JP2011147932A - Fluid-mixing device - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To suppress turbulence of a first and second fluid flow in the preceding stage of an expansion region of a flow path. <P>SOLUTION: A fluid-mixing device 100 includes a small-diameter pipe 11 and a large-diameter pipe 12 which stores the small-diameter pipe 11, and is provided with a fluid flow path part 10 which comprises a first flow path 11a in the small-diameter pipe 11 and a second flow path 12a in the large-diameter pipe 12 and outside the small-diameter pipe 11, a fluid joining contraction part 20 which is arranged at a fluid flow-out side of the fluid flow path part 10, which comprises a fluid joining region 21 where a first fluid passes through the first flow path 11a and a second fluid passes through the second flow path 12a and in which the joined first and second fluid are contracted to bore fine pores 22, and a flow path expansion part 30 which is arranged at the fluid flow-out side of the fluid joining contraction part 20 and includes a flow path expansion region 31 where the first and second fluid which have contracted the fine pore 22 flow in. The small-diameter pipe 11 is so formed that a pipe thickness of pipe end part 11b of the fluid flow-out side gets thinner toward a pipe end. <P>COPYRIGHT: (C)2011,JPO&INPIT

Description

  The present invention relates to a fluid mixer, and a fluid mixing method and an emulsion production method using the fluid mixer.

  Various fluid mixers have been proposed that allow a plurality of fluids to join and circulate through the pores.

  Patent Document 1 is an emulsification apparatus that produces an emulsion in which a dispersed phase is uniformly dispersed in a continuous phase, and includes an emulsifier, a dispersed phase supply piping system, a continuous phase supply piping system, and an emulsion discharge piping system. The emulsifier is a continuous phase that produces a primary emulsion by discharging a dispersed phase from a nozzle provided in a dispersed phase introduction channel that communicates with the dispersed phase supply piping system into a continuous phase that flows in a channel communicating with the continuous phase supply piping system. Produces a secondary emulsion by introducing an introduction channel, a stirring chamber adjacent to the continuous phase introduction channel downstream of the primary emulsion and agitating the primary emulsion adjacent to the stirring chamber downstream. And a decelerating chamber that is adjacent to the channel on the downstream side thereof and decelerates the secondary emulsion to send it to the emulsion discharge piping system.

  Patent Document 2 discloses an emulsifying apparatus for obtaining an emulsion by supplying two kinds of liquids, which are a dispersed phase and a continuous phase of an emulsion, to a micro-channel and emulsifying in the micro-channel. The liquid that becomes the continuous phase that flows between the cylinders of the double cylinder as a micro flow path is dispersed and supplied so as to be orthogonal to each other from a plurality of micro nozzles provided in the inner tube. Disclosed is an emulsifier for obtaining a primary emulsion, and a venturi tube provided adjacent to the emulsifier to pass a primary emulsion to obtain a secondary emulsion having a fine dispersed phase. Has been.

  Patent Document 3 discloses a first fluid guide device for guiding a first fluid and a second fluid in an apparatus for mixing fluid, particularly a gas injection valve, a mixing nozzle or a jet compression nozzle. And a second fluid guide device for fluid to be mixed with each other in a mixing region connected to both fluid guide devices, and at least one of the two fluid guide devices. The fluid guide device is associated with a means for generating turbulent flow in the fluid and a heating device disposed downstream of the means for generating turbulent flow with respect to the flow direction of the fluid. The heating device is disclosed so that the fluid can be heated before reaching the mixing region.

  In Patent Document 4, a fluid jet having a diameter smaller than the inner diameter of the absorption cell is injected from one end of the cylindrical absorption cell into the absorption cell at a speed higher than 500 feet per second, so that the jet speed is coaxial with the fluid jet. An emulsifying device is disclosed that is configured to generate a sufficiently slow fluid flow in an absorption cell and convert the kinetic energy of the fluid jet to shear energy at the interface between the fast fluid jet and the sufficiently slow fluid flow. Yes.

  Patent Document 5 discloses a fluid circulation pipe in which a plurality of fluid flow paths extending in parallel with each other inside the pipe are configured along the length direction, and the fluid circulation is continuously provided on the fluid outflow side of the fluid circulation pipe. A fluid mixing section in which a fluid reservoir region for storing a plurality of types of fluids flowing out from the pipe in a mixed state is formed, and mixing pores for circulating the plurality of types of fluids for laminar mixing Are disclosed.

JP 2007-313466 A JP 2007-111667 A JP-T-2004-536711 JP 2000-33249 A JP 2006-289250 A

  For example, when an emulsion is produced by joining an oil phase that is a dispersed phase and an aqueous phase that is a continuous phase, and then constricting them through pores and flowing them into a channel expansion area, It has been found that the dispersion mixing into the aqueous phase, that is, the emulsification, is mainly performed by convective mixing in the channel expansion region. Therefore, in order to carry out emulsification by uniformly dispersing and mixing the oil phase into the aqueous phase, the oil phase and the aqueous phase are premixed in the previous stage of the flow path expansion region where convective mixing occurs, which is undesirable. In other words, it is desirable that the turbulence of the flow of the oil phase and the water phase is small.

  The subject of this invention is suppressing the disturbance of the flow of the 1st and 2nd fluid in the front | former stage of a flow-path expansion area.

The fluid mixer of the present invention comprises:
A small-diameter pipe, and a large-diameter pipe that accommodates the small-diameter pipe in the same length direction. A first flow path is formed inside the small-diameter pipe, and the inside of the large-diameter pipe and the small diameter A fluid flow path portion in which a second flow path is configured outside the pipe;
A fluid merging area is provided on the fluid outflow side of the fluid flow path portion, where the first fluid flowing through the first flow path and the second fluid flowing through the second flow path merge, and the merge A fluid merging and converging part in which pores through which the first and second fluids contracted are perforated,
A flow path expanding portion that is provided on the fluid outflow side of the fluid converging and contracting section and that constitutes a flow path expanding area into which the first and second fluids that have flowed through the pores flow; and
With
The small-diameter pipe is formed so that the pipe thickness decreases as the pipe end portion on the fluid outflow side goes to the pipe end.

  The fluid mixing method of the present invention uses the fluid mixer of the present invention, and the first fluid flowing through the first flow path and the second fluid flowing through the second flow path are combined with the fluid. In the merging zone, the first fluid is joined so as to be covered with the second fluid, the first and second fluids joined in the fluid merging zone are contracted into the pores, and the pores are contracted The first and second fluids are caused to flow into the channel expansion area.

  The method for producing an emulsion according to the present invention uses the fluid mixer according to the present invention, wherein a fluid that is one of a continuous phase and a dispersed phase is used as the first fluid and a fluid that is the other as the second fluid. Using the fluid flowing through the first flow path and the fluid flowing through the second flow path in the fluid merging area, converging the fluid merged in the fluid merging area into the pores, and The fluid that has flowed through the pores is allowed to flow into the flow path expansion region.

  According to the present invention, the pipe end portion on the fluid outflow side of the small-diameter pipe is formed so that the pipe thickness decreases as it goes to the pipe end, so that the first and second fluids gradually approach and gradually merge. Therefore, the turbulence of the flow of the first and second fluids can be suppressed in the previous stage of the flow path expansion region.

It is a figure which shows the structure of the fluid mixing system which concerns on embodiment. It is a fragmentary longitudinal cross-sectional view of the principal part in a fluid mixer. It is the III-III sectional view in FIG. It is a fragmentary longitudinal cross-sectional view of the principal part in the modification of a fluid mixer. (A) Examples 1-3 and 5-7, (b) It is a fragmentary longitudinal cross-section of the principal part in the fluid mixer used in Example 4. FIG. (A) It is a partial longitudinal cross-sectional view of the principal part in the fluid mixer used in Comparative Examples 1 and 2 and (b) Comparative Example 3.

  Hereinafter, embodiments will be described in detail based on the drawings.

  FIG. 1 shows a fluid mixing system A according to this embodiment.

  The fluid mixing system A according to the present embodiment is used for mixing two kinds of fluids, and includes a fluid mixer 100 and an incidental part such as a fluid supply system.

  2 and 3 show a fluid mixer 100.

  The fluid mixer 100 includes a fluid flow path section 10, a fluid merging / contracting section 20 continuously provided on the fluid outflow side, and a flow path expanding section 30 continuously provided on the fluid outflow side. ing. As will be described below, the fluid mixer 100 is configured to suppress disturbance of the fluid flow in the previous stage of the flow path expanding unit 30.

  The fluid flow path unit 10 includes a small-diameter pipe 11 and a large-diameter pipe 12 that accommodates the small-diameter pipe 11 in the same length direction. As a result, in the fluid flow path section 10, the first flow path 11 a is configured inside the small diameter pipe 11, and the second flow path 12 a is configured inside the large diameter pipe 12 and outside the small diameter pipe 11. As described above, since the second flow path 12a is configured inside the large diameter pipe 12 and outside the small diameter pipe 11, the inside of the large diameter pipe 12 can be utilized to the maximum as a fluid flow path. The first and second fluids flow through the first flow path 11a and the second flow path 12a, respectively. From the viewpoint of suppressing the disturbance of the flow, the small diameter pipe 11 and the large diameter pipe 12 have a cross-sectional shape. Are preferably provided coaxially so as to be symmetrical. The first flow path 11a in the small diameter pipe 11 communicates with a first fluid supply unit (not shown) provided at one end of the apparatus, and the second flow path 12a in the large diameter pipe 12 is connected to the side surface of the apparatus. Is communicated with a second fluid supply section (not shown).

  The small-diameter tube 11 is not particularly limited in the cross-sectional shape of the outer shape and the hole. For example, the small-diameter tube 11 is circular, semicircular, elliptical, semielliptical, square, rectangular, trapezoidal, parallelogram, star shape. It may be indefinite or the like. The large-diameter tube 12 is not particularly limited in the cross-sectional shape of the hole, and is similar to the small-diameter tube 11, for example, circular, semicircular, elliptical, semielliptical, square, rectangular, trapezoidal, parallelogram May be a star shape, an indefinite shape, or the like. However, from the viewpoint of suppressing the disturbance of the flow of the first and second fluids flowing through the first flow path 11a and the second flow path 12a, respectively, the outer shape and the hole of the small diameter pipe 11 and the hole of the large diameter pipe 12 Each cross-sectional shape is preferably circular. That is, the cross-sectional shape of the first channel 11a is preferably circular, and the cross-sectional shape of the second channel 12a is preferably a donut shape.

  The small-diameter tube 11 may have the same outer shape or the same cross-sectional shape of the hole along the length direction, or may have a different shape. The large-diameter pipe 12 may have the same cross-sectional shape along the length direction of the hole, or may have a different shape. However, from the viewpoint of suppressing the disturbance of the flow of the first and second fluids flowing through the first flow path 11a and the second flow path 12a, respectively, the outer shape and the hole of the small diameter pipe 11 and the hole of the large diameter pipe 12 Each cross-sectional shape is preferably the same shape along the length direction. That is, it is preferable that the cross-sectional shape of both the first flow path 11a and the second flow path 12a is uniform to the pipe end along the length direction.

  The small diameter tube 11 has an outer diameter of, for example, 1.6 to 25 mm, preferably 3 to 15 mm, when both the outer shape and the hole have a circular cross section. The small diameter tube 11 has an inner diameter, that is, a flow path diameter of the first flow path 11a of, for example, 0.8 to 20 mm, and preferably 2 to 10 mm. When the cross-sectional shape of the hole is circular, the large-diameter tube 12 has an inner diameter of, for example, 1.8 to 50 mm, and preferably 4 to 20 mm. Moreover, the clearance gap of the 2nd flow path 12a between the small diameter pipe | tube 11 and the large diameter pipe | tube 12 is 0.1-12.5 mm, for example, and it is preferable that it is 0.3-6 mm.

  The small-diameter pipe 11 is formed such that the pipe thickness decreases as the pipe end portion 11b on the fluid outflow side goes to the pipe end. The shape of the pipe end portion 11b of the small-diameter pipe 11 is not particularly limited, but the first fluid that flows through the first flow path 11a and the second fluid that flows through the second flow path 12a gently merge. From the viewpoint of suppressing disturbance of the flow, the outer peripheral portion is preferably formed in a tapered shape, and the cross-sectional shape in the thickness direction is formed in a steeple shape sharp on the inner peripheral side. Is more preferable. Further, from the same viewpoint, the shape of the tube end portion 11b of the small-diameter tube 11 is such that the outer diameter of the tube end portion 11b gradually decreases from the upstream side to the downstream side along the length direction rather than the tapered shape. It may be. Specifically, as shown in FIG. 4, the pipe end portion 11 b of the small-diameter pipe 11 is formed in a curve in which the contour along the longitudinal direction of the outer peripheral surface thereof bulges outward such as an arc. May be. The curvature radius of the curve is, for example, 1 to 30 mm.

  The large-diameter pipe 12 has a gap δ at a portion corresponding to the pipe end portion 11b of the small-diameter pipe 11 and a part of the second flow path 12a formed between the pipe inner wall and the pipe end portion 11b of the small-diameter pipe 11. Is preferably uniform in the fluid flow direction, and the gap δ is, for example, 0.02 to 12.5 mm, preferably 0.05 to 12.5, and preferably 0.1 to 12.5. Is more preferable, and it is still more preferable that it is 0.3-6 mm. Further, the gap δ may be on the order of 0.02 to 0.1 mm, may be on the order of 0.1 to 1.0 mm, or may be on the order of 1.0 to 12.5 mm. Good. The fluid merging / contracting portion 20 has a fluid merging area 21 formed in front of the pipe end of the small diameter pipe 11, and pores 22 are continuously drilled in the fluid merging area 21. In the fluid merge area 21, the first fluid that has flowed through the first flow path 11 a and the second fluid that has flowed through the second flow path 12 a merge, and in the pore 22, the first and second fluids that have merged in the fluid merge area 21. Two fluids contract.

  The shape of the fluid confluence region 21 is not particularly limited, and the cross-sectional shape may be formed in a uniform shape along the fluid flow direction. You may form in the taper shape which converges toward. The shape of the fluid merging area 21 may be an arm shape in which the inner diameter gradually decreases from the upstream side toward the downstream side along the length direction as compared with the cone shape. Specifically, as shown in FIG. 4, the fluid merging area 21 has a pair of curves in which the contours along the longitudinal direction of the inner wall surface of the inner wall surface bulge outward, such as an arc, and the like. You may form with the line segment which connects a curve. The curvature radius of the curve is, for example, 1 to 30 mm. In the fluid confluence region 21, the distance L from the tube end of the small-diameter tube 11, that is, the end of the fluid flow path portion 10 to the pore 22 is, for example, 0.02 to 20 mm, and preferably 0.2 to 20 mm. . The distance L may be on the order of 0.02 to 0.1 mm, may be on the order of 0.1 to 1.0 mm, or may be on the order of 1.0 to 20.0 mm. Good.

  The pores 22 are preferably formed so that the perforation direction extends in the direction along the fluid outflow direction, and are preferably perforated coaxially with the small diameter tube 11 and the large diameter tube 12.

  The cross-sectional shape of the pore 22 is not particularly limited, and may be, for example, circular, semicircular, elliptical, semielliptical, square, rectangular, trapezoidal, parallelogram, star, indefinite, or the like. May be. The pores 22 may have the same cross-sectional shape along the fluid flow direction, or may have different shapes. However, from the viewpoint of suppressing the disturbance of the flow of the first and second fluids that have joined together, the cross-sectional shape of the pores 22 is preferably circular, and may be the same shape along the length direction. preferable. That is, it is preferable that the flow path in the pore 22 has a uniform cross-sectional shape from the fluid inflow end to the fluid outflow end along the fluid flow direction.

The pore 22 has a pore length l of, for example, 0.05 to 5 mm, preferably 0.1 to 5 mm, more preferably 0.1 to 3 mm, and 0.3 to 3 mm. More preferably. The hole length l may be on the order of 0.05 to 0.1 mm, may be on the order of 0.1 to 1.0 mm, and may be on the order of 1.0 to 5.0 mm. Also good. When the cross-sectional shape is circular, the hole diameter d is, for example, 0.1 to 3 mm, and preferably 0.2 to 1.5 mm. Further, the hole diameter d may be on the order of 0.1 to 1.0 mm, or may be on the order of 1.0 to 3.0 mm. The hole area s is, for example, 0.01 to 7 mm ² , and preferably 0.03 to ² mm ² . The pore 22 preferably has a ratio l / d of the pore length l to the pore diameter d of 0.15 ≦ l / d ≦ 40, more preferably 0.2 ≦ l / d ≦ 40, More preferably, 5 ≦ l / d ≦ 40, and even more preferably 1 ≦ l / d ≦ 20. The ratio l / d of the hole length l to the hole diameter d may be 0.15 ≦ l / d ≦ 1.0, 1.0 ≦ l / d ≦ 10, or 10 ≦ It may be 1 / d ≦ 40.

  In the channel expanding portion 30, a channel expanding region 31 is configured in front of the pores 22. The first and second fluids that have flowed through the pores 22 flow into the flow channel enlargement region 31. In addition, the flow path expansion area 31 communicates with a fluid discharge portion (not shown) provided at the other end of the apparatus.

  The shape of the channel expansion region 31 is not particularly limited, and the cross-sectional shape may be formed in a uniform shape along the fluid flow direction. It may be formed in a shape opening from the end to the end. When the cross-sectional shape is circular, the flow path enlarged region 31 has a maximum inner diameter D of, for example, 0.8 to 40 mm, preferably 1.5 to 25 mm, and a pore diameter d of the pore 22 of 2.5. It is preferably ˜100 times, and more preferably 5 to 40 times.

  The fluid mixer 100 may be composed of a plurality of members each formed of metal, ceramics, resin, etc., and the fluid flow path unit 10, the fluid merging / contracting unit 20, And the flow path expansion part 30 may be comprised.

  According to the fluid mixer 100 described above, the pipe end portion 11b on the fluid outflow side of the small diameter pipe 11 is formed so that the pipe thickness decreases as it goes to the pipe end. Gradually approaching and gently merging, so that the turbulence of the flow of the first and second fluids can be suppressed in the previous stage of the flow path expansion region 31.

  In the fluid mixer 100 having the above-described configuration, one small-diameter pipe 11 is accommodated in the large-diameter pipe 12. However, the present invention is not particularly limited to this, and a plurality of small-diameter pipes 11 are large-diameter pipes. The structure accommodated in 12 may be sufficient.

  In the fluid mixer 100, a first raw material supply pipe 42a extending from the first raw material storage tank 41a is connected to a first fluid supply unit communicating with the first flow path 11a. The first raw material supply pipe 42a is upstream of a first pump 43a for circulating the first fluid, a first flow meter 44a for detecting the flow rate of the first fluid, and a first filter 45a for removing contaminants of the first fluid. A first pressure gauge 46a that detects the pressure of the first fluid is attached to a portion between the first flow meter 44a and the first filter 45a. Each of the first pump 43a, the first flow meter 44a, and the first pressure gauge 46a is electrically connected to the flow controller 47.

  A second raw material supply pipe 42b extending from the second raw material storage tank 41b is connected to the second fluid supply unit communicating with the second flow path 12a. In the second raw material supply pipe 42b, a second pump 43b for circulating the second fluid, a second flow meter 44b for detecting the flow rate of the second fluid, and a second filter 45b for removing impurities of the second fluid are upstream. A second pressure gauge 46b that detects the pressure of the second fluid is attached to a portion between the second flow meter 44b and the second filter 45b. Each of the second pump 43b, the second flow meter 44b, and the second pressure gauge 46b is electrically connected to the flow controller 47.

  The flow rate controller 47 is configured to be capable of inputting the set flow rate and set pressure of the first fluid and incorporates an arithmetic element, and the set flow rate information of the first fluid and the flow rate detected by the first flow meter 44a. The operation of the first pump 43a is controlled based on the information and the pressure information detected by the first pressure gauge 46a. Similarly, the flow rate controller 47 is also configured to be able to input the set flow rate and set pressure of the second fluid, and the set flow rate information of the second fluid, the flow rate information detected by the second flow meter 44b, and the second pressure. The second pump 43b is operated and controlled based on the pressure information detected by the total 46b.

  A mixed fluid recovery pipe 48 extends from the fluid discharge portion communicating with the flow path enlargement region 31 and is connected to the recovery tank 49.

  Next, the operation of the fluid mixing system A will be described in the case of producing an oil-in-water emulsion using the first fluid as a water phase as a continuous phase and the second fluid as an oil phase as a dispersed phase. The oil-in-water emulsion may be produced using the first fluid as the oil phase and the second fluid as the water phase. However, from the viewpoint of producing a uniform emulsion, the first fluid is designated as the continuous phase and the second fluid. A dispersed phase is preferable. Further, the first and second fluids are not particularly limited to this, and have fluidity other than the solid phase such as a gas phase, a liquid phase, a gas-liquid mixed phase, an emulsified phase, and a solid-liquid mixed phase (slurry). What is necessary is just the property of hold | maintaining.

  Examples of the oil phase include mineral oil, vegetable oil, and synthetic oil.

  Examples of the aqueous phase include water, an aqueous solution, a mixed solution of water and an organic solvent, and the like.

    When the fluid mixing system A is operated, the first pump 43a passes the water phase as a continuous phase from the first raw material storage tank 41a through the first raw material supply pipe 42a, sequentially through the first flow meter 44a and the first filter 45a. Then, it is continuously supplied to the first flow path 11a of the small diameter tube 11 of the fluid flow path section 10. The first flow meter 44 a sends the detected water phase flow rate information to the flow rate controller 47. Further, the first pressure gauge 46 a sends the detected pressure information of the first pressure gauge 46 a to the flow controller 47.

  The second pump 43b causes the oil phase to be a dispersed phase to pass through the second raw material storage tank 41b, the second raw material supply pipe 42b, and the second flow meter 44b and the second filter 45b in order, so that the fluid flow path unit 10 It supplies continuously to the 2nd flow path 12a between the large diameter pipe 12 and the small diameter pipe 11. FIG. The second flow meter 44 b sends the detected oil phase flow rate information to the flow rate controller 47. Further, the second pressure gauge 46 b sends the detected pressure information of the second pressure gauge 46 b to the flow rate controller 47.

  The flow controller 47 sets the water phase set flow rate information and the set pressure information, and the flow rate information detected by the first flow meter 44a and the pressure information detected by the first pressure meter 46a. And the first pump 43a is controlled to maintain the set pressure. At the same time, the flow controller 47 sets the oil phase based on the set flow rate information and set pressure information of the oil phase, and the flow rate information detected by the second flow meter 44b and the pressure information detected by the second pressure meter 46b. The second pump 43b is operated and controlled so that the set flow rate and the set pressure are maintained.

  In the fluid mixer 100, in the fluid flow path unit 10, the water phase flows through the first flow path 11a and the oil phase flows through the second flow path 12a. At this time, the flow rate of the aqueous phase (the flow velocity of the aqueous phase flowing into the fluid merge region 21 from the first flow path 11a) is, for example, 1 to 100 L / h, and the pressure is, for example, 0.01 to 5 MPa. The flow rate of the oil phase (the flow rate of the oil phase flowing into the fluid merging area 21 from the second flow path 12a) is less than the flow rate of the water phase, for example, 0.1 to 50 L / h, and the pressure is, for example, 0.01 ~ 5 MPa. Then, the flow rate of the water phase is set to 0.05 to 2 m / s by the flow rate setting and the pressure setting of the water phase, and the flow rate of the oil phase is set to, for example, 0.05 to 2 m by the flow rate setting and pressure setting of the oil phase. 2 m / s. In the fluid flow path part 10, the flow rate of the fluid combining the aqueous phase and the oil phase is, for example, 0.05 to 2 m / s.

  In the fluid confluence / condensation unit 20, the water phase and the oil phase that have flowed out of the fluid flow channel unit 10 are, in the fluid merge region 21, the oil phase from the second flow channel 12 a ahead of the water phase from the first flow channel 11 a. Flows in and merges in a form that covers the water phase with the oil phase. At this time, in the fluid confluence / confluence section 20, the flow rate of the fluid combined with the water phase and the oil phase is, for example, 0.05 to 2 m / s. From the viewpoint of suppressing turbulence in the flow of the water phase and the oil phase, the oil phase flowing into the fluid merge region 21 from the second flow channel 12a having the flow velocity of the water phase flowing into the fluid merge region 21 from the first flow channel 11a. The ratio to the flow rate is preferably 0.5-2. Further, the flow velocity of the fluid combined with the water phase and the oil phase in the fluid flow path portion 10 is made the same as the flow velocity at the time when the water phase and the oil phase in the fluid merging and contracting portion 20 are merged for the first time. Is preferably eliminated. Furthermore, the pressure loss before and after the fluid mixer 100 is preferably 0.01 to 5 MPa. These can be controlled by the flow rate setting and pressure setting of the oil phase and the water phase, respectively.

  The water phase and the oil phase that merged in the fluid merging zone 21 contract in the pores 22. At this time, from the viewpoint of suppressing the turbulence of the flow of the water phase and the oil phase, it is preferable that the water phase and the oil phase merged in the fluid merge region 21 are contracted into the pores 22 under laminar flow conditions. This can also be controlled by the respective flow rate settings and pressure settings of the water phase and the oil phase. The laminar flow condition is a flow condition in which the Reynolds number (Re) is smaller than 2300, and the contraction under the laminar flow condition means that the water phase and the oil phase are merged for the first time before the contraction starts. It means that the flow condition at the time is the laminar flow condition.

  In the flow channel enlargement unit 30, in the flow channel expansion region 31, the water phase and the oil phase that have flown through the pores 22 flow in, and an emulsion is produced by convective mixing between the water phase and the oil phase. Since the convective mixing between the water phase and the oil phase in the channel expansion region 31 dominates the emulsification, in order to perform uniform dispersion mixing of the oil phase into the water phase, Although it is preferable that the phase and the oil phase are premixed so as not to cause undesirable non-uniformity, according to the fluid mixing system A according to the present embodiment, the fluid mixer 100 is provided on the fluid outflow side of the small diameter pipe 11. Since the pipe end portion 11b is formed so that the pipe thickness becomes thinner as it goes to the pipe end, the water phase and the oil phase gradually approach and gradually merge, so that the water phase And turbulence in the flow of the oil phase can be suppressed. Therefore, the water phase and the oil phase are premixed in the previous stage of the channel expansion region 31, so that undesired non-uniformity does not occur, and the convection mixing that controls the emulsification in the channel expansion region 31 takes a short time. Uniform dispersion and mixing between the water phase and the oil phase can be performed, and as a result, an emulsion having a small droplet diameter and a narrow distribution can be obtained.

[Experiment 1]
Production experiments of the following emulsions of Examples 1 to 4 and Comparative Examples 1 to 2 were conducted. The contents of each are also shown in Table 1.

Example 1
Cyclic silicone (trade name: KF-995, manufactured by Shin-Etsu Chemical Co., Ltd.) as the oil phase to be the dispersed phase, and polyvinyl alcohol (product name: Gohsenol EG-05, manufactured by Nippon Gosei Kagaku Kogyo Co., Ltd.) as the aqueous phase to be the continuous phase. Each 5 mass% aqueous solution was prepared.

  And the fluid mixing system A of the same structure as the said embodiment was used, and the emulsion was manufactured for the said oil phase as the 1st fluid and the said water phase as the 2nd fluid. The fluid mixer 100 is supplied such that the oil phase and the water phase are mixed at a ratio of 20% by mass of the former and 80% by mass of the latter, and the flow rates of the oil phase and the water phase are 3.0 to 7%. Variable in the range of 0.0 L / h.

In the fluid mixer 100, as shown in FIG. 5A, each of the small-diameter pipe 11 and the large-diameter pipe 12 has a circular cross-sectional shape and is uniform along the length direction of the small-diameter pipe 11 to the pipe end. The inner diameter of the circular cross-sectional shape is 4 mm (therefore, the channel diameter of the first channel 11a is 4 mm), the outer diameter is 8 mm, and the inner diameter of the large-diameter tube is 10 mm (therefore, the gap between the second channels 12a is 1 mm). The tube end portion 11b of the small diameter tube 11 is formed so that the outer peripheral portion thereof is formed in a tapered shape, and the tube thickness is reduced toward the tube end, and is configured between the tube inner wall of the large diameter tube 12. The gap δ, which is a part of the second flow path 12a, is uniform and 2.5 mm. The fluid confluence region 21 is formed in a cone shape that converges at an angle of 120 °. The pore 22 has a pore length l of 0.75 mm, a pore diameter d of 0.3 mm (thus 1 / d = 2.5), and a pore area s of 0.07065 mm ² . The flow path enlargement region 31 is formed in a continuous cone shape in a cone shape that spreads at an angle of 120 °, and the maximum inner diameter D is 7 mm, which is 23 times the hole diameter d of the pores 22. The ratio of the flow rate of the oil phase flowing into the fluid merge region 21 from the first flow path 11a to the flow rate of the aqueous phase flowing into the fluid merge region 21 from the second flow path 12a was 1.0.

  As a result, the area-based average droplet diameter was 20.0 μm when the pressure loss before and after the fluid mixer 100 was 0.15 MPa. When the pressure loss was 0.34 MPa, the area-based average droplet diameter was 11.4 μm. The area-based average droplet diameter when the pressure loss was 0.63 MPa was 7.6 μm. The area-based average droplet diameter was measured by a laser scattering / diffraction method (Horiba, Ltd .: apparatus name LA-910) (hereinafter the same applies to Examples 2 to 4 and Comparative Examples 1 to 2).

(Example 2)
The pore length l is 1.75 mm, the pore diameter d is 0.7 mm (therefore, l / d = 2.5, the pore area s is 0.3847 mm ² ), and the maximum inner diameter D of the channel expansion region 31 is Is 10 mm that is 7 mm, and the gap δ forming a part of the second flow path 12 a formed between the pipe end portion 11 b of the small diameter pipe 11 and the pipe inner wall of the large diameter pipe 12 is uniform and 0.5 mm. A fluid mixer 100 having a configuration shown in FIG. 5A is used. The oil phase is the second fluid and the water phase is the first fluid, and the flow rates of the oil phase and the water phase are 20.0 to 44.0 L / An emulsion was produced in the same manner as in Example 1 except that the amount was changed in the range of h. The ratio of the flow rate of the water phase flowing from the first flow path 11a to the fluid merge area 21 to the flow velocity of the oil phase flowing from the second flow path 12a to the fluid merge area 12 was 1.2.

  As a result, the area-based average droplet diameter when the pressure loss before and after the fluid mixer 100 was 0.17 MPa was 16.1 μm. The area-based average droplet diameter when the pressure loss was 0.56 MPa was 8.6 μm. The area-based average droplet diameter when the pressure loss was 0.89 MPa was 7.4 μm.

(Example 3)
The pore length l is 0.15 mm, the pore diameter d is 0.3 mm (therefore, l / d = 0.5, the pore area s is 0.07065 mm ² ), and the maximum inner diameter D of the flow path expansion region 31 Is 23 mm, which is 7 mm, and the gap δ which is a part of the second flow path 12 a formed between the pipe end portion 11 b of the small diameter pipe 11 and the pipe inner wall of the large diameter pipe 12 is uniform and 0.5 mm. A fluid mixer 100 having a configuration shown in FIG. 5A is used, the oil phase is the second fluid and the water phase is the first fluid, and the flow rates of the oil phase and the water phase are 3.0 to 6.6 L / An emulsion was produced in the same manner as in Example 1 except that the amount was changed in the range of h. The ratio of the flow rate of the water phase flowing from the first flow path 11a to the fluid merge area 21 to the flow velocity of the oil phase flowing from the second flow path 12a to the fluid merge area 21 was 1.0.

  As a result, the area-based average droplet diameter when the pressure loss before and after the fluid mixer 100 was 0.11 MPa was 21.3 μm. The area-based average droplet diameter when the pressure loss was 0.33 MPa was 10.0 μm. The average droplet diameter based on area when the pressure loss was 0.50 MPa was 7.7 μm.

Example 4
The pore length l is 0.85 mm, the pore diameter d is 0.33 mm (therefore, l / d = 2.6, the pore area s is 0.08549 mm ² ), and the maximum inner diameter D of the flow path enlargement region 31 is Is 21 mm, 7 mm, and the gap δ, which is a part of the second flow path 12 a formed between the tube end portion 11 b of the small diameter tube 11 and the inner wall of the large diameter tube 12, is uniform and 0.5 mm. Yes, the contour along the longitudinal direction of the longitudinal section of the outer peripheral surface of the pipe end portion 11b of the small diameter pipe 11 is formed in an arc having a central angle of 90 °, and the length of the inner wall surface of the fluid confluence region 21 in the longitudinal section. The fluid mixer 100 having the configuration shown in FIG. 5B in which the contours along the vertical direction are each formed by a pair of circular arcs having a central angle of 90 ° and line segments connecting the circular arc curves is used. The oil phase is the second fluid and the water phase is the first fluid, and the flow rates of the oil phase and the water phase are 3.0 to Was produced emulsion in the same manner as in Example 1 except that the variable range of .2L / h. The ratio of the flow velocity of the water phase flowing from the first flow path 11a to the fluid merge area 21 to the flow velocity of the oil phase flowing from the second flow path 12a to the fluid merge area 21 was 1.2.

  As a result, the area-based average droplet diameter when the pressure loss before and after the fluid mixer 100 was 0.10 MPa was 23.3 μm. The area-based average droplet diameter when the pressure loss was 0.32 MPa was 10.9 μm. The area-based average droplet diameter when the pressure loss was 0.65 MPa was 7.4 μm.

(Comparative Example 1)
Using the fluid mixer 100 ′ having the configuration shown in FIG. 6 (a), the flow rate of the oil phase and the water phase was varied in the range of 9.6 to 21.0 L / h, and the same as in Example 1. An emulsion was produced.

As shown in FIG. 6A, the fluid mixer 100 ′ has a circular cross-sectional shape of each of the small-diameter tube 11 ′ and the large-diameter tube 12 ′, and extends along the length direction of the small-diameter tube 11 ′. The inner diameter of the circular cross-sectional shape that is uniform up to the tube end is 4.5 mm (therefore, the channel diameter of the first channel 11a ′ is 4.5 mm), the outer diameter is 6.4 mm, and the inner diameter of the large-diameter tube 12 ′. Is 18 mm (therefore, the gap between the second flow paths 12a ′ is 5.8 mm). The small-diameter pipe 11 ′ has a pipe end face perpendicular to the axial direction, and the pipe end is positioned 2 mm behind the converging start position of the fluid confluence region 21 ′ into the cone shape in the large-diameter pipe 12 ′. The fluid merging area 21 ′ is formed in a cone shape that converges at an angle of 120 °. The pore 22 'has a hole length l of 2 mm, a hole diameter d of 0.5 mm (thus 1 / d = 4), and a hole area s of 0.1963 mm ² . The flow path enlargement region 31 ′ is formed in a continuous cone shape in a cone shape spreading at an angle of 120 °, and the maximum inner diameter D is 18 mm, which is 36 times the hole diameter d of the pore 22 ′. is there. The ratio of the flow rate of the oil phase flowing from the first flow path 11a to the fluid merge area 21 to the flow velocity of the water phase flowing from the second flow path 12a to the fluid merge area 21 was 3.4.

  As a result, the area-based average droplet diameter was 26.7 μm when the pressure loss before and after the fluid mixer 100 ′ was 0.14 MPa. When the pressure loss was 0.20 MPa, the area-based average droplet diameter was 20.7 μm. When the pressure loss was 0.35 MPa, the area-based average droplet diameter was 13.8 μm. The area-based average droplet diameter when the pressure loss was 0.53 MPa was 10.3 μm. The area-based average droplet diameter when the pressure loss was 0.75 MPa was 8.9 μm.

(Comparative Example 2)
The configuration shown in FIG. 6 (a) is that the pore length l of the pore 22 ′ is 2 mm, the pore diameter d is 0.56 mm (thus 1 / d = 3.6), and the pore area s is 0.2462 mm ² . Except for using the fluid mixer 100 'and changing the flow rate of the oil phase and the water phase in the range of 16.0 to 30.0 L / h with the oil phase as the second fluid and the water phase as the first fluid. In the same manner as in Comparative Example 1, an emulsion was produced. The ratio of the flow velocity of the water phase flowing from the first flow path 11a to the fluid merge area 21 to the flow velocity of the oil phase flowing from the second flow path 12a to the fluid merge area 21 was 53.7.

  As a result, the area-based average droplet diameter was 19.0 μm when the pressure loss before and after the fluid mixer 100 ′ was 0.25 MPa. The area-based average droplet diameter when the pressure loss was 0.51 MPa was 11.7 μm. The area-based average droplet diameter when the pressure loss was 0.80 MPa was 9.2 μm.

  According to the results of the above Examples 1 to 4 and Comparative Examples 1 and 2, when comparing the average droplet diameter under the same pressure loss, in Examples 1 to 4, compared to Comparative Examples 1 and 2 It can be seen that the average droplet diameter is small.

[Experiment 2]
Reaction experiments of the following Examples 5 to 7 and Comparative Example 3 were performed. The contents are also shown in Table 2.

(Example 5)
As two aqueous solutions that react by mixing, 0.022N sulfuric acid and borate buffer were prepared. The composition of the borate buffer solution consists of boric acid 0.009 mol / L, sodium hydroxide 0.09 mol / L, potassium iodate 0.00625 mol / L, and potassium iodide 0.0313 mol / L. When these two liquids are mixed, the neutralization reaction (I) and the oxidation-reduction reaction (II) in which iodine is generated proceed simultaneously.

Here, since the amount of iodine produced decreases as the mixing of the two liquids is completed in a short time, the amount of I ₃ ⁻ ions in chemical equilibrium (III) with the produced iodine is determined at an absorption wavelength of 353 nm. It is possible to evaluate the mixing time. That is, when the mixed liquid is sampled and the absorbance is measured, the smaller the absorbance, the higher the mixing performance of the fluid mixer. This reaction system is academically used for the mixing performance evaluation of mixers and is generally called Villermaux / Dushman reaction. Details of this reaction system are described in P. Guichardon and L. Falk, Chemical Engineering Science 55 (2000) 4233-4243.

  Then, using the fluid mixing system A having the same configuration as that of the above embodiment, a reaction experiment was performed using the sulfuric acid as the first fluid and the boric acid buffer as the second fluid.

  The fluid mixer 100 (FIG. 5A) used in Example 1 was supplied with sulfuric acid and a borate buffer so that mixing was performed at a ratio of 50% by mass of the former and 50% by mass of the latter. At this time, the flow rates of sulfuric acid and borate buffer were set to 3.0 L / h. The ratio of the flow rate of sulfuric acid flowing from the first flow path 11a to the fluid merge area 21 to the flow rate of borate buffer flowing from the second flow path 12a to the fluid merge area 21 was 0.25.

  As a result, the pressure loss before and after the fluid mixer 100 was 0.118 MPa, and the absorbance was 0.033. The absorbance was measured with a spectrophotometer (Shimadzu Corporation: apparatus name UVmini-1240) (hereinafter the same applies to Examples 6 and 7 and Comparative Example 3).

(Example 6)
Reaction experiment similar to Example 5 except that the fluid mixer 100 (FIG. 5A) used in Example 2 was supplied with sulfuric acid and borate buffer at a flow rate of 12.0 L / h. Went. The ratio of the flow rate of sulfuric acid flowing from the first flow path 11a to the fluid merge area 21 to the flow rate of borate buffer flowing from the second flow path 12a to the fluid merge area 21 was 0.3.

  As a result, the pressure loss before and after the fluid mixer 100 was 0.094 MPa, and the absorbance was 0.021.

(Example 7)
A reaction experiment was conducted in the same manner as in Example 5 except that sulfuric acid and borate buffer were supplied to the fluid mixer 100 (FIG. 5A) used in Example 3. The ratio of the flow rate of sulfuric acid flowing from the first flow path 11a to the fluid merge area 21 to the flow rate of borate buffer flowing from the second flow path 12a to the fluid merge area 21 was 0.25.

  As a result, the pressure loss before and after the fluid mixer 100 was 0.104 MPa, and the absorbance was 0.020.

(Comparative Example 7)
A reaction experiment was conducted in the same manner as in Example 5 except that sulfuric acid and borate buffer were supplied at a flow rate of 4.8 L / h to the fluid mixer 100 ′ having the configuration shown in FIG. .

As shown in FIG. 6B, in the fluid mixer 100 ′, the small-diameter pipe 11 ′ and the large-diameter pipe 12 ′ each have a circular cross-sectional shape, and are along the length direction of the small-diameter pipe 11 ′. The inner diameter of the circular cross-sectional shape that is uniform up to the tube end is 1.7 mm (therefore, the channel diameter of the first channel 11a ′ is 1.7 mm), the outer diameter is 3.2 mm, and the inner diameter of the large-diameter tube 12 ′. Is 4.4 mm (therefore, the gap between the second flow paths 12a ′ is 0.6 mm). The small-diameter pipe 11 ′ has a pipe end surface perpendicular to the axial direction, and the pipe end is positioned 0.5 mm behind the pore 22 ′ in the large-diameter pipe 12 ′. The fluid merge area 21 ′ is formed in a cylindrical shape. The opposed surface of the tube end surface of the small-diameter tube 11 ′ is formed as a vertical wall-like flat surface. The pore 22 ′ has a pore length l of 0.9 mm, a pore diameter d of 0.3 mm (thus 1 / d = 3), and a pore area s of 0.07065 mm ² . The channel expansion area 31 ′ is formed in a cylindrical shape that spreads at an angle of 180 °, and the maximum inner diameter D is 1.1 mm, which is 3.7 times the hole diameter d of the pore 22 ′. The ratio of the flow rate of sulfuric acid flowing from the first flow path 11a to the fluid merge area 21 to the flow rate of borate buffer flowing from the second flow path 12a to the fluid merge area 21 was 3.56.

  As a result, the pressure loss before and after the fluid mixer 100 'was 0.109 MPa, and the absorbance was 0.063.

  According to the results of Examples 5 to 7 and Comparative Example 3 described above, it is understood that the absorbance in Examples 5 to 7 is smaller than that in Comparative Example 3 when the absorbance under the same pressure loss is compared. As described above, this means that the mixing performance of the fluid mixer used in Examples 5 to 7 is higher than that of the fluid mixer used in Comparative Example 3.

  The present invention is useful for a fluid mixer, a fluid mixing method using the fluid mixer, and a method for producing an emulsion.

DESCRIPTION OF SYMBOLS 100 Fluid mixer 10 Fluid flow path part 11 Small diameter pipe 11a 1st flow path 11b Pipe end part 12 Large diameter pipe 12a 2nd flow path 20 Fluid confluence contraction part 21 Fluid confluence area 22 Fine pore 30 Flow path expansion part 31 Flow Road expansion area

Claims (13)

A small-diameter pipe, and a large-diameter pipe that accommodates the small-diameter pipe in the same length direction. A first flow path is formed inside the small-diameter pipe, and the inside of the large-diameter pipe and the small diameter A fluid flow path portion in which a second flow path is configured outside the pipe;
A fluid merging area is provided on the fluid outflow side of the fluid flow path portion, where the first fluid flowing through the first flow path and the second fluid flowing through the second flow path merge, and the merge A fluid merging and converging part in which pores through which the first and second fluids contracted are perforated,
A flow path expanding portion that is provided on the fluid outflow side of the fluid converging and contracting section and that constitutes a flow path expanding area into which the first and second fluids that have flowed through the pores flow; and
With
The small diameter pipe is a fluid mixer formed such that a pipe end portion on a fluid outflow side becomes thinner as going to the pipe end.   2. The fluid mixer according to claim 1, wherein the small-diameter pipe has a uniform cross-sectional shape of the first flow path along a length direction to a pipe end.   The fluid mixer according to claim 1 or 2, wherein the small-diameter pipe has a tapered outer peripheral portion of a pipe end portion on a fluid outflow side.   3. The fluid mixing according to claim 1, wherein the small-diameter pipe is formed in a curved shape in which a contour along a longitudinal direction in a longitudinal section of an outer peripheral surface of a pipe end portion on a fluid outflow side is bulged outward. vessel.   The large-diameter pipe has a gap formed as a part of the second flow path formed between an inner wall of the pipe and a pipe end portion of the small-diameter pipe formed uniformly in the fluid flow direction. 4. The fluid mixer described in any one of 4 above. A fluid mixing method using the fluid mixer according to any one of claims 1 to 5,
The first fluid that has flowed through the first flow path and the second fluid that has flowed through the second flow path are merged in the fluid merge area, and the first and second fluids merged in the fluid merge area are A fluid mixing method in which a first fluid and a second fluid that have flown through the pores and flowed through the pores are allowed to flow into the flow path expansion region.   The fluid mixing method according to claim 6, wherein the first fluid and the second fluid in the fluid merging region are joined so as to cover the first fluid with the second fluid.   The ratio of the flow rate of the first fluid flowing from the first flow path to the fluid merge area to the flow speed of the second fluid flowing from the second flow path to the fluid merge area is 0.5 to 2. 6. The fluid mixing method described in 6 or 7.   The fluid mixing method according to claim 6, wherein the first and second fluids merged in the fluid merge region are contracted into the pores under laminar flow conditions.   Fluid combined with the first and second fluids when the first and second fluids merge together for the first time in the fluid merging and contracting part The fluid mixing method according to any one of claims 6 to 9, wherein the flow velocity of the same is made the same.   The fluid mixing method according to claim 6, wherein a pressure loss before and after the fluid mixer is set to 0.01 to 5 MPa. A method for producing an emulsion using the fluid mixer according to any one of claims 1 to 5,
Using the fluid that is one of the continuous phase and the dispersed phase as the first fluid and the fluid that is the other as the second fluid,
The fluid that has flowed through the first flow path and the fluid that has flowed through the second flow path are merged in the fluid merge area, the fluid merged in the fluid merge area is contracted into the pores, and A method for producing an emulsion, wherein a fluid in which pores are contracted is allowed to flow into a channel enlargement region.   The method for producing an emulsion according to claim 12, wherein an oil-in-water emulsion is produced by using an aqueous phase that is a continuous phase as the first fluid and an oil phase that is a dispersed phase as the second fluid.

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