Vortex type fluid mixer

Abstract

A vortex-type fluid mixer (11) is provided with: a volute chamber (25) defined by a cylindrical peripheral side wall (13), and a first end wall (15) and a second end wall (17) provided at both ends thereof and facing each other; an inlet flow path (19) that opens in the peripheral side wall (13); an outlet flow path (21) that opens in the first end wall (15); and a merging section (23) that is provided upstream of the inlet flow path (19) and merges the at least two fluid supply paths. The volute chamber (25) is configured such that when the fluid supplied from the at least two fluid supply paths and merged at the merging section (23) flows into the volute chamber (25) via the inlet flow path (19), a vortex is formed, and the fluid that forms the vortex in the volute chamber (25) and is mixed flows out from the outlet flow path (21).

Description

Technical Field

[0001] This invention relates to a vortex fluid mixer, which is used in fluid transport piping in various industries such as chemical plants, semiconductor manufacturing, food, medical, and biological fields, and uses vortices to mix two or more fluids. Background Technology

[0002] As a method for mixing fluids flowing within pipes in various industries such as chemical plants, semiconductor manufacturing, food processing, medical treatment, and biotechnology, a static mixer, as disclosed in Patent Document 1, is generally used, which installs a torsion blade-shaped static mixer element within the pipe. Typically, the static mixer element has a structure where multiple smallest unit components are connected in series, with the smallest unit being a rectangular plate twisted 180 degrees around its length axis. In a typical static mixer, the end of the right element (the end in the direction of the torsion axis), which is shaped like a rectangular plate twisted 180 degrees to the right, and the end of the left element (the end in the direction of the torsion axis), which is shaped like a rectangular plate twisted 180 degrees to the left, are orthogonally joined to each other at multiple points in the direction of fluid flow within the pipe. With this structure, the fluid flowing within the pipe is divided in two each time it passes through an element, and the fluid flows along the torsion surface of the element, thereby being agitated by the action of the flow reversing from the center of the pipe to the pipe wall, resulting in uniform mixing of the fluid in the radial direction of the piping.

[0003] [Existing Technical Documents]

[0004] [Patent Literature]

[0005] Patent Document 1: Japanese Patent Application Publication No. 2001-205062

[0006] Patent Document 2: International Publication No. 2010 / 016448 Summary of the Invention

[0007] [The problem the invention aims to solve]

[0008] In the mixing of fluids using a static mixer, the concentration deviation (uneven concentration distribution) in the radial direction of the piping can be reduced for different types of fluids because the fluid is stirred along the flow path. However, the concentration deviation (uneven concentration distribution) in the flow direction of the piping cannot be reduced for different types of fluids. Methods for reducing the concentration deviation (uneven concentration distribution) in the flow direction of different types of fluids include: setting up a tank midway through the flow path, storing the fluid in the tank, homogenizing the concentration, and then discharging the fluid; or, as described in Patent Document 2, setting up multiple branches in the flow path, allowing different types of fluids to merge again at different locations, and using time differences to mix them and homogenize the concentration. However, setting up tanks or multiple branches requires a large space. Therefore, when space is limited in the apparatus, it is difficult to eliminate the concentration deviation (uneven concentration distribution) in the flow direction by using tanks or time-difference mixing. However, for example, in a semiconductor wafer production line, if a solution with a concentration deviation is applied to semiconductor wafers, it may cause defects.

[0009] Therefore, the purpose of this invention is to solve the problems existing in the prior art and provide a fluid mixer that can save space and reduce the concentration deviation in both the radial and flow directions of the piping.

[0010] [Technical means to solve the problem]

[0011] In view of the aforementioned objective, the present invention provides a vortex fluid mixer comprising: a vortex chamber defined by a cylindrical peripheral wall and a first end wall and a second end wall disposed at both ends of the peripheral wall and facing each other; an inlet flow path extending along the central axis of the inlet flow path and opening in the peripheral wall; an outlet flow path extending along the central axis of the outlet flow path and opening in the first end wall; and a confluence portion disposed upstream of the inlet flow path, such that at least two fluid supply paths merge, wherein the vortex chamber is configured such that when fluids supplied from the at least two fluid supply paths and merging at the confluence portion flow into the vortex chamber via the inlet flow path, a vortex is formed, and the fluids that have formed a vortex and are mixed in the vortex chamber flow out from the outlet flow path.

[0012] In the vortex-type fluid mixer, a vortex chamber is defined by a cylindrical peripheral wall and opposing first and second end walls at its two ends. An inlet flow path opens on the peripheral wall of the vortex chamber, and an outlet flow path opens on the first end wall. When fluids merging at the confluence point upstream of the inlet flow path flow into the vortex chamber through the inlet flow path, a vortex is formed. Therefore, the fluid flowing in from the inlet flow path becomes a swirling flow and vortex-like flow within the vortex chamber before flowing out from the outlet flow path. As a result, even when different types of fluids merge at the confluence point, the stirring effect of the vortex in the vortex chamber reduces concentration deviations (uneven concentration distribution) between the different types of fluids. Furthermore, the inventors of this application discovered that in a vortex fluid mixer with the structure described above, the fluid flowing into the vortex chamber from the inlet flow path depends on the position of the fluid flow in the cross-section of the inlet flow path perpendicular to the flow direction. During the period from flowing into the vortex chamber from the inlet flow path until flowing out from the outlet flow path, the fluid flows along different paths, and the length of the streamlines from flowing into the vortex chamber from the inlet flow path until flowing out from the outlet flow path is different. As a result, fluids at different positions in the flow direction in the inlet flow path (i.e., fluids flowing along different paths with different streamline lengths) are mixed at various points within the vortex chamber and at the inlet of the outlet flow path. Therefore, by utilizing the mixing effect of the time difference, it is possible to reduce the concentration deviation (uneven concentration distribution) of different types of fluids in the flow direction.

[0013] In the vortex fluid mixer, the inlet flow path is preferably configured such that the central axis of the inlet flow path passes away from the central axis of the vortex chamber that connects the center of the first end wall and the center of the second end wall.

[0014] The outlet flow path is preferably configured such that the central axis of the outlet flow path extends through a position away from the central axis of the inlet flow path.

[0015] In addition, the outlet flow path is preferably configured such that the central axis of the outlet flow path extends on the central axis of the vortex chamber.

[0016] In one embodiment, a protrusion may also be included, projecting into the vortex chamber from at least one of the first end wall and the second end wall. In this case, the protrusion may be located off-center from the vortex chamber's central axis, or it may be located off-center from the outlet flow path's central axis.

[0017] Alternatively, in another embodiment, the second end wall may also be composed of a diaphragm. In this case, the diaphragm can be moved by a drive unit to approach or move away from the first end wall.

[0018] The first end wall and the second end wall are circular or elliptical in shape.

[0019] [The effects of the invention]

[0020] This invention generates vortices within a vortex chamber, reducing concentration variations between different fluid types through the stirring effect of these vortices. Furthermore, the fluid flowing into the vortex chamber from the inlet flow path depends on its position within the cross-section of the inlet flow path perpendicular to the flow direction. It flows along different paths from the inlet flow path into the vortex chamber until it exits through the outlet flow path, and the streamline lengths from inlet flow path into the vortex chamber to exit through the outlet flow path also vary. Therefore, fluids at different positions in the flow direction within the inlet flow path are mixed throughout the vortex chamber and at the inlet of the outlet flow path. By utilizing the mixing effect of time differences, the concentration variations between different fluid types in the flow direction can be reduced. Attached Figure Description

[0021] Figure 1 This is a partial cross-sectional perspective view showing the overall structure of the vortex fluid mixer according to the first embodiment of the present invention by cutting a portion to make the interior visible.

[0022] Figure 2 It means along Figure 1 A directional cross-sectional view showing the positions of multiple regions on a section cut along line II-II and viewed in the direction of the arrow.

[0023] Figure 3 It is a schematic representation of crossing Figure 2 The fluid in region H Figure 1 A diagram illustrating the streamlines of the flow within the vortex chamber of a vortex fluid mixer.

[0024] Figure 4 It is a schematic representation of crossing Figure 2 The fluid in region I Figure 1 A diagram illustrating the streamlines of the flow within the vortex chamber of a vortex fluid mixer.

[0025] Figure 5 It is a schematic representation of crossing. Figure 2 The fluid in region F Figure 1 A diagram illustrating the streamlines of the flow within the vortex chamber of a vortex fluid mixer.

[0026] Figure 6 This is a schematic diagram of a vortex fluid mixer according to a second embodiment of the present invention, viewed from the side.

[0027] Figure 7 This is a schematic diagram showing the interior of a vortex fluid mixer according to a third embodiment of the present invention from the side.

[0028] Figure 8This is a schematic diagram showing the interior of a vortex fluid mixer according to a fourth embodiment of the present invention from the side.

[0029] Figure 9 This is an explanatory diagram showing the structure and dimensions of a vortex fluid mixer used in numerical simulation.

[0030] Figure 10 This is an explanatory diagram showing the structure and dimensions of a vortex fluid mixer used in numerical simulation.

[0031] Figure 11 It is a graph showing the time variation of the maximum and minimum values ​​of the passive scalar of the mixed fluid obtained at the reference position of the inlet flow path in the numerical simulation of using a vortex fluid mixer.

[0032] Figure 12 This is a graph showing the time variation of the maximum and minimum values ​​of the passive scalar of the mixed fluid at the reference position of the outlet flow path in each region during numerical simulation using a vortex fluid mixer.

[0033] Figure 13 In numerical simulations using a vortex fluid mixer, the flow through... Figure 2 The diagram shows a comparison of the streamline lengths of the fluid flowing within the vortex chamber at the reference position of the inlet flow path.

[0034] Figure 14 It is a graph showing the time-varying average value of the passive scalar of the fluid passing through a reference position of the outlet flow path as the fluid with passive scalar values ​​of 1 and 0 alternately flows in from the inlet flow path using a numerical simulation of a vortex fluid mixer.

[0035] Figure 15 It is a graph showing the time-varying average value of the passive scalar of the fluid passing through a reference position of the inlet flow path as the fluid with passive scalar values ​​of 1 and 0 alternately flows in from the outlet flow path in a numerical simulation using a vortex fluid mixer. Detailed Implementation

[0036] Hereinafter, embodiments of the vortex fluid mixer according to the present invention will be described with reference to the accompanying drawings. First, referring to... Figure 1 The overall structure of the vortex fluid mixer 11 of the first embodiment will be described.

[0037] The vortex fluid mixer 11 includes: a cylindrical peripheral wall 13 extending along a central axis; a first end wall 15 and a second end wall 17 disposed at opposite ends of the peripheral wall 13 along the central axis; an inlet flow path 19; an outlet flow path 21; and a confluence portion 23 disposed upstream of the inlet flow path 19. The first end wall 15 and the second end wall 17 have the same shape and are configured to block the two ends of the peripheral wall 13 along the central axis. The space surrounded by the peripheral wall 13, the first end wall 15, and the second end wall 17 constitutes a vortex chamber 25. The central axis O of the vortex chamber, which extends in a manner connecting the center of the first end wall 15 and the center of the second end wall 17, coincides with the central axis of the peripheral wall 13. Furthermore, in this specification, the center of the first end wall 15 and the center of the second end wall 17 refer to the centroid positions of the first end wall 15 and the second end wall 17, respectively. In the illustrated embodiment, the first end wall 15 and the second end wall 17 are circular, and the peripheral wall 13 is cylindrical. However, the shapes of the first end wall 15 and the second end wall 17 are not limited to circular shapes. As long as vortices can be generated in the vortex chamber 25, they can be set to any shape such as an elliptical shape, a triangular shape, or a quadrilateral shape, or a polygonal shape.

[0038] The inlet flow path 19 extends along an inlet flow path central axis P1 perpendicular to the central axis O of the vortex chamber and opens at the peripheral sidewall 13. The inlet flow path central axis P1 extends through the center of the cross-section of the inlet flow path 19. Similarly, the outlet flow path 21 extends outward from the vortex chamber 25 along an outlet flow path central axis P2 parallel to the central axis O of the vortex chamber and opens at the first endwall 15 of the vortex chamber 25. The outlet flow path central axis P2 extends through the center of the cross-section of the outlet flow path 21. In the illustrated embodiment, both the inlet flow path 19 and the outlet flow path 21 comprise circular tubes with a circular cross-section. However, the cross-sections of the inlet flow path 19 and the outlet flow path 21 are not limited to a circular shape and can also be polygonal shapes such as elliptical or quadrilateral shapes. Furthermore, in the illustrated embodiment, the inlet flow path 19 comprises a straight circular tube, but it can also be other shapes such as a nozzle shape, as long as fluid can flow into the vortex chamber 25.

[0039] The inlet flow path 19 is configured such that the central axis P1 of the inlet flow path passes through an eccentric position away from the central axis O of the vortex chamber. Therefore, the fluid flowing in from the inlet flow path 19 encounters the peripheral wall 13 within the vortex chamber 25 and flows along the peripheral wall 13, generating a swirling flow, becoming a vortex, and flowing out from the outlet flow path 21. To facilitate the generation of the swirling flow, the inlet flow path 19 is preferably configured such that the fluid flowing into the vortex chamber 25 from the inlet flow path 19 flows along the peripheral wall 13. On the other hand, as long as the fluid flowing into the vortex chamber 25 from the inlet flow path 19 flows out from the outlet flow path 21 after generating a vortex, the outlet flow path 21 can be located at any position on the first end wall 15. That is, the outlet flow path 21 only needs to be configured such that the central axis P2 of the outlet flow path extends through a position away from the central axis P1 of the inlet flow path, to prevent the fluid flowing into the vortex chamber 25 from the inlet flow path 19 from directly flowing out from the outlet flow path 21.

[0040] In the illustrated embodiment, the inlet flow path 19 extends tangentially to the cylindrical peripheral wall 13, with the central axis P1 of the inlet flow path parallel to the tangent. Fluid flows from the inlet flow path 19 substantially tangentially relative to the peripheral wall 13 into the vortex chamber 25. Furthermore, the outlet flow path 21 opens into the first end wall 15, and its central axis P2 passes through the center of the first end wall 15, meaning the central axis P2 of the outlet flow path extends in a straight line with the central axis O of the vortex chamber. With this structure, the fluid flowing in from the inlet flow path 19 generates a swirling flow within the vortex chamber 25 along the peripheral wall 13, and gradually approaches the center while flowing in a vortex shape towards the outlet flow path 21.

[0041] The confluence section 23 is configured to allow different types of fluids supplied from at least two fluid supply paths connected to different fluid supply sources to merge and flow into the vortex chamber 25 via the inlet flow path 19. In the illustrated first embodiment, the confluence section 23 includes a T-shaped flow path where one end of a straight main flow path 23a is connected to the inlet flow path 19, and one end of a secondary flow path 23b is connected midway thereto. Fluid A is supplied from the other end of the main flow path 23a and fluid B is supplied from the other end of the secondary flow path 23b, and fluid A and fluid B are merged at the confluence section 23. The shape of the confluence section 23 is not limited to a T-shape; for example, it can also be a Y-shape. In addition, two or more secondary flow paths 23b can be connected to the main flow path 23a, and three or more types of fluids can be merged at the confluence section 23. The main flow path 23a or the secondary flow path 23b constituting the confluence section 23 is preferably a straight circular pipe with a circular cross-section, but it is not limited to a circular pipe and can be a pipe with a cross-section of any shape. In addition, the pipe diameter (inner diameter) of the main flow path 23a and the secondary flow path 23b is preferably equal, but the pipe diameter (inner diameter) of the secondary flow path 23b may also be smaller than the pipe diameter (inner diameter) of the main flow path 23a.

[0042] In the vortex-type fluid mixer 11, different types of fluids converging at the confluence section 23 flow into the vortex chamber 25 via the inlet flow path 19. Furthermore, the central axis P1 of the inlet flow path passes through an eccentric position away from the central axis O of the vortex chamber, and the central axis P2 of the outlet flow path extends through a position away from the central axis P1 of the inlet flow path. Therefore, within the vortex chamber 25, the fluid flowing in from the inlet flow path 19 contacts the peripheral wall 13 and flows along the peripheral wall 13, generating a swirling flow, becoming a vortex, and flowing out from the outlet flow path 21. That is, the confluence of different types of fluids flowing in from the inlet flow path 19 forms a vortex within the vortex chamber 25. Therefore, the confluence of fluids flowing in from the inlet flow path 19, through the stirring effect of the vortex, can reduce the concentration deviation (uneven concentration distribution) of the different types of fluids, thereby reducing the radial concentration deviation (uneven concentration distribution) of the different types of fluids in the inlet flow path 19.

[0043] Furthermore, the inventors have discovered that in the structure where the fluid flowing in from the inlet flow path 19 becomes a swirling flow and generates vortices in the vortex chamber 25 as described above, and then flows out from the outlet flow path 21, the fluid flowing in from the inlet flow path 19 depends on the radial position of the fluid flow in the cross section of the inlet flow path 19 perpendicular to the flow direction, i.e., the central axis P1 of the inlet flow path. The path of the swirling flow that travels during the period from flowing into the vortex chamber 25 from the inlet flow path 19 until flowing out from the outlet flow path 21 is different, and the length of the streamline from flowing into the inlet flow path 19 until flowing out from the outlet flow path 21 is different.

[0044] Figure 2 Indicates will follow Figure 1 The inlet flow path 19, cut along line II-II and perpendicular to the central axis P1 of the inlet flow path, is divided into nine regions, from region A to region I. The positions of regions A to region I are observed when the cross-section is viewed in the direction of the arrow. Figures 3 to 5 These represent streamlines obtained by numerically reproducing the fluid flow in regions H, I, and F, respectively. The fluid in region H flows along... Figure 3 As shown, the streamlines flow from the inlet flow path 19 through the vortex chamber 25 into the outlet flow path 21. Therefore, the streamlines of the vortex within the vortex chamber 25 are short and will not remain in the vortex chamber 25 for too long before flowing out through the outlet flow path 21. The fluid in region I flows along... Figure 4 As shown, the streamlines flow from the inlet flow path 19 through the vortex chamber 25 into the outlet flow path 21. Therefore, it can be known that the length of the vortex in the vortex chamber 25 is greater than that of the vortex in the outlet flow path 21. Figure 3 The streamline shown is slightly longer, resulting in a slightly longer residence time within the vortex chamber 25 compared to the fluid flowing in region H, and exiting from the outlet flow path 21. The fluid in region F flows along... Figure 5As shown, the streamlines flow from the inlet flow path 19 through the vortex chamber 25 into the outlet flow path 21. Therefore, it can be known that the length of the vortex in the vortex chamber 25 is greater than that of the vortex in the outlet flow path 21. Figure 4 The streamline shown is longer, and the fluid stays in the vortex chamber 25 for a longer time compared to the fluid flowing in region I, and flows out from the outlet flow path 21.

[0045] Thus, depending on the location of the fluid flow region in the cross-section of the inlet flow path 19, the path and streamline length of the fluid traveling in the vortex chamber 25 are different. Therefore, the fluid in different regions of the inlet flow path 19 travels along different paths, merging and mixing at various points in the vortex chamber 25 and at the inlet to the outlet flow path 21. The mixing of fluids of different streamline lengths traveling along different paths results in the mixing of fluids at different positions in the flow direction of the inlet flow path 19. Therefore, a mixing effect utilizing time difference is achieved, thereby reducing concentration deviation (uneven concentration distribution) in the flow direction of different types of fluids. Furthermore, as... Figures 3 to 5 As shown, the fluid flowing out of the vortex chamber 25 also flows in the outlet flow path 21 while generating a swirling flow. Therefore, it can be seen that the mixing effect brought about by the swirling flow is also obtained.

[0046] Thus, the vortex fluid mixer 11 according to the present invention does not require the installation of tanks or branch lines, and can reduce the concentration deviation (uneven concentration distribution) of the fluids merging in the confluence section 23 in both the radial and flow directions, thereby achieving the effect of obtaining a more uniform concentration of the mixed fluid.

[0047] Furthermore, the vortex fluid mixer according to the present invention can reduce concentration deviation (uneven concentration distribution) simply by generating a swirling flow within the vortex chamber 25. Therefore, the vortex fluid mixer is not limited to... Figure 1 The structure of the embodiment shown in the figure.

[0048] For example, it can also be like Figure 6 As shown in the vortex fluid mixer 51 according to the second embodiment, the second end wall is formed by a diaphragm 17'. In the second embodiment, the diaphragm 17' can be driven by a drive unit (not shown) to move it closer to or away from the first end wall 15, thereby increasing / decreasing the volume of the vortex chamber 25 to adjust the flow rate of the fluid within the vortex chamber 25. The drive unit can be driven by various methods such as manual, air-driven, or electric. By adjusting the flow rate of the fluid within the vortex chamber 25, appropriate mixing with less concentration unevenness can be achieved according to the type of fluid being mixed.

[0049] Alternatively, a protrusion protruding into the vortex chamber 25 may be provided on the first end wall 15 or the second end wall 17 of the vortex fluid mixer. Figure 7This refers to a vortex fluid mixer 61 according to a third embodiment, which has a protrusion 63 provided on the first end wall 15. Figure 8 This illustrates a vortex-type fluid mixer 71 according to the fourth embodiment, where a protrusion 63 is provided on the second end wall 17. The protrusion 63 is not limited in location as long as it is configured to obstruct the vortex flow in the vortex chamber 25. However, the protrusion 63 is preferably configured such that at least a portion of it overlaps with the extension of the inlet flow path 19 into the vortex chamber 25, so that the swirling flow of fluid flowing from the inlet flow path 19 into the vortex chamber 25 collides with the protrusion 63 more quickly. Furthermore, the protrusion 63 is cylindrical in shape, and its cross-section can be of any shape. For example, the cross-section of the protrusion 63 can be circular, elliptical, quadrilateral, triangular, rhomboid, or other polygonal or plate-like shapes. In the illustrated embodiment, the protrusion 63 is a cylindrical shape with a circular cross-section. With this protrusion 63 provided in the vortex chamber 25, the fluid flows along the circumference of the protrusion 63. Therefore, compared with the case without the protrusion 63, the length of the streamline of the fluid flowing from the inlet flow path 19 into the vortex chamber 25 until it flows out from the outlet flow path 21 can be extended, thereby further improving the stirring effect brought about by the vortex (swirling flow).

[0050] In addition, Figures 6 to 8 In the vortex fluid mixer 51 according to the second embodiment, the vortex fluid mixer 61 according to the third embodiment, and the vortex fluid mixer 71 according to the fourth embodiment shown, the mixture is used with... Figure 1 The common components of the vortex fluid mixer 11 of the first embodiment shown are marked with the same reference numerals. Furthermore, the components marked with the same reference numerals have the same structure. Therefore, the description of the common components with respect to the vortex fluid mixer 11 of the first embodiment is omitted here.

[0051] [Example]

[0052] The following is about the use of and Figure 1 The analysis results obtained from numerical simulation of a vortex fluid mixer with the same structure as the vortex fluid mixer 11 shown in the first embodiment will be explained. In the following description, for ease of understanding, the structural designations of the vortex fluid mixer used in the numerical simulation will be the same as those of the vortex fluid mixer 11.

[0053] Unless otherwise specified, numerical simulation is performed using devices such as... Figure 9 and Figure 10The vortex fluid mixer 11 with the structure and dimensions shown is used. Specifically, the vortex chamber 25 has a cylindrical shape with a diameter of 20 mm and a height of 4 mm. An inlet flow path 19 with a diameter of 4 mm is connected to the peripheral wall 13 such that its central axis P1 passes through a position 7.5 mm away from the center of the vortex chamber 25. Furthermore, the main flow path 23a of the confluence section 23, with a diameter of 4 mm, is connected to the extension of the inlet flow path 19 in a straight line. The right end of the main flow path 23a in the figure extends 30 mm away from the center of the vortex chamber 25 and perpendicular to the central axis P1 of the inlet flow path. A secondary flow path 23b with a diameter of 4 mm and a length of 15 mm is connected to the main flow path 23a such that its central axis extends 20 mm away from the center of the vortex chamber 25 and perpendicular to the central axis P1 of the inlet flow path. Furthermore, a cylindrical outlet flow path 21 with a diameter of 4 mm and a length of 15 mm is connected to the first end wall 15 in such a way that it extends along the outlet flow path central axis P2, which is aligned with the central axis O of the vortex chamber. That is, the outlet flow path 21 extends from the first end wall 15 along the outlet flow path central axis P2, which passes through the center of the first end wall 15 and is perpendicular to the first end wall 15.

[0054] First, numerical simulation was used to confirm the concentration deviation (uneven concentration distribution) of the fluid caused by the radial positions in the inlet flow path 19 and the outlet flow path 21. In the numerical simulation, blue water was supplied to the main flow path 23a of the confluence section 23 at a rate of 500 mL / min, and red water was supplied to the secondary flow path 23b at a rate of 500 mL / min, causing them to merge at the confluence section 23. At the reference positions immediately before the vortex chamber 25 in the inlet flow path 19 and immediately after the vortex chamber 25 in the outlet flow path 21, the mixing method of blue and red water was evaluated using a passive scalar as an indicator. The passive scalar is a color-dependent indicator of the mixed fluid, where red is considered as 1 (red water concentration is 100%) and blue is considered as 0 (red water concentration is 0%). The passive scalar of the fluid in the inlet flow path 19 is determined at a reference position 15 mm away from the center of the vortex chamber 25 and perpendicular to the central axis P1 of the inlet flow path. The passive scalar of the fluid in the outlet flow path 21 is determined at a reference position 15 mm away from the first end wall 15 of the vortex chamber 25.

[0055] Figure 11 This is a graph showing the time-dependent change of a passive scalar quantity of the fluid in inlet flow path 19. Figure 12 This is a graph showing the time-dependent change of a passive scalar quantity of the fluid in outlet flow path 21. Additionally, in Figure 11 and Figure 12In the diagram, the cross-sections at the reference positions of the inlet flow path 19 and the outlet flow path 21 are divided into multiple regions. The passive scalar quantity of the fluid in each region is calculated. The solid line represents the time-dependent variation of the maximum value of the passive scalar quantity of the fluid in each region, and the dashed line represents the time-dependent variation of the minimum value. According to Figure 11 It can be seen that in the inlet flow path 19, according to the region of the profile, the difference in the passive scalar of the fluid is large, that is, the radial concentration distribution is uneven, and the mixing is insufficient. On the other hand, according to Figure 12 It can be seen that in the outlet flow path 21, there is almost no difference in the passive scalar quantity of the fluid caused by the region of the cross section, that is, there is almost no unevenness in the radial concentration distribution of the fluid, and the mixing is thorough. Therefore, it is confirmed that by using the vortex fluid mixer 11, the concentration deviation (uneven concentration distribution) caused by the radial position of different types of fluids is reduced, thereby achieving the effect of eliminating radial concentration deviation (uneven concentration distribution), that is, the effect of homogenizing the radial concentration.

[0056] Next, numerical simulation was used to confirm the effect of reducing the concentration deviation (uneven concentration distribution) of the fluid in the flow direction in the inlet flow path 19 obtained by using the vortex fluid mixer 11.

[0057] Figure 13 Indicates use Figure 9 and Figure 10 The results of a numerical simulation of the vortex fluid mixer 11 of the dimensions shown are performed under the same conditions as the numerical simulation used to confirm the concentration deviation (uneven concentration distribution) of the fluid caused by the radial position in the inlet flow path 19 and the outlet flow path 21. Figure 13 The cross-section at the reference position of the inlet flow path 19 (located 15 mm from the line passing through the center of the vortex chamber 25 and perpendicular to the central axis P1 of the inlet flow path) is shown as follows. Figure 2 This is a chart comparing the lengths of the streamlines traveled by the fluid in each region through the vortex chamber 25 until it exits from the outlet flow path 21 when the area is divided into nine regions from region A to region I as shown. Figure 13 It can be seen that the streamline lengths of the fluid from region A to region I are different, especially the streamline lengths of the fluid in regions A, B, G, and H are significantly different from those in regions C, D, E, F, and I. Therefore, it can be seen that by using the vortex fluid mixer 11, fluids with streamlines of different lengths are mixed at various points in the vortex chamber 25 and at the inlet of the flow path 21 from the vortex chamber 25, thereby reducing the concentration deviation (uneven concentration distribution) of the fluid in the flow direction in the inlet flow path 19.

[0058] Figure 14 and Figure 15 It means that it is in use Figure 9 and Figure 10 In the numerical simulation of the vortex fluid mixer 11 with the shown structure, a graph showing the time-varying passive scalar (concentration index) of the fluid obtained in the other of the inlet flow path 19 and outlet flow path 21 is displayed when blue water and red water are alternately supplied to one of the inlet flow path 19 and outlet flow path 21. However, the method used to obtain... Figure 14 and Figure 15 The vortex fluid mixer 11 used in the numerical simulation Figure 9 and Figure 10 The vortex fluid mixer 11 shown differs in structure and size in that the inlet flow path 19 is a circular tube with a diameter of 4 mm and a length of 15 mm, omitting the confluence section 23, and the outlet flow path 21 is a circular tube with a diameter of 3 mm and a length of 10 mm, but is otherwise common.

[0059] In the numerical simulation, a reference position 15 mm away from the center of the vortex chamber 25 and perpendicular to the central axis P1 of the inlet flow path is defined as the reference position of the inlet flow path 19, and a position 10 mm away from the first end wall 15 of the vortex chamber 25 is defined as the reference position of the outlet flow path 21. For one of the reference positions of the inlet flow path 19 and the outlet flow path 21, the passive scalar of the fluid is alternately and repeatedly supplied with red water at 500 mL / min for 1 second (passive scalar of 1 (concentration of red water is 100%)) and then supplied with blue water at 500 mL / min for 1 second (passive scalar of 0 (concentration of red water is 0%)). The passive scalar value of the fluid at the other of the reference positions of the inlet flow path 19 and the outlet flow path 21 is then determined. Figure 14 This is a graph showing the time-dependent change of the passive scalar quantity of the fluid at the reference position of the outlet flow path 21 when blue and red water are alternately supplied to the reference position of the inlet flow path 19. Figure 15 This is a graph showing the time-dependent change of the passive scalar quantity of the fluid at the reference position of the inlet flow path 19 when blue and red water are alternately supplied to the reference position of the outlet flow path 21 for comparison. Furthermore, the value of the passive scalar quantity of the fluid at the reference position is set as the average value obtained by averaging the values ​​of the passive scalar quantity of the fluid in each region of the cross-section at the reference position.

[0060] right Figure 14 and Figure 15 A comparison shows that, in Figure 14 In, the amplitude ratio of passive scalars Figure 15 The situation is small. Under the condition of alternately supplying fluid with passive scalar values ​​of 0 and 1, a smaller amplitude of the passive scalar value means a reduction in concentration deviation (uneven concentration distribution) in the flow direction. Additionally, as... Figure 14As in the numerical simulation, when fluid is supplied from the inlet flow path 19 and flows out from the outlet flow path 21, a swirling flow is generated in the vortex chamber 25, resulting in a stirring effect caused by the vortex. On the other hand, as... Figure 15 Under the conditions of the numerical simulation, when fluid is supplied from the outlet flow path 21 and flows out from the inlet flow path 19, it is difficult to generate a swirling flow in the vortex chamber 25, and the stirring effect brought about by the vortex cannot be obtained. Therefore, according to Figure 14 and Figure 15 By comparison, it can be confirmed that as long as the vortex fluid mixer 11 is used to supply the confluence fluid from the inlet flow path 19, and the fluid flows out from the outlet flow path 21 through the vortex chamber 25, the effect of the vortex can reduce the concentration deviation (uneven concentration distribution) of the confluence fluid in the flow direction.

[0061] The vortex fluid mixers 11, 51, 61, and 71 according to the present invention have been described above with reference to the illustrated embodiments, but the present invention is not limited to the illustrated embodiments. For example, in the illustrated embodiment, a cylindrical vortex chamber 25 is used, but as long as vortices can be generated within the vortex chamber 25, an elliptical or polygonal cylindrical vortex chamber can also be used. Furthermore, in the illustrated embodiment, a secondary flow path 23b is connected to the main flow path 23a in the confluence section 23 to allow two fluids to merge, but two or more secondary flow paths 23b can also be connected to the main flow path 23a in the confluence section 23 to allow three or more fluids to merge.

[0062] Explanation of icon numbers

[0063] 11: Vortex Fluid Mixer

[0064] 13: Peripheral sidewall

[0065] 15: First end wall

[0066] 17: Second end wall

[0067] 17': Diaphragm

[0068] 19: Inlet Flow Path

[0069] 21: Exit flow path

[0070] 23: Convergence Department

[0071] 25: Vortex chamber

[0072] 51: Vortex fluid mixer

[0073] 61: Vortex fluid mixer

[0074] 63: Protrusion

[0075] 71: Vortex Fluid Mixer

Claims

1. A vortex fluid mixer, characterized in that... include: The vortex is defined by a cylindrical peripheral wall and a first end wall and a second end wall disposed at both ends of the peripheral wall and facing each other. An inlet flow path extends along the central axis of the inlet flow path and opens in the peripheral sidewall; An outlet flow path extends along the central axis of the outlet flow path and opens in the first end wall; as well as A confluence section is located upstream of the inlet flow path, allowing at least two fluid supply paths to merge. The vortex chamber is configured such that when fluids supplied from the at least two fluid supply paths and merged at the confluence point flow into the vortex chamber via the inlet flow path, a vortex is formed, and the fluids that form vortices and mix in the vortex chamber flow out from the outlet flow path.

2. The vortex fluid mixer according to claim 1, wherein, The inlet flow path is configured such that the central axis of the inlet flow path passes away from the central axis of the vortex chamber that connects the center of the first end wall and the center of the second end wall.

3. The vortex fluid mixer according to claim 2, wherein, The outlet flow path is configured such that the central axis of the outlet flow path extends through a location away from the central axis of the inlet flow path.

4. The vortex fluid mixer according to claim 2, wherein, The outlet flow path is configured such that the central axis of the outlet flow path extends along the central axis of the vortex chamber.

5. The vortex fluid mixer according to claim 2, further comprising a protrusion extending into the vortex chamber from at least one of the first end wall and the second end wall.

6. The vortex fluid mixer according to claim 5, wherein, The protrusion is positioned off-center from the central axis of the vortex chamber.

7. The vortex fluid mixer according to claim 5, wherein, The protrusion is positioned off-center from the center axis of the outlet flow path.

8. The vortex fluid mixer according to claim 1, wherein, The second end wall is composed of a diaphragm.

9. The vortex fluid mixer according to claim 8, wherein, The diaphragm moves via a drive unit to approach or move away from the first end wall.

10. The vortex fluid mixer according to any one of claims 1 to 9, wherein, The first end wall and the second end wall are circular or elliptical in shape.

Images