CN216703990U

CN216703990U - Vortex type liquid raw material online static mixer

Info

Publication number: CN216703990U
Application number: CN202220148556.5U
Authority: CN
Inventors: 尼克·迈尔斯; 李国祯; 王筝; 菲利普·赫尔
Original assignee: University of Nottingham Ningbo China
Current assignee: University of Nottingham Ningbo China
Priority date: 2022-01-19
Filing date: 2022-01-19
Publication date: 2022-06-10
Anticipated expiration: 2032-01-19

Abstract

Disclosed is a vortex type liquid raw material online static mixer, wherein, a pipe body extends along the central axis of the pipe body; the first raw material inlet is arranged at the top end of the pipe body and is collinear with the central axis; the second raw material inlet is arranged on the side wall of the tube body and is vertical to the central axis; the first vortex flow pipe is arranged in the pipe body and communicated with the first raw material inlet; the second vortex flow pipe is arranged in the pipe body and communicated with the first vortex flow pipe and the second raw material inlet; the third vortex flow pipe is arranged in the pipe body and communicated with the second vortex flow pipe; the discharge port is arranged at the bottom end of the pipe body and communicated with the third vortex flow pipe; the first transition section is located at the upper end of the inner pipe wall, the first transition section has a first length and a first cross section in the longitudinal direction of the vortex pipe, the first cross section is smoothly changed into a blade shape from a circle with a radius R while the first transition section is twisted by a first predetermined angle in the longitudinal direction, and the vortex flow section is connected with the first transition section.

Description

Vortex type liquid raw material online static mixer

Technical Field

The utility model relates to the field of liquid raw material mixing, in particular to an online static mixer for vortex liquid raw materials.

Background

The mixing operation is a pretreatment procedure in a plurality of technical processes such as industrial production, food processing raw material mixing and the like, and the quality of the mixing effect directly influences the production efficiency and the product quality. In liquid-liquid mixing applications, mixing devices can be classified into dynamic mixers and static mixers, depending on whether there are moving elements or not. The static mixer has no external driving device, and impacts the internal static element by the energy flow of the fluid to increase the velocity gradient and the turbulent kinetic energy of the fluid so as to perform cutting and mixing actions on the raw materials. The dynamic mixer can generate extremely strong shearing and flow dividing capacity and good mixing performance by means of the power element inside the dynamic mixer. Despite the difference of unpowered components, the mixing principle of static and dynamic mixers is to achieve good dispersion and thorough mixing of fluids by creating a separation and vortex phenomenon of the fluids. In the fields of petrochemical industry, food processing and the like, mixers mostly work under a closed condition, at the moment, a mixing device is not suitable to be provided with an external driving device, and a static mixer without a moving element has certain advantages. The static mixer belongs to a pipeline type device, generally does not occupy larger space, has simpler internal structure, and generally has lower energy consumption and maintenance requirement. At present common SK type, the inside unit that produces the vortex of SV type static mixer is that the left and right torsional spiral piece group weld face of haplopore way becomes, and the structure is comparatively complicated, and the pressure loss of production is great, and inside after inlaying this spiral piece, has brought the difficulty for the washing and the maintenance of equipment, and has the risk of jam. Aiming at the technical problem, the patent provides an online pipeline mixer which is lower in energy consumption, has a self-cleaning function and is easy to maintain.

The above information disclosed in this background section is only for enhancement of understanding of the background of the utility model and therefore it may contain information that does not form the prior art that is well known to those of ordinary skill in the art.

SUMMERY OF THE UTILITY MODEL

In order to solve the problems, the utility model provides an online static mixer for vortex liquid raw materials, which realizes the online sufficient mixing effect of the raw materials under the condition of continuously adding materials in the processes of conveying, processing, filling and the like of two or more raw materials. The added liquid raw materials are uniformly mixed, the product quality is ensured, and the energy consumption and the equipment maintenance cost are reduced.

The purpose of the utility model is realized by the following technical scheme.

An online static mixer for vortex liquid raw materials comprises,

a tube extending along a central axis thereof;

a first feedstock inlet disposed at a top end of the tube body and collinear with the central axis;

the second raw material inlet is arranged on the pipe body;

the first vortex flow pipe is arranged in the pipe body and communicated with the first raw material inlet;

the second vortex flow pipe is arranged in the pipe body and is communicated with the first vortex flow pipe and the second raw material inlet;

the third vortex flow pipe is arranged in the pipe body and communicated with the second vortex flow pipe;

the discharge hole is formed in the bottom end of the pipe body and communicated with the third vortex flow pipe; wherein the first vortex flow pipe, the second vortex flow pipe and the third vortex flow pipe comprise inner pipe walls positioned in the pipe body, the inner pipe walls comprise,

a first transition section located at an upper end of the inner pipe wall, the first transition section having a first length in a longitudinal direction of the vortex tube and a first cross section smoothly transitioning from a circular shape having a radius R to a vane shape including a square having a side length of 2R and a semicircle having a radius R extending on each side of the square while the first transition section is twisted by a first predetermined angle in the longitudinal direction;

a swirl flow section connecting the first transition section, the swirl flow section having a second length in a longitudinal direction of the swirl flow tube and a second cross section that twists by a second predetermined angle in the longitudinal direction as the swirl flow section twists;

a second transition section connecting the swirling flow section and located at a lower end of the inner tube wall, the second transition section having a third length and a third cross section in the longitudinal direction of the swirling flow tube, the third cross section smoothly transitioning from the vane shape to a circle of radius R while the second transition section twists in the longitudinal direction by a third predetermined angle.

In the vortex type online static mixer for liquid raw materials, the second raw material inlet comprises 2 inlet pipes which are arranged on the opposite wall of the pipe body and are vertical to the central axis, and the 2 inlet pipes are not on the same horizontal plane.

In the online static mixer for the vortex type liquid raw materials, the rotating direction of the first vortex tube is opposite to that of the second vortex tube, and the rotating direction of the third vortex tube is opposite to that of the second vortex tube.

In the vortex type liquid raw material online static mixer, the second raw material inlet is arranged at the top end of the pipe body and is not communicated with the first vortex flow pipe.

In the vortex type liquid raw material online static mixer, a pipe body between the first vortex flow pipe and the second vortex flow pipe is a premixing area, the length of the pipe body is 1-120 times of the pipe diameter of the first vortex flow pipe, and a pipe body between the third vortex flow pipe and the second vortex flow pipe is a straight pipe, and the length of the pipe body is 1-120 times of the pipe diameter of the second vortex flow pipe.

In the online static mixer for the vortex type liquid raw materials, at least one vortex flow tube with opposite rotation directions in sequence is arranged between the discharge port and the third vortex flow tube.

In the vortex type liquid raw material online static mixer, the blade shape is 2 blade shape, 3 blade shape, 4 blade shape, 5 blade shape or 6 blade shape.

In the online static mixer for the vortex type liquid raw materials, the first preset angle is 90 degrees, the second preset angle is 180 degrees, and the third preset angle is 80 degrees.

In the vortex type liquid raw material online static mixer, the first cross section torsion angle is gradually changed based on an alpha transition curve, wherein,

l is a first length, x is a position coordinate of the first cross section in the length direction, t and k are two power law variable coefficients of alpha transition curve gradual change, and the shape of the gradual change curve can be adjusted. Preferably 0.8 < t < 1.2, 0.4 < k < 0.8, the vortex generation efficiency is optimal.

In the vortex type liquid raw material online static mixer, the first cross section torsion angle and/or the third cross section torsion angle gradually change based on a Vitossby curve or a cosine function.

Compared with the prior art, the utility model has the beneficial effects that:

the utility model has no resistance parts such as embedded fins, spiral sheets and the like, and has very low pressure drop and energy consumption, minimum energy consumption and very high mass transfer efficiency. The self-cleaning function is realized, the maintenance cost is reduced, the process is continuous, and the mixing process is not interrupted; the mixing distance and the installation space are very small, and the mixer is a part of the pipeline and can be regarded as a special pipeline, so that the defects of a traditional stirring tank and the like are avoided; no moving parts, no abrasion and almost no maintenance cost; the device can not be blocked, and the installation mode and the material can be any shape, any size and any material; forced mixing of the entire process stream can greatly reduce the sump volume, or even eliminate the sump.

The above description is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clearly apparent, and to make the implementation of the content of the description possible for those skilled in the art, and to make the above and other objects, features and advantages of the present invention more obvious, the following description is given by way of example of the specific embodiments of the present invention.

Drawings

Various other advantages and benefits of the present invention will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the utility model. It is obvious that the drawings described below are only some embodiments of the utility model, and that for a person skilled in the art, other drawings can be derived from them without inventive effort. Also, like parts are designated by like reference numerals throughout the drawings.

In the drawings:

FIG. 1 is a schematic structural view of a vortex liquid feed in-line static mixer of the present invention;

FIG. 2 is a schematic diagram of the arrangement of the second feed inlet of the swirling liquid feed in-line static mixer of the present invention;

FIG. 3 is a schematic diagram of the two streams of liquid forming a swirling flow of a swirling liquid feed in-line static mixer of the present invention at the second feed inlet;

FIG. 4 is a plot of the volumetric content of the feedstock and the trajectory of the liquid feedstock in one embodiment of the in-line static mixer of the present invention for a swirling liquid feedstock;

FIG. 5 is a schematic of the feed non-uniformity coefficient for one embodiment of the vortex liquid feed in-line static mixer of the present invention;

FIG. 6 is a schematic diagram of a three-blade configuration of an embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 7 is a schematic diagram of a four-bladed configuration of one embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 8 is a schematic diagram of a five-bladed configuration of one embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 9 is a schematic diagram of the construction of the vortex tube of one embodiment of the in-line static mixer for a swirling liquid feed of the present invention;

FIG. 10 is a schematic cross-sectional view of the inner wall of a vortex liquid feed at a transition stage location in the transition zone of an embodiment of the in-line static mixer of the present invention;

FIG. 11 is a schematic view of a different gradual transition mode of an embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 12 is a schematic diagram of the placement of the second feed inlet of one embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 13 is a plot of the volumetric content of the feedstock for one embodiment of the in-line static mixer of the present invention for a swirling liquid feedstock;

FIG. 14 is a schematic of the feed non-uniformity coefficient for one embodiment of the vortex liquid feed in-line static mixer of the present invention;

FIG. 15 is a schematic diagram of the placement of the second feed inlet of one embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 16 is a schematic diagram of the placement of the second feed inlet of one embodiment of the swirling liquid feed in-line static mixer of the present invention;

FIG. 17 is a plot of the feedstock volume content distribution and liquid feedstock flow trajectory for an embodiment of the vortex liquid feedstock in-line static mixer of the present invention;

FIG. 18 is a schematic of the feed non-uniformity coefficient for one embodiment of the vortex liquid feed in-line static mixer of the present invention;

FIG. 19 is a schematic of the feed non-uniformity coefficient for one embodiment of the vortex liquid feed in-line static mixer of the present invention;

FIG. 20 is a plot of the volumetric content of the feedstock and the trajectory of the liquid feedstock in one embodiment of the in-line static mixer of the present invention for a swirling liquid feedstock;

FIG. 21 is a schematic of the feed non-uniformity coefficient for one embodiment of the vortex liquid feed in-line static mixer of the present invention;

FIG. 22 is a comparison plot of the feed nonuniformity coefficients for the three embodiments of FIGS. 19, 1 and 16;

FIG. 23 is a schematic diagram of the placement of a second feed inlet for an embodiment of the swirling liquid feed of the present invention containing particles in one liquid of an in-line static mixer;

FIG. 24 is a plot of the volumetric content of the feed for an embodiment of the in-line static mixer of the present invention in which the swirling liquid feed contains particles in the liquid;

FIG. 25 is a schematic illustration of the material non-uniformity coefficient for an embodiment of the swirling liquid material in-line static mixer of the present invention having particles in the liquid;

FIG. 26 is a schematic diagram of the placement of the second feed inlet of one embodiment of the swirling liquid feed in-line static mixer of the present invention.

The utility model is further explained below with reference to the figures and examples.

Detailed Description

Specific embodiments of the present invention will be described in more detail below with reference to fig. 1 to 26 of the accompanying drawings. While specific embodiments of the utility model are shown in the drawings, it should be understood that the utility model may be embodied in various forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the utility model to those skilled in the art.

It should be noted that certain terms are used throughout the description and claims to refer to particular components. As one skilled in the art will appreciate, various names may be used to refer to a component. This specification and claims do not intend to distinguish between components that differ in name but not function. In the following description and in the claims, the terms "include" and "comprise" are used in an open-ended fashion, and thus should be interpreted to mean "include, but not limited to. The description which follows is a preferred embodiment of the utility model, but is made for the purpose of illustrating the general principles of the utility model and not for the purpose of limiting the scope of the utility model. The scope of the present invention is defined by the appended claims.

For the purpose of facilitating understanding of the embodiments of the present invention, the following description will be made by taking specific embodiments as examples with reference to the accompanying drawings, and the drawings are not to be construed as limiting the embodiments of the present invention.

For better understanding, as shown in fig. 1 to 26, an in-line static mixer for a swirling liquid material includes,

a pipe body 1 extending along a central axis thereof;

a first raw material inlet 2 which is arranged at the top end of the tube body 1 and is collinear with the central axis;

the second raw material inlet 3 is arranged on the side wall of the pipe body 1 and is vertical to the central axis;

the first vortex flow pipe 4 is arranged in the pipe body 1 and communicated with the first raw material inlet 2;

the second vortex flow pipe 5 is arranged in the pipe body 1 and is communicated with the first vortex flow pipe 4 and the second raw material inlet 3;

a third vortex tube 6 which is provided in the pipe body 1 and communicates with the second vortex tube 5;

the discharge hole is formed in the bottom end of the pipe body 1 and communicated with the third vortex flow pipe 6; wherein the first vortex flow pipe 4, the second vortex flow pipe 5 and the third vortex flow pipe 6 all comprise inner pipe walls positioned in the pipe body 1, the inner pipe walls comprise,

a first transition section 8 located at an upper end of the inner pipe wall, the first transition section 8 having a first length and a first cross section in a longitudinal direction of the swirl flow pipe, the first cross section smoothly transitioning from a circular shape having a radius R to a vane shape including a square having a side length of 2R and a semicircle having a radius R extending on each side of the square while the first transition section 8 is twisted by a first predetermined angle in the longitudinal direction, a cross-sectional area of the first cross section remaining constant;

a swirling flow section 10 connecting the first transition section 8, the swirling flow section 10 having a second length in the longitudinal direction of the swirling flow tube and a second cross section being the shape of the vane as the swirling flow section 10 twists by a second predetermined angle in the longitudinal direction;

a second transition section 9 connecting the swirling flow section 10 and located at a lower end of the inner tube wall, the second transition section 9 having a third length and a third cross section in the longitudinal direction of the swirling flow tube, the third cross section smoothly transitioning from the vane shape to a circular shape with a radius R while the second transition section 9 is twisted by a third predetermined angle in the longitudinal direction, a cross sectional area of the third cross section remaining unchanged, the cross sectional areas of the first, second and third cross sections being the same.

In the preferred embodiment of the vortex type liquid material in-line static mixer, the second material inlet 3 comprises 2 inlet pipes arranged at the opposite sides of the pipe body 1 and is not on the same horizontal plane.

In the preferred embodiment of the on-line static mixer for the vortex liquid raw materials, the first vortex tube 4 rotates in a direction opposite to the second vortex tube 5, and the third vortex tube 6 rotates in a direction opposite to the second vortex tube 5.

In the preferred embodiment of the online static mixer for the vortex type liquid raw materials, the pipe body 1 between the first vortex flow pipe 4 and the second vortex flow pipe 5 is a premixing area 7, and the length of the pipe body is 1-120 times of the pipe diameter of the first vortex flow pipe 4.

In the preferred embodiment of the online static mixer for the vortex liquid raw materials, the pipe body 1 between the third vortex pipe 6 and the second vortex pipe 5 is a straight pipe, and the length of the pipe body is 1-120 times of the pipe diameter of the second vortex pipe 5.

In the preferred embodiment of the online static mixer for the vortex liquid raw materials, at least one vortex tube with opposite rotation directions is arranged between the discharge port and the third vortex tube 6.

In a preferred embodiment of the vortex liquid raw material in-line static mixer, the blade shape is 2 blade shape, 3 blade shape, 4 blade shape, 5 blade shape or 6 blade shape.

In a preferred embodiment of the vortex type liquid raw material in-line static mixer, the first predetermined angle is 90 degrees, the second predetermined angle is 180 degrees, and the third predetermined angle is 80 degrees.

In a preferred embodiment of the swirl liquid feed inline static mixer, the first cross-sectional twist angle is gradual based on an alpha transition curve, wherein,

l is a first length, and x is a position coordinate of the first cross section in the length direction. t and k are two power law variable coefficients of alpha transition curve gradual change, and the shape of the gradual change curve can be adjusted. Preferably 0.8 < t < 1.2, 0.4 < k < 0.8, the vortex generation efficiency is optimal.

In a preferred embodiment of the swirl type liquid raw material in-line static mixer, the first cross-section torsion angle and/or the third cross-section torsion angle is gradually changed based on a victorissist curve or a cosine function.

In one embodiment, as shown in fig. 2, the secondary feed inlets 3 are arranged in a tangential inlet manner, i.e. one at the upper end and the other at the lower end. The two flows enter the annular region between the inner and outer tubes vertically, forming a vortex flow, as shown in fig. 3. First liquid raw materials gets into the blender through first raw materials entry 2 after, through first vortex flow tube 4 after, for the vortex effect of applying of first liquid raw materials self, when the export of first raw materials in the blender flows out, has the torrent shear energy of reinforcing, can promote to go the dispersion effect in downstream space. The second liquid feed passes through the second feed inlet 3, creating a tangential velocity in the form of a tangential inlet, creating a swirling flow in the annular region between the inner and outer tubes. The first liquid feed and the second liquid feed both present a swirling flow when entering the premixing zone 7, having a strong swirling shear action. The two liquids create sufficient mutual shear and mixing in the premixing zone 7. Wherein the first liquid material and the second liquid material can rotate in the same or opposite directions. But one of them is rotated in the opposite direction to the vortex rotation of the second vortex tube 5 to create further counter-current liquid cutting-position shifting-remixing, enhancing mixing. The length of the premixing area 7 is preferably 0 to 120 times of the pipe diameter d of the first vortex pipe 4, and the preferable length is 40 to 80 d. The liquid feed passing through the premixing zone 7 has a swirling effect of its own and the unevenness is already low. After entering the second vortex flow pipe 5, on the basis of the original vortex, the vortex is generated by superposition again, and the mixing is further promoted.

Can set up certain straight tube section after second vortex flow pipe 5 again as required, mixing action continuation zone makes the vortex flow continuously develop in the straight tube section, further promotes the mixture. The mixing action continuous area can reach the length of 0-120 times of the pipe diameter D of the outer pipe, and the ideal length is 40-80D. Can increase the third vortex flow tube 6 that vortex direction of rotation and second vortex flow tube 5 are opposite at the pipe section back in first mixing action continuation zone as required. Can set up the second mixing action continuation zone straight tube list behind second vortex flow tube 5 as required and with the fourth vortex flow tube of 6 opposite direction of rotation of third vortex flow tube. And so on until the fully mixed liquid feedstock exits the mixer from the discharge port.

The following is a preliminary CFD simulation of the mixer effect. The first liquid feed was an oil, having a density of 889kg/m3 and a viscosity of 0.00332kg/(ms), entering the mixer from the first feed inlet 2. The second liquid material was water, had a density of 998.2kg/m3 and a viscosity of 0.001003kg/(ms), and entered the mixer through the second material inlet 3. The surface tension coefficient between oil and water was set to 0.15N/m. After the calculation, the volume content distribution of the oil is shown in fig. 4, wherein red indicates that the oil content is 100%, and blue indicates that the oil content is 0, i.e., the water content is 100%. Figure 5 shows the data for the non-uniformity coefficient for two liquids, the variation in the path from the outlet of the first vortex tube 4 to the discharge opening. For the quantification of the mixing effect, it is currently mature to determine the mixing effect according to the magnitude of the non-uniform coefficient. Generally, the mixing is considered to be good when the coefficient of the unevenness is 0.05 or less, and complete mixing is considered to be achieved when the coefficient of the unevenness is 0.01 or less.

The non-uniformity coefficient ψ is defined as:

wherein σ represents a standard deviation of the mixed concentration distribution on the cross section, and is calculated by the mixed concentration of all points on the cross section, and the expression is as follows:

mean values of the mixed concentration on the cross-section:

fig. 5 shows a swirling flow of the liquid feed and second liquid feed streams generated by the tangential injection of the first swirl tube 4 and second feed inlet 3, which produces a strong dispersion, shear and mixing action of the two liquids in the premixing zone 7, reducing the non-uniformity coefficient from 2.2 to around 0.05 in the premixing zone 7. Then mix again through second vortex flow tube 5, the inhomogeneous coefficient has reached 0.0012, has reached the complete mixing state.

In one embodiment, the mixer includes a first vortex tube 4, a second vortex tube 5, or a third vortex tube 6, which is comprised of a first transition section 8, a vortex flow section 10, and a second transition section 9. Wherein the cross-sectional shape of the swirling flow section 10 may be 2-vane shape, 3-vane shape, 4-vane shape, 5-vane shape, and 6-vane shape. Among them, the shape of 3, 4, 5 blades is preferable. As shown in fig. 6 to 8. The cross-sectional shape of the vane is 4 vanes, the generated vortex effect is maximum, the pressure loss caused by the vane is minimum, and the energy efficiency ratio is highest. The vortex flow section 10 is formed by rotating and drawing a cross-sectional shape counterclockwise or clockwise along the central axis. The ratio of the stretched length to the equivalent radius (i.e., the pitch ratio) is preferably controlled to be in the range of 1 to 16. The angle of rotation is preferably between 90 and 720 degrees. The cross section of the first transition section 8 is preferably formed by a circular cross section which is gradually changed into a blade-shaped cross section over its length and is rotated by a predetermined angle, the logical ratio of which preferably coincides with the logical ratio of the swirl flow section 10, and the rotation angle is preferably 360 °/the number n of blades in the cross section. The second transition section 9 has a cross section which is tapered from a vane shape to a circle over its length and is rotated by a certain angle, preferably a logical ratio which is identical to that of the swirl flow section 10, and the rotation angle is preferably 360 DEG/the number n of vanes in the cross section.

Since early numerical simulations and experimental verification showed that the 4-blade section has the optimal energy efficiency ratio, a preferred embodiment of the vortex tube is described below in a 4-blade shape, as shown in fig. 9. The first vortex tube 4, the second vortex tube 5 or the third vortex tube 6 comprises an outer tube wall and an inner tube wall, wherein,

the inner pipe wall comprises a first inner pipe wall,

As shown in fig. 10, in the first and second transition sections 9, the cross-sectional shape of the inner wall of the pipe is changed from a circular shape to a blade-shaped cross-section, and the cross-section is rotated clockwise (+1) or counterclockwise (-1) by a predetermined angle in the axial direction. The angle of rotation is 90 degrees. Wherein, the Rcs is the diameter of the circumcircle of the square inside after the gradual change is finished. And R is the diameter of the internal square circumscribed circle in the gradual change process. rf is the radius of the blade-shaped fan after the gradual change is finished, and r is the radius of the blade-shaped fan in the gradual change process. A is the center of the blade-shaped fan. y is the distance from A to the center O of the square circumscribed circle. The angle formed by the radius of the blade-shaped fan and the square vertical side (FB) is included. This is 45 ° when the cross-section is circular and 90 ° when the cross-section is the shape of a complete blade. As the entrance angle gradually increases from 45 ° to 90 °, a series of transition sections may be formed. These sections are rotated clockwise (or counterclockwise) through a predetermined angle in the course of the axial gradation. As shown in fig. 11, if the pitch change between the cross sections is uniform during the clockwise rotation of each cross section in the axial direction, the transition is linear. In order to generate a greater swirl strength and reduce the on-way pressure loss, a smoother transition can be designed at the beginning and end of the transition section, i.e. a smaller angle of rotation per unit distance. Such as an alpha transition curve based on a cosine function, or using a vitoscinki curve. Wherein,

preferably, in the vortex tube, the first length is equal to the third length, and the first length and/or the third length is half of the second length.

In the vortex flow pipe, the outer pipe wall is a straight pipe, and the radius R is 0.01m to 100 m.

In the vortex tube, a ratio of the first length or the third length to the second length is equal to a ratio of the first predetermined angle or the third predetermined angle to the second predetermined angle.

In the vortex tube, the first preset length is one fourth of the vortex tube, the second preset length is one half of the vortex tube, and the third preset length is one fourth of the vortex tube.

In the vortex flow pipe, the vortex flow pipe is connected with a pipeline with the radius of R.

In the vortex tube, the first predetermined angle is 90 degrees, the second predetermined angle is 180 degrees, and the third predetermined angle is 90 degrees.

In the vortex tube, the sum of the first predetermined angle, the second predetermined angle and the third predetermined angle is 360 degrees.

In the vortex tube, the ratio of the sum of the first length, the second length and the third length to the radius R is 8: 1.

Wherein, the ratio of the sum of the first length, the second length and the third length to the radius R is 8: 1, which is based on the ratio of the strength of the vortex generated by the vortex flow pipe to the pressure loss caused by the vortex flow pipe. I.e. the maximum intensity of the vortex flow is generated with the minimum pressure loss. When applied to different treatment systems, such as the cleaning of milk processing equipment, a smaller ratio (e.g., 6: 1) may be used to produce a greater cleaning effect.

In addition to the exemplary embodiment described above, a simpler liquid feed entry is shown in FIG. 12. The second swirl tube 5, the first mixing action sustaining zone, etc. in the exemplary embodiment of fig. 1 can then be directly connected. This embodiment is simple and suitable for mixing applications where the mixing uniformity is low, e.g. a non-uniformity coefficient of around 0.05. Wherein the first liquid raw material enters from the small round tube; the second liquid feedstock enters from the annular inlet. The simulation graph is shown in fig. 13, and the distribution of the uneven coefficients is shown in fig. 14.

Another simpler embodiment is shown in fig. 15: wherein the first liquid feedstock enters from the horizontal round tube and the second liquid feedstock enters from the vertical round tube.

As shown in fig. 16, in another embodiment of the inlet, the first swirl tube 4 extending into the mixer can be moved to the outside so that the first liquid material meets the second liquid material at the outlet of the mixer in the same region where they shear-split-position move to-rejoin. Allowing the two liquids to mix earlier. The direction of the swirl generated by the first material inlet 2 of the second embodiment coincides with the direction of the swirl generated by the tangential inlet for the second material. Opposite to the direction of rotation of the following second swirl tube 5. CFD numerical simulations show that this embodiment of the liquid feed inlet produces better mixing, and because of the extended length and effect of the premixing zone 7, near complete mixing is achieved in the premixing zone 7 with a non-uniformity coefficient of near 0.01. And can achieve full and complete mixing after passing through the second vortex tube 5. The simulation graph is shown in fig. 17, and the distribution of the uneven coefficients is shown in fig. 18.

FIG. 19 is a schematic of the feed non-uniformity coefficient for one embodiment of the swirling liquid feed in-line static mixer of the present invention. FIG. 20 is a plot of the volumetric content of the feedstock as well as a plot of the liquid feedstock flow path for an embodiment of the swirling liquid feedstock in-line static mixer of the present invention. FIG. 21 is a schematic view of the material non-uniformity coefficient of one embodiment of the swirling liquid material in-line static mixer of the present invention. FIG. 22 is a graph showing a comparison of the coefficients of nonuniformity of raw materials in the three embodiments of FIGS. 19, 1 and 16. It can be demonstrated from the figure that the embodiment of the feed inlet has an important influence on the final liquid feed mixing effect. The tangential inlet to the second liquid feed in the embodiment of FIG. 1 increases the swirl strength and mixing effect of the pre-mix section as compared to the embodiment of FIG. 19. The embodiment shown in fig. 16 allows the two liquids to directly interact with each other and impact and mix when entering the system, further improving the mixing effect in the premixing area, and the final mixing effect is better. These comparisons indicate that the innovative design of the liquid feed entry system has an important role in the efficacy of the static mixer.

The utility model also applies to the original mixing of the liquid raw material with particles, in which several embodiments of the utility model are also presented above. When the particle diameter is very small, such as micron-sized, and the density is close to that of the raw material liquid, the above raw material inlet embodiments can achieve good mixing effect. When the particles are large, the feeding of the liquid raw material containing particles can be performed as shown in fig. 23. Wherein the first and second particulate-containing feedstock inlets may be arranged in parallel. As shown in fig. 24 to 25, two different particles enter the pipeline in parallel, mixing is not obvious before entering the vortex flow pipe, mixing is enhanced after entering the vortex flow pipe, different cross sections are cut along the pipeline axis on the pipeline of the numerical simulation by adopting a non-uniformity analysis method similar to that when different liquids are mixed, each cross section is divided into 100 grids, the number of the first particles in each grid is obtained (100 data are obtained), and the standard deviation and the average value of the 100 data are obtained, namely, the distribution diagram of the non-mixing degree of the similar liquids along the pipeline flow channel direction is obtained. It can be seen that the degree of mixing of the particles is significantly increased after passing through the vortex tube. The number of collisions of the two particles monitored, increased significantly as the liquid feed flowed through the vortex tube, indicating that mixing of the two particle-containing feeds was significantly enhanced.

FIG. 26 is a schematic diagram of the placement of the second feed inlet of one embodiment of the swirling liquid feed in-line static mixer of the present invention. This kind of embodiment is applicable to the great liquid raw materials of mixed difficulty, increases a vortex flow tube respectively at the entrance of second liquid raw materials both sides, can let the liquid raw materials get into the vortex shearing action of producing the degree behind the blender, promotes the mixture of liquid. The basic principles of the present application have been described above with reference to specific embodiments, but it should be noted that advantages, effects, etc. mentioned in the present application are only examples and are not limiting, and the advantages, effects, etc. must not be considered to be possessed by various embodiments of the present application. Furthermore, the foregoing disclosure of specific details is for the purpose of illustration and description and is not intended to be limiting, since the foregoing disclosure is not intended to be exhaustive or to limit the disclosure to the precise details disclosed.

The foregoing description has been presented for purposes of illustration and description. Furthermore, the description is not intended to limit embodiments of the application to the form disclosed herein. While a number of example aspects and embodiments have been discussed above, those of skill in the art will recognize certain variations, modifications, alterations, additions and sub-combinations thereof.

Claims

1. A vortex type liquid raw material on-line static mixer is characterized in that the mixer comprises,

a tube extending along a central axis thereof;

the second raw material inlet is arranged on the pipe body;

a swirling flow section connecting the first transition section, the swirling flow section having a second length in a longitudinal direction of the swirling flow tube and a second cross section that twists by a second predetermined angle in the longitudinal direction as the swirling flow section;

2. The vortex liquid feed in-line static mixer of claim 1 wherein the second feed inlet comprises 2 inlet tubes disposed on opposite walls of the tube and perpendicular to the central axis, the 2 inlet tubes not being in the same horizontal plane.

3. An in-line static mixer of a swirling liquid feed as claimed in claim 1, wherein the first swirl tube rotates in a direction opposite to the second swirl tube and the third swirl tube rotates in a direction opposite to the second swirl tube.

4. The in-line static mixer of claim 1, wherein the second material inlet is disposed at a top end of the tube body and does not communicate with the first swirling tube.

5. The in-line static mixer of vortex-type liquid raw material as claimed in claim 1, wherein the tube body between the first vortex tube and the second vortex tube is a premixing zone having a length 1-120 times the diameter of the first vortex tube, and the tube body between the third vortex tube and the second vortex tube is a straight tube having a length 1-120 times the diameter of the second vortex tube.

6. The in-line static mixer of claim 1, wherein at least one swirl tube is disposed between the outlet and the third swirl tube, the swirl tubes rotating in opposite directions.

7. The swirling liquid feed inline static mixer of claim 1, wherein the blade shape is a 2-blade shape, a 3-blade shape, a 4-blade shape, a 5-blade shape, or a 6-blade shape.

8. The swirling liquid feed in-line static mixer of claim 1, wherein the first predetermined angle is 90 degrees, the second predetermined angle is 180 degrees, and the third predetermined angle is 80 degrees.

9. The swirling liquid feed in-line static mixer of claim 1, wherein the first cross-sectional twist angle is gradual based on an alpha transition curve, wherein,

l is a first length, x is a position coordinate of the first cross section in the length direction, and t and k are two power law variable coefficients of gradual change of an alpha transition curve.

10. The swirling liquid feed inline static mixer of claim 1, wherein the first cross-sectional twist angle and/or the third cross-sectional twist angle is/are graduated based on a vittonsisky curve or a cosine function.