a certain distance flows into the branch flow path D, and flows over the place beyond it. This layer passes through the branch channel D without flowing into it. Here, let H be the separation distance from the wall surface of the main flow path M upstream of the limit flow line flowing into the branch flow path D.

  Further, among the particle components contained in the two-phase fluid flowing in the layer within the limit streamline, the particles flowing in a place where the distance from the wall surface of the main flow path M is within a certain distance follow the fluid to branch the flow path D. Particles that flow into the flow path and beyond the flow path pass through the branch flow path D without being able to follow the fluid flowing into the branch flow path D. Here, the separation distance from the wall surface of the main channel M upstream of the limit particle trajectory flowing into the branch channel D is Y.

Here, since the two-phase fluid layer that flows in a place where the separation distance from the wall surface of the main flow path M is smaller than d / 2 (corresponding to the particle radius) can be assumed that particles are not included, Of the two-phase fluid flowing into the path D, the fluid containing the particle component is limited to the fluid flowing in the place where the separation distance y from the wall surface of the main channel M upstream satisfies d / 2 ≦ y ≦ Y. Therefore, the particle volume flowing into the branch channel D per unit time is
{α ₀ (Yd / 2) U}
If the flow rate of the branch channel D is q = UH = uh, the volume concentration α of the particles flowing out from the branch channel D can be expressed by the following theoretical formula. Here, q is a flow rate per unit width of depth, and has a unit of m ² / S.

Here, in the above theoretical formula (1), when arranged as {d / H = dU / q = dU / (hu) = ζ}, the volume concentration α of the two-phase fluid flowing down the branch channel D and the main channel The following formula (2) is derived as a theoretical formula representing the ratio (α / α ₀ ) of the volume concentration α ₀ of the two-phase fluid flowing through M.

Here, from the above theoretical formula (1), when the value of {Y / d} is 0.5 or less, the volume concentration ratio (α / α ₀ ) becomes zero. When particles follow the flow, Y = H, and when the value of {H / d = 1 / ζ} is 0.5 or less, that is, when the value of ζ is 2 or more, the volume concentration ratio (α / α ₀ ) is 0. become. That is, according to the above theoretical formulas (1) and (2), when these conditions are satisfied, the volume concentration α of the branch channel D is set to 0, that is, the particle component having a particle diameter d or larger is not included. It is expected that only the fluid can be delivered to the branch channel D side.

  It should be noted that both {Y / d} and {Y / H} in the above theoretical formulas (1) and (2) are specific gravity = particle density / fluid density of the system to be separated, Reynolds number = fluid density × particle diameter × flow velocity / fluid Viscosity changes according to the value of ζ (= dU / q). As these values increase, {Y / d} and {Y / H} have a property of taking smaller values. In determining the values of {Y / d} and {Y / H}, the drag applied to the particles by the relative velocity of the particles and the fluid, the additional mass applied to the particles moving in acceleration in the fluid, and the flow field in which no particles exist It can be obtained by a simulation calculation using the equation of motion of the particle, taking into account the force received by the particle due to the pressure distribution.

  For example, in a two-phase fluid in a two-dimensional channel, the Reynolds number is small even if the ratio of the particle density to the fluid density does not greatly exceed 1, or the particle density is much larger than the fluid density. In this case, since all the particle components in the two-phase fluid flow into the branch channel D following the fluid, Y = H, that is, {Y / H = 1}, and the following theoretical formula (2) Therefore, if a flow rate satisfying {U ≧ 2q / d} is given under the condition satisfying {ζ ≧ 2}, only a fluid not containing a particle component larger than the diameter d can be sent to the branch channel D side. become.

On the other hand, in the case of a two-phase fluid in which the ratio of the density of the particles to the density of the fluid greatly exceeds 1 and the Reynolds number greatly exceeds 1 like a gas containing droplets, as shown in FIG. The relationship between {Y / d} and U is obtained using the simulation result. FIG. 2 shows the result of simulation for the case where the air flow rate q per unit width is 0.125 m ² / s in air (gas-liquid fluid) containing water droplets having a diameter of 30 μm. When the simulation result shown in FIG. 2 is obtained, the value of U (flow velocity of the two-phase fluid flowing through the main channel M) is set to a value at which the value of {Y / d} is 0.5 (in the case of FIG. 2, U = If it is set to be larger than 42 m / s), only a fluid that does not contain a particle component larger than the diameter d can be delivered to the branch channel D side.

The present inventor conducted a preliminary experiment using a two-dimensional channel model conceptually shown in FIG. 3A in order to verify the validity of the theoretical formula (2). In this preliminary experiment, polystyrene particles were used as the solid phase and saline adjusted to the same specific gravity as that of the polystyrene was used as the fluid, and the predetermined conditions for the main channel M (aspect ratio: H / B = 1.66 · 0.6) were used. Under (U, u, h, d), the polystyrene particle volume concentration α of the two-phase fluid flowing down the branch channel D and the polystyrene particle volume concentration α ₀ of the two-phase fluid flowing through the main channel M are measured, and ζ ( = DU / q) and the volume concentration ratio (α / α ₀ ) were calculated. In this experiment, the above condition (particle density / fluid density = 1, that is, Y / H = 1) is substituted into the theoretical formula (2), and α / α ₀ = 0 when ζ = 2. Although a theoretical straight line (solid line) was set, the experimental results agreed well with the theoretical straight line (solid line) as shown in FIG.

  The present inventor has repeatedly studied a novel two-phase fluid separation method based on the above-described demonstration results. As a result, {U} in ζ (= dU / q) of the above theoretical formula (2) is defined as the relative velocity between the slit opening of the branch flow path D and the two-phase fluid stored in the main flow path M. As a result of conceiving the configuration to be imparted and conducting a demonstration experiment based on the configuration, the present inventors have succeeded in separating the particle components from the two-phase fluid as desired, leading to the present invention.

  As described above, according to the present invention, a novel two-phase fluid separation device that can freely separate particle components having a desired particle diameter regardless of the specific gravity difference between the phases of the two-phase fluid, and A method is provided.

The conceptual diagram which shows the two-dimensional flow path for demonstrating this invention. The figure which shows the simulation result about a gas-liquid fluid. The figure which shows the result of the preliminary experiment of a two-dimensional channel model. The figure which shows the two-phase fluid separation apparatus of 1st Embodiment of the 1st form of this invention. The figure which shows the form of the rotation container applicable to 1st Embodiment of 1st type of this invention. The figure which shows the form of the rotation container applicable to 1st Embodiment of 1st type of this invention. The figure which shows the two-phase fluid separation apparatus of 2nd Embodiment of the 1st form of this invention. The figure which shows the two-phase fluid separation apparatus of 3rd Embodiment of the 1st form of this invention. The figure which shows the two-phase fluid separation apparatus of embodiment of the 2nd form of this invention. The figure which shows the two-phase fluid separation apparatus which comprised the storage container as an open container or a pipe | tube. FIG. 3 is a diagram showing a solid-liquid separator model of Example 1. The figure which shows the relationship between the mass flow rate (g / s) of discharge liquid, and the rotation speed (rpm) of a rotation container. The figure which shows the relationship between the mass (g / s) of the polystyrene particle contained in the discharge | emission liquid discharged | emitted per unit time, and the rotation speed (rpm) of a rotation container. The figure which shows the relationship of the mass percent concentration (%) of the polystyrene particle | grains contained in discharge | emission liquid, and the rotation speed (rpm) of a rotation container. The figure which shows the relationship between volume concentration ratio ((alpha) / (alpha) ₀ ) and (zeta) (= dU / q) about the solid-liquid separator model of Example 1. FIG. The figure which shows the gas-liquid separator model of Example 2. FIG. The figure which shows the relationship between the volume flow volume (L / s) of exhaust, and the rotation speed (rpm) of a rotating plate. The figure which shows the relationship between the mass (mg / s) of the water droplet contained in the exhaust_gas | exhaustion discharged | emitted per unit time, and the rotation speed (rpm) of a rotating plate. The figure which shows the relationship between the volume concentration (g / m < ³ >) of the water droplet contained in exhaust_gas | exhaustion, and the rotation speed (rpm) of a rotating plate. The figure which shows the relationship between volume concentration ratio ((alpha) / (alpha) ₀ ) and (zeta) (= dU / q) about the gas-liquid separator model of Example 2. FIG. The figure which shows the solid-liquid separator model of the present Example 3. The figure which shows the relationship of the mass percent concentration (%) of the polystyrene particle contained in discharge | emission liquid, and the rotation speed (rpm) of a stirring blade. The figure which shows volume concentration ratio ((alpha) / (alpha) ₀ ) and (zeta) (= dU / q) about the solid-liquid separator model of Example 3. FIG.

  Hereinafter, the present invention will be described with reference to embodiments shown in the drawings, but the present invention is not limited to the embodiments shown in the drawings. In the drawings referred to below, the same reference numerals are used for common elements, and the description thereof is omitted as appropriate.

  The implementation of the two-phase fluid separation device of the present invention can be roughly divided into two types depending on the configuration that generates the relative velocity between the opening communicating with the fluid discharge side and the two-phase fluid to be separated. . That is, the first type in which a relative speed is generated between the stationary two-phase fluid and the two-phase fluid by circulatingly moving on the opening side with respect to the stationary two-phase fluid; This is a second type in which a relative speed is generated between the opening by circulating movement. Hereinafter, the first format described above will be described first.

  FIG. 4 shows a two-phase fluid separation device 10 according to the first embodiment of the first type. As shown in FIG. 4A, the two-phase fluid separation device 10 includes a sealed container 11 for introducing a two-phase fluid to be separated and a rotating container 12. The rotating container 12 is connected to a rotation driving means 13 such as a motor, and is configured to be able to control rotation at a desired speed in the direction of the arrow.

  FIG. 4B shows only the rotating container 12 extracted. The rotating container 12 includes a container 14 formed in a hollow disk shape (that is, a hollow columnar shape having a short height) and an elongated cylindrical portion 15. The cylindrical portion 15 is connected to the center of one bottom surface of the container 14 so that the internal space of the cylindrical portion 15 and the internal space of the container 14 communicate with each other, and the rotating container 12 is a hollow container having a rotationally symmetrical shape. It is configured as.

  Two openings 16, 16 are formed on one bottom surface of the bottom surface of the container 14 of the rotating container 12, and the internal space of the sealed container 11 passes through the openings 16, 16. It communicates with the inside. The opening 16 is formed as an elongated rectangular slit having a width h, and is opposed to the bottom surface of the container 14 so that the long side of the opening 16 is substantially perpendicular to the rotation direction of the rotating container 12 indicated by the arrow R. Is formed. The rotating container 12 is rotatably disposed inside the sealed container 11, and the cylindrical portion 15 protrudes to the outside so as to penetrate the wall surface of the sealed container 11 and is connected to a discharge channel (not shown).

Processing for separating the two-phase fluid using the two-phase fluid separation device 10 having the above-described configuration will be described below. First, a two-phase fluid is introduced from the introduction channel 17 into the sealed container 11. Here, for convenience of explanation, it is assumed that the two-phase fluid has two kinds of particles L and S dispersed in a liquid phase or gas phase fluid, and the particle diameter of the particles L is d. The particle size of the particles S is smaller than d. In the case of the example shown in FIG. 4, since the inside of the sealed container 11 is completely filled with the two-phase fluid, the flow rate of the two-phase fluid introduced into the sealed container 11 from the introduction flow path 17 and the rotation container 12 The flow rate Q ₀ of the two-phase fluid discharged from the cylindrical portion 15 becomes equal, and when Q ₀ is divided by the area of the opening 16, a predetermined flow rate {u corresponding to the processing flow rate set in the two-phase fluid separation device 10 is obtained. } And the flow rate per unit width q = uh.

  Here, if the rotation of the rotating container 12 is stopped, the particles L and the particles S in the two-phase fluid introduced from the introduction flow path 17 are both in the rotating container 12 from the openings 16 and 16. Although it flows in and flows out to the outside through the cylindrical portion 15, in the two-phase fluid separation device 10 of the present embodiment, the rotation container 12 is rotated by the rotation driving means 13, and the rotation speed is controlled. A fluid that does not contain the particles L having the particle diameter d (that is, a fluid that contains only the particles S) can be delivered to the outside.

  The rotational speed (rpm) of the rotating container 12 in the present embodiment can be obtained by the following procedure. First, in the case of a two-phase fluid in which particles follow the fluid, a relative velocity U (in the short side direction of the opening 16) satisfying {U ≧ 2q / d} as a critical particle diameter d and a flow rate q per unit width. The required flow velocity of the two-phase fluid flow R) is calculated. On the other hand, when the particle is a two-phase fluid that does not follow the fluid, a relative velocity U that satisfies the above-described {Y / d ≦ 0.5} is calculated. Based on these calculated relative speeds U, a rotational speed (rpm) necessary to realize this is obtained. By controlling the operation of the two-phase fluid separation device 10 with the rotation speed, the particles L and the particles S in the two-phase fluid can be separated.

  In addition, the rotation container in this embodiment is not limited to the form shown in FIG. FIG. 5 illustrates another form of the rotating container applicable to this embodiment. A rotating container 20 shown in FIG. 5A includes a container 21 formed in a rectangular parallelepiped shape and an elongated cylindrical part 22, and a T-shaped hollow formed by connecting the cylindrical part 22 to the center of the upper surface of the container 21. The container 21 is configured, and two openings 23 a and 23 b are formed on the bottom surface of the container 21.

  Further, in the rotating container 20, in order to make the boundary layer of the fluid in contact with the openings 23a and 23b thinner, for example, as shown by being surrounded by a broken line in the drawing, a hollow container 21 is used instead of the rectangular parallelepiped container 21. A container 24 formed in a shape can be used. By forming the opening 25 in the face portion of the bowl-shaped container 24, the relative speed of the opening and the fluid simply rotates, just as the speed on the airplane wing is greater than the flight speed. A relative speed larger than the relative speed obtained by the above can be obtained, and since the speed increasing region is from the tip to the opening 25, the thickness of the boundary layer can be kept small.

  Furthermore, as shown by a broken line in the lower left of the figure, a flat plate 26 is provided so as to protrude from the bottom surface of the container 21, and an opening 23 is provided there, so that the turbulence is parallel to the flat plate 26 around the opening 23. A small flow is formed, and as a result, the thickness of the boundary layer near the opening 23 can be kept small. Furthermore, as shown in the cross-sectional view of the container 21 surrounded by a broken line at the lower right of the figure, the opening 23 is formed as a through hole inclined with respect to the thickness direction of the container 21, so that the main flow direction of the fluid is increased. This creates a U-turning flow, resulting in an increased filtering effect in a two-phase fluid where the particles do not follow the fluid.

  FIG. 6 illustrates another form of the rotating container applicable to this embodiment. A rotating container 30 shown in FIG. 6 includes a container 31 formed in a hollow columnar shape and an elongated cylindrical part 32, and a two-stage columnar hollow formed by connecting the cylindrical part 32 to the center of the upper surface of the container 31. An opening 33 is formed on the outer peripheral surface of the container 31.

  As mentioned above, although the form of the rotation container applicable to this embodiment was illustrated in FIG. 5 and FIG. 6, the rotation container in this embodiment is not limited to the form mentioned above, It connects to the discharge side of a fluid. A hollow container having a rotationally symmetric shape with a hollow portion, which may have any shape as long as it has at least one opening on its wall surface, and those skilled in the art can make various design changes. Will.

  Next, a description will be given based on the second embodiment of the first form of the present invention. FIG. 7 shows a two-phase fluid separation device 40 according to a second embodiment of the invention. As shown in FIG. 7A, the two-phase fluid separation device 40 includes a rectangular parallelepiped sealed container 41 for introducing the two-phase fluid to be separated, and a circular shape formed on the outer wall surface 41 a of the sealed container 41. A regular circular rotating wall 42 fitted to the opening so as to be flush with the outer wall surface is included. The rotating wall 42 is connected to a rotation driving means 43 such as a motor via a shaft 44 perpendicular to the outer wall surface 41a of the sealed container 41, and the shaft 44 serves as a rotating shaft at a desired speed in the direction of arrow R. It is comprised so that rotation control is possible. Further, as shown in FIG. 7B, the discharge flow path 45 is formed on the outer wall surface 41 a of the sealed container 41 so as to cover the rotating wall 42.

  The rotating wall 42 is formed in a regular circular disk shape, and two openings 46a and 46b penetrating the rotating wall 42 are formed. The internal space of the sealed container 41 passes through the openings 46a and 46b. And communicated with the discharge channel 45. The openings 46a and 46b shown in FIG. 7 are formed in an elongated rectangular shape, and with respect to the rotating wall 42 such that the long sides of the openings 46a and 46b are substantially perpendicular to the rotating direction of the rotating wall 42 indicated by the arrow R. Is formed.

The principle that the two-phase fluid separation device 40 having the above-described configuration separates the two-phase fluid is basically the same as that described above for the first embodiment. Here, two-phase fluid introduced at a predetermined flow rate Q ₀ in the sealed container 41 from the introduction flow path 47 has an opening 46a formed in the rotating wall 42, from 46b, the discharge flow path 45 side at the same flow rate Q ₀ Therefore, the rotational speed (rpm) of the rotating wall 42 can be obtained by the following procedure.

First, the flow rate Q ₀ of the openings 46a, obtains a flow velocity u is divided by the area of the 46b, calculates the flow rate {q = uh} per unit length of the two-phase fluid discharged. Here, when the particle diameter {d} of the particle L to be kept in the closed container 41 is a two-phase fluid in which the particle follows the fluid, the relative velocity satisfying {U ≧ 2q / d}. U (required flow velocity of the flow R of the two-phase fluid in the short side direction of the opening 46) is calculated. On the other hand, when the particle is a two-phase fluid that does not follow the fluid, a relative velocity U that satisfies the above-described {Y / d ≦ 0.5} is calculated. Based on these calculated relative speeds U, a rotational speed (rpm) necessary to realize this is obtained. By controlling the operation of the two-phase fluid separation device 42 with the rotation speed, the particles L and the particles S in the two-phase fluid can be separated.

  Next, with reference to FIG. 8, it demonstrates based on 3rd Embodiment of the 1st form of this invention. FIG. 8 shows a two-phase fluid separation device 50 according to a third embodiment of the invention. As shown in FIG. 8A, the two-phase fluid separation device 50 includes a hollow cylindrical sealed container 51 for introducing the two-phase fluid to be separated, and a part of the sealed container 51 in the circumferential direction is A cylindrical rotating wall 52 is formed so as to be rotatable about the central axis of the sealed container 51 (column). The cylindrical rotating wall 52 is rotatably connected to the outer wall of the hermetic container 51 by a rotary joint 53, and from a rotation driving means 55 such as a motor via a gear 54 provided on the outer periphery of the rotating wall 52. Power is transmitted, and the rotation is controlled at a desired speed in the arrow R direction with the central axis of the sealed container 51 as the rotation axis.

  Two openings 55a and 55b are formed through the rotating wall 52, and the internal space of the sealed container 51 communicates with the outside of the sealed container 51 through the openings 55a and 55b. The openings 55a and 55b shown in FIG. 8 are formed in an elongated rectangular shape, and with respect to the rotating wall 52 such that the longitudinal sides of the opening 55a and 55b are substantially perpendicular to the rotating direction of the rotating wall 52 indicated by the arrow R. Is formed. Further, as shown in FIG. 8B, a discharge flow path 56 is formed on the outer peripheral wall surface of the sealed container 51 so as to cover the rotating wall 52, and the inner space of the sealed container 51 has an opening 55a. , 55b and the discharge flow path 56. The principle that the two-phase fluid separation device 50 shown in FIG. 8 separates the two-phase fluid is basically the same as that described above for the second embodiment, and thus the description thereof is omitted.

  As mentioned above, although the 1st form of this invention was demonstrated with 1st Embodiment-3rd Embodiment, the opening part formed in the rotation container and rotation wall in this invention is a rectangle with a large aspect ratio, parallel four sides It is preferably formed as a slit opening such as a shape or a fan shape, and it is preferable that the long side thereof is formed so as to face the rotation direction of the rotating container approximately perpendicularly. In addition, about the shape of the opening part and its number, a suitable aspect can be employ | adopted suitably according to mounting of each apparatus. In addition, in the first type of the present invention, in order to prevent the surrounding fluid from generating vortices due to the rotation of the rotating container or the rotating wall, a baffle plate or the like is provided at an appropriate position near each opening. Rectification means can be installed.

  As described above, with reference to FIGS. 4 to 6, among the implementations of the two-phase fluid separation device of the present invention, relative movement between the stationary two-phase fluid and the two-phase fluid is performed by circulating the opening side. Having described the first form for generating the velocity, the second type for generating the relative speed between the two openings by circulating the two-phase fluid with respect to the stationary opening will now be described. This will be described below with reference to FIG.

  FIG. 9 shows a two-phase fluid separation device 60 which is a second type of embodiment of the present invention. As shown in FIG. 9A, the two-phase fluid separation device 60 rotates a hollow cylindrical sealed container 61 for introducing the two-phase fluid to be separated, and the two-phase fluid introduced into the sealed container 61. A rotary stirring blade 62 for stirring is included. An opening 63 that is a rectangular through hole is formed on the bottom surface 61 b of the sealed container 61, and the discharge flow path 64 is connected to the bottom surface 61 b so as to communicate with the opening 63. In addition, the opening part 63 can employ | adopt an appropriate | suitable aspect suitably similarly to having demonstrated the 1st format mentioned above.

  The rotary stirring blade 62 is rotationally driven by a rotational driving means (not shown) so that the rotational direction of the rotary stirring blade 62 is substantially perpendicular to the long side of the rectangular opening 63. As a result, a flow R of the two-phase fluid is formed so as to face the long side of the rectangular opening 63 approximately perpendicularly, and a relative velocity is generated between the two-phase fluid and the opening 63.

The principle that the two-phase fluid separation device 60 having the above-described configuration separates the two-phase fluid is basically the same as that described above for the first embodiment of the first type except the configuration for generating the relative velocity. The same. In other words, two-phase fluid introduced at a predetermined flow rate Q ₀ in the sealed container 61 from the introduction flow path 65 from the opening 63 formed in the bottom surface 61b, and is discharged from the discharge passage 64 at the same flow rate Q _0. The flow rate Q ₀ is divided by the area of the discharge channel 64 obtains the flow velocity u and calculates the flow rate {q = uh} per unit length of the two-phase fluid discharged.

  Here, when the particle diameter {d} of the particle L that is desired to remain in the sealed container 61 is set, and the particle is a two-phase fluid that follows the fluid, the relative velocity satisfying {U ≧ 2q / d}. U (required flow velocity of the flow R of the two-phase fluid in the short side direction of the opening 63) is calculated. On the other hand, when the particle is a two-phase fluid that does not follow the fluid, a relative velocity U that satisfies the above-described {Y / d ≦ 0.5} is calculated. Based on these calculated relative speeds U, a rotational speed (rpm) necessary to realize this is obtained. By controlling the operation of the two-phase fluid separation device 42 with the rotation speed, the particles L and the particles S in the two-phase fluid can be separated. In the present embodiment, the opening 63 and the discharge passage 64 communicating with the opening 63 may be formed on the outer peripheral surface 61a of the sealed container 61 as shown in FIG. 9B.

  In the first type and second type embodiments described above, the container in which the two-phase fluid is stored is described as a sealed container, but the present invention uses the container for storing the two-phase fluid as an open container. It can also be configured. FIG. 10A shows a two-phase fluid separation device 10-2 in which the two-phase fluid storage container is configured as an open container 11-2 in the configuration illustrated in FIG. In the two-phase fluid separator 10-2, the flow rate {q} per unit length of the fluid to be discharged is controlled by providing a flow rate control valve 18 on the discharge side of the two-phase fluid, and the flow rate { It is preferable to operate by selecting a rotation speed suitable for q} and the critical particle size.

  Further, FIG. 10B shows a two-phase fluid separation device 10-3 in which the two-phase fluid storage container is configured as a tube 11-3 having no closed end in the configuration illustrated in FIG. In the two-phase fluid separation device 10-3, in addition to providing the flow control valve 18 on the discharge side of the two-phase fluid, the flow control valve 19 is provided behind the pipe 11-3 in the flow direction, and is operated. A two-phase fluid containing large particles with a high concentration is discharged downstream of the control valve 19. The application development described above is not limited to the modification of the configuration illustrated in FIG. 4, and can be similarly applied to all the other embodiments of the format 1 and the format 2 described above.

  The two-phase fluid separation apparatus of the present invention can be applied to all gas-liquid, solid-liquid, and solid-gas two-phase fluids, and various processes can be performed with one apparatus. For example, by targeting particles with a predetermined diameter or more and concentrating them in the container, it is possible to introduce a plurality of particle size distributions by introducing only the fluid containing no particle component into the container and continuing to operate. It is also possible to carry out a process of removing (removing) only the particle components having a diameter smaller than a predetermined diameter from the container from the two-phase fluid having

  Furthermore, the two-phase fluid separation device of the present invention can reliably separate particles even when the specific gravity difference of each phase of the two-phase fluid is small, and the limiting particle diameter of filtering is controlled by the rotational speed control. Can be easily changed. In addition, the two-phase fluid separation device according to the present invention does not generate large gravity to target particles (particles having a large specific gravity), which is unavoidable in the conventional centrifugal filter device, so that fragile particle components are separated. It is effective for various applications.

  Hereinafter, the two-phase fluid separation device of the present invention will be described more specifically with reference to examples. However, the present invention is not limited to the examples described later.

Example 1
A solid-liquid separator model to which the present invention was applied was prepared, and an evaluation experiment was performed according to the following procedure. FIG. 11 shows the produced solid-liquid separator model 100. The solid-liquid separator model 100 of this embodiment communicates with a container 101 (width 40 cm, depth 23 cm, height 27 cm), a rotating container 120 rotatably supported by a support 102, and the inside of the rotating container 120. The drainage pipe 103 connected in such a manner.

  The rotating container 120 is configured as a T-shaped container in which a cylinder is connected to the upper surface of a rectangular parallelepiped, and two openings 121a and 121b are formed on the bottom surface of the rectangular parallelepiped portion. The shapes of the openings 121a and 121b are both fan-shaped with a radius R1 = 55 mm (center angle θ = 5.7 °) centered on the rotation center c and a radius R2 = 40 mm similarly centered on the rotation center c. The remaining shape is a fan shape with a central angle of 5.7 °. Further, the upper end of the cylindrical portion of the rotating container 120 and the drain pipe 103 were connected by a rotary joint 104. Further, the rotation of the motor 105 disposed on the support 102 is transmitted to the cylindrical portion of the rotating container 120 via the pulley 106, the connecting belt 107, and the pulley 108, and the rotating container 120 is rotationally driven.

  In the container 101, a solid-liquid two-phase fluid 109 to be separated was stored. In this example, a solid-liquid two-phase fluid having the same specific gravity between the liquid phase and the solid phase was used as the test fluid. Specifically, a test fluid was prepared by dispersing polystyrene spherical particles having a diameter of 2.1 mm and a specific gravity of 1.044 in saline similarly adjusted to a specific gravity of 1.044.

  It arrange | positioned so that the rectangular parallelepiped part of the rotation container 120 might be immersed in the solid-liquid two-phase fluid 109. FIG. In addition, the drain pipe 103 is fixed so that the end of the drain pipe 103 is below the water surface of the solid-liquid two-phase fluid 109, and the fluid in the rotating container 120 is naturally sucked up to the drain pipe 103 side and discharged by the siphon principle. It was to so.

  In the solid-liquid separator model 100 described above, the condition of the rotational speed (rpm) of the rotating container 120 was changed, and the mass of polystyrene particles contained in the test fluid discharged from the drain pipe 103 was measured.

  FIG. 12 shows the relationship between the mass flow rate (g / s) of the discharged liquid discharged from the drain pipe 103 and the rotation speed (rpm) of the rotating container 120. As shown in FIG. 12, the resistance of water increases as the rotational speed of the rotating container 120 increases, and the mass flow rate (g / s) of the discharged liquid decreases.

  FIG. 13 shows the relationship between the mass (g / s) of polystyrene particles contained in the effluent discharged per unit time and the rotational speed (rpm) of the rotating container 120. In addition, about the mass of the polystyrene particle | grains, the waste liquid was sieved, the polystyrene particle | grains were capture | acquired, the moisture was wiped off, and the mass was measured after drying. As shown in FIG. 13, the mass (g / s) of polystyrene particles contained in the discharged liquid decreased as the rotation speed of the rotating container 120 increased.

  Here, the data on the mass flow rate (g / s) of the effluent shown in FIG. 12 and the data on the mass (g / s) of polystyrene particles contained in the effluent shown in FIG. The mass percent concentration (%) of the polystyrene particles contained was derived. FIG. 14 shows the relationship between the mass percent concentration (%) of polystyrene particles contained in the effluent and the rotational speed (rpm) of the rotating container 120. As shown in FIG. 14, the mass percent concentration (%) of polystyrene particles contained in the discharged liquid decreased substantially linearly as the rotational speed of the rotating container 120 increased.

  Based on the experimental results described above, it was verified whether or not the behavior of the solid-liquid separator model 100 of this example matched the above theoretical formula (2) of the present inventor.

FIG. 15 shows the relationship between the volume concentration ratio (α / α ₀ ) and {ζ = Ud / uh} in the experimental data obtained for the solid-liquid separator model 100 of this example. In this embodiment, for each term in {ζ = U · d / (u · h)}, U: relative speed due to rotation of the rotating container 120, d: diameter of polystyrene particles, u: inside the drainage pipe 103 , H: the width of the opening 121. Here, S: area of the opening 121, r: the radius of an arbitrary point, N: rotational speed of the rotating vessel 120, n: number of openings 121, Q _0: when the flow rate flowing out of the drain pipe 103, U = 2π · r · N, S = (R1 ² −R2 ² ) · θ · n, h = r · θ, u = Q ₀ / S, and ζ is expressed by the equation {ζ = Ud / (uh) = 2πN · n · d (R1 ² −R2 ² ) / Q ₀ }. The experimental results were in good agreement with the theoretical straight line indicated by the broken line, as indicated by the ● plot in FIG.

Furthermore, after replacing the rectangular parallelepiped container of the rotating container 120 with the hollow bowl-shaped container surrounded by the broken line in FIG. 5A, an experiment was performed under the same conditions as described above. The relationship between the volume concentration ratio (α / α ₀ ) and {ζ = Ud / uh} was determined. The result of the plot of Δ in FIG. 15 shows the result. As FIG. 15 shows, the experimental result using the rotation container 120 which provided the opening part in the phase part of the bowl-shaped container brought the result which approximated the theoretical value shown with a broken line.

(Example 2)
Next, a gas-liquid separator model to which the present invention was applied was produced, and an evaluation experiment was performed according to the following procedure. FIG. 16A shows the produced gas-liquid separator model 200. The gas-liquid separator model 200 of this example was produced by forming an air inlet 202 and an air outlet 203 with respect to a sealed container 201 (width 50 cm, depth 30 cm, height 30 cm). A fan 204 is provided at the air inlet 202 to introduce outside air into the sealed container 201. On the other hand, a rotary plate 220 having an opening formed therein was rotatably fitted in the exhaust port 203, and was rotated by a motor 205. Furthermore, the exhaust port 203 was covered with a rectangular parallelepiped container 206 (width 40 cm, depth 25 cm, height 25 cm), and a pipe having an inner diameter of 54 mm was attached so as to penetrate the ceiling of the rectangular parallelepiped container 206. The exhaust flow rate was obtained by inserting a hot-wire anemometer from the side of the exhaust pipe 207 and measuring the flow rate in the pipe. In this experiment, air containing mist is aspirated by generating mist in an airtight container 201 using an agricultural sprayer 208 (BH-590: manufactured by Panasonic / generated mist particle size of 50 to 100 μm). A state equivalent to that introduced from the mouth 202 was reproduced.

  FIG. 16B shows a top view of the rotating plate 220. In this embodiment, two openings 221 a and 221 b are formed in the rotating plate 220. The shapes of the openings 221a and 221b are both fan-shaped with a radius R1 = 100 mm (center angle θ = 10 °) centered on the rotation center c and a radius R2 = 60 mm similarly centered on the rotation center c. It was set as the remaining shape which removed the fan shape of (center angle 10 degrees).

  In the gas-liquid separator model 200 described above, the condition of the rotational speed (rpm) of the rotating plate 220 was changed, and the mass of water droplets contained in the air discharged from the exhaust pipe 207 was measured. The amount of water droplets contained in the exhaust was measured by the following procedure. A gauze was attached to the outlet of the exhaust pipe 207 to prevent water droplets from flowing out earlier, and this gauze was collected later. Furthermore, the moisture adhering to the inner wall of the rectangular parallelepiped container 206 was completely wiped off with absorbent cotton, the masses of the collected gauze and absorbent cotton were measured, and the increment of mass was the amount of water droplets contained in the exhaust.

  FIG. 17 shows the relationship between the volume flow rate (L / s) of the exhaust discharged from the exhaust pipe 207 and the rotational speed (rpm) of the rotating plate 220. As shown in FIG. 17, the volumetric flow rate (L / s) of the exhaust gas decreased because the air resistance increased as the rotational speed of the rotating plate 220 increased.

  FIG. 18 shows the relationship between the mass (mg / s) of water droplets contained in the exhaust gas discharged per unit time and the rotational speed (rpm) of the rotating plate 220. As shown in FIG. 18, the mass (mg / s) of water droplets in the exhaust decreased as the rotational speed of the rotating plate 220 increased.

Here, the data of the volume flow rate (L / s) of the exhaust shown in FIG. 17 and the data of the mass (mg / s) of the water droplets in the exhaust shown in FIG. The volume concentration (g / m ³ ) was derived. FIG. 19 shows the relationship between the volume concentration (g / m ³ ) of water droplets contained in the exhaust and the rotational speed (rpm) of the rotating plate 220. As shown in FIG. 19, the volume concentration (g / m ³ ) of water droplets contained in the exhaust gas decreased as the rotational speed of the rotating plate 220 increased.

FIG. 20 shows the relationship between the volume concentration ratio (α / α ₀ ) and the rotational speed (rpm) of the rotating plate 220 in the experimental data obtained for the gas-liquid separator model 200 of this example. The plots of ▲ and ■ in the figure show that the main spray particle size of the National Nebulizer BH-590 used is 50 to 100μ, so each rotation for 50μ (▲) and 100μ (■) The volume concentration ratio (α / α ₀ ) in the numbers is obtained by simulation calculation based on the above theoretical formula (2), and “x” in the figure indicates an experimental point. As shown in FIG. 20, the experimental results and the simulation results agreed well.

  Next, a solid-liquid separator model was prepared based on the second format described above with reference to FIG. 9, and an evaluation experiment was performed according to the following procedure. FIG. 21 shows the produced solid-liquid separator model 300. The solid-liquid separator model 300 of the present embodiment includes a container 301 (width 40 cm, depth 30 cm, height 30 cm) and a plate-like stirring blade 302 (width 14 cm, height 10 cm, thickness) disposed in the container 301. 5mm).

  Two openings 303a and 303b were formed on the bottom surface of the container 301, and a drainage channel 304 was formed so as to cover it. Note that the shapes of the openings 303a and 303b are both fan-shaped with a radius R1 = 55 mm (center angle θ = 5.7 °) centered on the intersection c with the rotation axis of the stirring blade 302. The remaining shape after removing the fan shape having a center radius R2 = 40 mm (central angle 5.7 °) was used.

  In this example, the same polystyrene spherical particle-saline dispersion as that used in Example 1 was stored in the container 301 as a test fluid. In the solid-liquid separator model 300 described above, the mass of polystyrene particles contained in the test fluid flowing out of the drainage channel 304 was measured by changing the rotation speed (rpm) condition of the stirring blade 302.

  For the solid-liquid separator model 300, the mass percent concentration (%) of polystyrene particles contained in the discharged liquid flowing out from the drainage channel 304 was calculated in the same procedure as in Example 1. FIG. 22 shows the relationship between the mass percent concentration (%) of polystyrene particles contained in the discharged liquid and the rotational speed (rpm) of the stirring blade 302. As shown in FIG. 22, the mass percent concentration (%) of polystyrene particles contained in the effluent decreased with an increase in the rotation speed of the stirring blade 302. In addition, each plot ((circle), (triangle | delta), (square)) shows that the same experiment was tried 3 times in order to confirm reproducibility.

  Based on the experimental results described above, it was verified whether or not the behavior of the solid-liquid separator model 300 of this example matched the above theoretical formula (2) of the present inventor.

FIG. 23 shows the relationship between the volume concentration ratio (α / α ₀ ) and {ζ = Ud / uh} in the experimental data obtained for the solid-liquid separator model 300 of this example. Note that the value of ζ was determined by the same concept as in Example 1. The experimental results were in good agreement with the theoretical solid line, as shown by the plots in FIG.

DESCRIPTION OF SYMBOLS 10 ... Two-phase fluid separator, 11 ... Sealed container, 12 ... Rotating container, 13 ... Rotation drive means, 14 ... Container, 15 ... Cylindrical part, 16 ... Opening part, 17 ... Introduction flow path, 18, 19 ... Flow control Valves, 20 ... Rotating container, 21 ... Container, 22 ... Cylindrical part, 23 ... Opening, 24 ... Bowl-shaped container, 25 ... Opening part, 26 ... Flat plate, 30 ... Rotating container, 31 ... Container, 32 ... Cylindrical part , 33 ... opening, 40 ... two-phase fluid separation device, 41 ... sealed container, 42 ... rotating wall, 43 ... rotation drive means, 44 ... shaft, 45 ... discharge channel, 46 ... opening, 47 ... introduction channel 50 ... Two-phase fluid separator, 51 ... Sealed container, 52 ... Rotary wall, 53 ... Rotary joint, 54 ... Gear, 55 ... Rotation drive means, 56 ... Discharge flow path, 60 ... Two-phase fluid separator, 61 ... Sealed container, 62 ... Rotating stirring blade, 63 ... Opening, 64 ... Discharge flow path, 6 DESCRIPTION OF SYMBOLS ... Introduction channel, 100 ... Solid-liquid separator model, 101 ... Container, 102 ... Support body, 103 ... Drain pipe, 104 ... Rotary joint, 105 ... Motor, 106 ... Pulley, 107 ... Connection belt, 108 ... Pulley, DESCRIPTION OF SYMBOLS 109 ... Solid-liquid two-phase fluid, 120 ... Rotary container, 121 ... Opening part, 200 ... Gas-liquid separator model, 201 ... Sealed container, 202 ... Intake port, 203 ... Exhaust port, 204 ... Fan, 205 ... Motor, 206 DESCRIPTION OF SYMBOLS ... rectangular parallelepiped container, 207 ... exhaust pipe, 208 ... agricultural sprayer, 220 ... rotating plate, 221 ... opening, 300 ... solid-liquid separator model, 301 ... container, 302 ... stirring blade, 303 ... opening, 304 ... drainage Flow path,

Claims (4)

A two-phase fluid separation device for separating particulate components in a two-phase fluid,
A storage container for storing a two-phase fluid;
It is composed of a hollow container having a rotationally symmetric shape and a cylindrical part connected to the center part of the bottom surface of the hollow container, and is rotatably arranged in the storage container, and the cylindrical part is connected to the discharge channel , A rotating container;
At least one opening having a long side facing the rotation direction is formed on the bottom surface of the hollow container constituting the rotating container,
By controlling the rotation speed of the rotating container, a fluid not containing a particle component having a predetermined diameter or more is sent to the discharge channel.
Two-phase fluid separator. A two-phase fluid separation device for separating particulate components in a two-phase fluid,
A container for storing a two-phase fluid, wherein a part of the wall surface of the container is rotatably configured;
A discharge channel connected to the storage container so as to cover the wall surface configured to be rotatable, and
On the wall surface configured to be rotatable, at least one opening having a long side facing the rotation direction is formed,
The discharge channel is provided so as to communicate with the storage container through the opening,
By controlling the rotational speed of the wall surface configured to be rotatable, a fluid that does not contain a particle component having a predetermined diameter or more is sent to the discharge flow path.
Two-phase fluid separator. The wall surface configured to be rotatable is a regular circular rotating wall whose axis of rotation is an axis perpendicular to the outer wall surface of the container.
The two-phase fluid separator according to claim 2. The wall surface configured to be rotatable is a part of the outer peripheral wall of the container configured as a hollow cylinder, and is a cylindrical rotating wall having the central axis of the hollow cylinder as a rotation axis.
The two-phase fluid separator according to claim 2.