A fluid material mixing system based on multi-state motion

Abstract

The application belongs to the field of fluid mixing and reaction equipment, and discloses a fluid material mixing system based on polymorphic motion, which comprises a reactor cavity, a plurality of adjacent cavities are arranged in the reactor cavity, and different cavities have the same or different flow cross sections; two adjacent cavities are communicated through at least one orifice, and each orifice has the same or different flow cross section; liquid flows into the cavities from an inlet, part of the liquid directly turns back in the forward channel, part of the liquid turns by 90 degrees and flows into the orifice, and then turns by 90 degrees and flows to the next cavity. The application sets the orifices with different shapes, sizes and quantities between the adjacent cavities with different flow cross sections, can flexibly change the flow rate of the fluid, and makes the fluid appear in the polymorphic motion modes such as turbulent flow, vortex, reverse reflux, turn-back pressure fluctuation, secondary flow and flow separation in the forward channel, so that the mixing efficiency is significantly improved.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of fluid mixing and reaction equipment, and particularly relates to a fluid material mixing system based on polymorphic motion. BACKGROUND

[0002] The existing fluid material mixing generally adopts a conventional single-stage pipeline mixer. The conventional single-stage pipeline mixer is mainly connected through a U-shaped return of a circular pipe and generally has a fixed pipe diameter. When in use, the fluid flowing in the pipeline produces laminar flow mixing, and the fluid in the return area (at the position of the U-shaped turn) is subjected to intensified pressure difference between the outside and the inside of the return due to uneven velocity distribution, which can cause fluid rotational motion and generate pressure vortex.

[0003] The mixing of the single-stage pipeline mixer mainly depends on laminar diffusion, and therefore, to enhance the mixing efficiency, generally needs to:

[0004] a) increase the length of the pipeline to enhance the mixing effect, which leads to a large device volume and increased processing cost.

[0005] b) increase the roughness of the pipeline wall, for example, use a corrugated pipe, which can accumulate garbage and cause pipeline blockage.

[0006] c) embed a flow resistance in the pipeline to enhance the mixing effect, which can easily cause pipeline blockage and has high energy consumption.

[0007] Moreover, no matter which improvement is adopted, the single-stage mixing effect is still poor and difficult to adapt to high-concentration or high-viscosity fluid; therefore, in order to meet the mixing effect, the pipeline mixer is often set as a multi-stage mixer to meet the mixing effect by changing the flow rate from the inlet to the outlet, and the pipe diameter of the mixer in the rear stage is often increased step by step to achieve the purpose of reducing the flow rate. The reduced flow rate leads to further deterioration of the mixing effect, and therefore, the rear stage needs to increase longer pipelines. Due to the lengthening of the pipeline and the increase of the pipe diameter, it leads to a large floor area and high cost.

[0008] In actual use, the dosing pipe is inserted into the pipeline mixer to mix the liquid in the pipeline with the liquid in the pipeline through water flow or increased laminar exchange of the pipeline mixer. At this time, if the flow rate in the pipeline is too fast or the flow is too large, the liquid mixing will not be uniform enough. Moreover, when the analysis instrument is inserted into the pipeline for measurement, if the liquid mixing is not uniform, the accuracy of the measurement result will be seriously affected.

[0009] In addition, the liquid medicine pulse also has an adverse effect on the mixing uniformity, because the liquid medicine is not continuously added to the pipeline, leading to uneven mixing in the liquid, and often needs to be finally collected into a liquid tank, a pool or other container cavity, so as to realize the full mixing and reaction of the liquid medicine in the liquid by increasing the volume, slowing down the flow rate, and even further stirring, which undoubtedly increases the complexity and cost of the process flow. SUMMARY

[0010] In order to solve the above problems, the application provides a fluid material mixing system based on polymorphic motion, which can fully mix the liquid medicine and liquid, and effectively avoid the influence of liquid medicine pulse on mixing uniformity.

[0011] Therefore, the technical scheme of the application is as follows: a fluid material mixing system based on polymorphic motion, comprising a reactor cavity, a plurality of adjacent cavities are arranged in the reactor cavity, and the different cavities have the same or different sizes and shapes of flow cross sections; adjacent two cavities are communicated through at least one orifice, and each orifice has the same or different sizes and shapes of flow cross sections.

[0012] The liquid flows into the cavities from the inlet, and in the flowing process: part of the liquid in the cavities directly turns back in the forward channel, part of the liquid flows into the orifice by turning 90 degrees, and then flows to the next cavity by turning 90 degrees.

[0013] On the basis of the above scheme and as a preferred scheme of the above scheme: another cavity can be arranged on the front, rear, left, right, upper and lower sides of each cavity, and the two cavities are communicated through an orifice.

[0014] On the basis of the above scheme and as a preferred scheme of the above scheme: the liquid in the cavities has a laminar flow, and the flow directions of the laminar flows in the adjacent two cavities are different by 180 degrees.

[0015] When the liquid directly turns back in the forward channel, the liquid in the cavities has a turbulent flow, vortex, reverse reflux and / or turn-back pressure fluctuation state;

[0016] When the liquid flows into the orifice by turning 90 degrees, and then flows to the next cavity by turning 90 degrees, the liquid has a turbulent flow, vortex, double vortex flow, flow separation and / or low-pressure backflow state at the orifice.

[0017] On the basis of the above scheme and as a preferred scheme of the above scheme: a movable adjusting plate is arranged on the orifice to adjust the size or shape of the flow cross section of the orifice; or, the orifice is provided with a spoiler with different hole diameters and different hole shapes.

[0018] On the basis of the above scheme and as a preferred scheme of the above scheme: one end of the adjacent two cavities is communicated through an orifice, or both ends are communicated through an orifice, or the middle is communicated through a plurality of orifices.

[0019] As a preferred scheme of the above scheme and on the basis of the above scheme: the reactor cavity is a square cavity, a horizontal or vertical partition plate is arranged in the reactor cavity to form adjacent partitions; the partition plate is provided with an orifice communicating the two partitions, or the partition plate end and the inner wall of the square cavity form an orifice.

[0020] As a preferred scheme of the above scheme and on the basis of the above scheme: the reactor cavity is a square cavity, a plurality of parallel square pipes are arranged in the reactor cavity, an orifice is arranged between adjacent square pipes, and the orifice communicates the two square pipes.

[0021] As a preferred scheme of the above scheme and on the basis of the above scheme: the reactor cavity is a cylindrical cavity, a plurality of axially arranged circular partitions are arranged in the cylindrical cavity, and at least one orifice is arranged between adjacent two circular partitions; a flow channel is arranged in each circular partition and communicates with the orifice.

[0022] As a preferred scheme of the above scheme and on the basis of the above scheme: the flow channel in the circular partition is an equidistant spiral structure or a variable-pitch spiral structure.

[0023] As a preferred scheme of the above scheme and on the basis of the above scheme: the inlet and outlet of the cylindrical cavity are arranged in a tangential direction or perpendicular to the upper and lower end faces.

[0024] In addition to conforming to the traditional laminar flow and vortex principle, the present application introduces more motion principles, as follows:

[0025] 1) Direct U-turn in the forward channel: the liquid in the flow has momentum (the product of mass and velocity). When the flow direction needs to change sharply by 180°, the inertia of the liquid will resist this change, and the fluid will try to maintain the original flow direction. The fluid near the U-turn wall is forced to slow down, turn, or even partially stop, while the fluid in the center continues to advance or tries to "squeeze" through the U-turn point under the action of inertia and pressure gradient. This dramatic change in momentum leads to the following complex phenomena:

[0026] a) Forming a turbulent vortex, applying dynamic load to fluid clusters or droplets through stretching, shearing and other forces, causing inertial breakage and viscous shear breakage of the dispersed phase, significantly reducing the droplet size and expanding the distribution range, thereby increasing the interfacial contact area and improving the mixing efficiency;

[0027] b) Forming a reverse flow, breaking the stable stratification of the laminar flow state, promoting irregular collision and mixing of fluids in different regions, reducing the influence of liquid pulse, and making the mixing more uniform;

[0028] c) U-turn pressure fluctuation, inducing repeated conversion of fluid kinetic energy and pressure energy, which is helpful for mixing.

[0029] 2) 90 degrees + 90 degrees turning in the forward channel: the fluid has inertia, tends to maintain the original direction and speed of movement. The first 90-degree turn into a narrow orifice, the fluid is forced to change direction and accelerate (because the orifice cross-sectional area is usually smaller than the cavity, the speed increases). The liquid core part will impact the wall opposite the gap due to inertia, and be "extruded" and accelerated in the gap. The second 90-degree turn out of the gap into the next cavity, the flow direction changes again, and the cross-section expands again, the continuous sharp turn and cross-section change greatly disturb the momentum of the fluid, resulting in the following complex phenomena:

[0030] a) strong turbulent vortex is formed, which exerts dynamic load on the fluid clusters or droplets through stretching, shearing and other forces, causing inertial breakage and viscous shear breakage of the dispersed phase, significantly reducing the droplet size and expanding the distribution range, thereby increasing the interfacial contact area and improving the mixing efficiency;

[0031] b) secondary flow is formed at the location where the flow direction changes, exhibiting a double vortex structure, which further enhances the mixing effect together with the turbulent flow;

[0032] c) flow separation occurs at the right-angle turning area, forming a low-pressure backflow area, which further enhances the mixing effect.

[0033] 3) Designing adjacent cavities of different sizes can change the flow rate (speed up or slow down). If multiple different size cavities are connected in series, periodic flow disturbances will occur:

[0034] a) Periodic acceleration / deceleration cycle: the flow rate changes repeatedly, and the energy is converted between kinetic energy and pressure energy at a high frequency;

[0035] b) Turbulent oscillation and pressure pulsation: the size and location of the separation zone change dynamically, causing low-frequency pressure fluctuations.

[0036] 4) If it is designed as a cylindrical cavity, the spiral flow channel will also change the liquid flow rate, which will intensify the secondary flow, further distort and enhance the mixing effect.

[0037] In summary, according to the fluid dynamics mechanism, the present application has three layers of reaction:

[0038] Primary mixing: the fluid is preliminarily mixed with the reagent in a laminar flow state in the straight pipe section (the reagent addition port is on the side wall of the pipe), or in a turbulent flow state at the end (the reagent addition port is at the end of the pipe);

[0039] Secondary reinforcement: When fluid flows through 90 degrees + 90 degrees "orifice", variable cross-section, and flow diversion, due to sudden reduction or sudden change of cross-sectional area, and sudden change of flow direction, etc., local flow rate multiplication, liquid backflow, liquid rotation, etc. are generated, inducing vortex and turbulence "multi-state motion";

[0040] Third-order reaction: When the spin fluid enters the next stage of the cavity, due to the recovery or expansion of the cross-sectional area, or the increase of the volume, the reverse shear force is generated, and the reaction contact time is prolonged.

[0041] Therefore, the multi-state motion modes of different size scales, such as laminar flow, vortex flow, double vortex, reverse flow, turnaround pressure fluctuation, vortex, turbulence, flow separation and backflow, etc. appear in the coagulation reactor of the present application, and the basic mixing principle is summarized as follows:

[0042] a) Large-scale multi-state motion mode dominates macroscopic mixing, and small-scale multi-state motion mode refines the mixing structure in local area through turbulence diffusion and vortex stretching mechanism, forming a multi-scale cooperative mixing enhancement effect;

[0043] b) Multi-state motion mode accelerates energy transfer efficiency, kinetic energy is transferred from large scale to small scale, forming an energy cascade process, and finally converted into heat energy. This process accelerates molecular diffusion through microscale energy dissipation, and strengthens the mixing effect, making the mixing fine and uniform.

[0044] Compared with the prior art, the present application has the following advantages:

[0045] By setting orifices with different shapes, sizes and numbers between adjacent cavities with different flow cross sections, the flow rate of the fluid can be flexibly changed, so that the fluid appears in a flow state of direct turnaround or turning 90 degrees + 90 degrees in the forward channel, thereby forming multi-state motion modes such as turbulent vortex, reverse backflow, turnaround pressure fluctuation, secondary flow and flow separation, thereby significantly improving the mixing efficiency.

[0046] The adjustable sliding plate or the turbulence plate with different hole diameters and hole shapes arranged on the orifice can adjust the flow cross-sectional size or shape of the orifice, and further accurately control the flow state and mixing effect of the fluid.

[0047] The various connection modes between adjacent cavities, such as one end connection, two end connection or multiple connections in the middle, especially the two-way circulation flow state and flow slowing down area formed by two end connection, provide more adjustability for the mixing process, and adapt to the mixing needs of different characteristic fluids.

[0048] Whether by setting a cavity plate in the cavity or by setting multiple parallel connected pipes to form a cavity, the overall structure is relatively simple and compact compared with the traditional multi-stage pipeline mixer, reducing the space occupation caused by the lengthening and enlarging of the pipeline, and reducing the processing cost.

[0049] A set or multiple sets of reactors cavities in series / parallel can be arranged in the shell to achieve modular design, facilitating flexible construction and adjustment according to actual needs, and having good modular scalability. BRIEF DESCRIPTION OF DRAWINGS

[0050] Figure 1 It is a structural principle schematic diagram of Example 1; wherein: ① laminar flow, ② backflow, ③ turbulent flow, vortex, double vortex flow, secondary flow, etc., ④ bidirectional circulating flow;

[0051] Figure 2 It is a structural principle schematic diagram of Example 2;

[0052] Figure 3 It is a structural sectional view of Example 3;

[0053] Figure 4 It is a structural sectional view of Example 4;

[0054] Figure 5 It is an internal structure schematic diagram of Example 4;

[0055] Figure 6 It is a structural schematic diagram of Example 5;

[0056] Figure 7 It is an internal structure schematic diagram of Example 5;

[0057] Figure 8 It is an internal flow channel schematic diagram of Example 5;

[0058] Figure 9 It is a structural schematic diagram of Example 6.

[0059] In the figure, the marks are: reactor cavity 1, reactor inlet 11, reactor outlet 12, intermediate port 13, square cavity 14, cavity partition plate 15, cavity partition 2, orifice 3, flow slowing zone 4, adjusting plate 5, square pipeline 6, pipeline type reactor cavity 7, cylindrical shell 8, circular cavity partition plate 81, circular cavity partition 82, spiral flow channel 83. DETAILED DESCRIPTION

[0060] Example 1

[0061] The fluid material mixing system described in this embodiment includes a shell, a set of reactor cavities 1 is arranged in the shell, or multiple sets of reactor cavities can be arranged according to the use requirements, which can be connected in series or in parallel between the multiple sets of reactor cavities. The shell is provided with a reactor inlet 11 and a reactor outlet 12, which are connected with the inside of the reactor cavity 1. The reactor cavity 1 is provided with multiple adjacent cavities 2 (not less than 3), liquid enters from the reactor inlet 11 and flows towards the direction of the reactor outlet 12, flowing through each cavity 2.

[0062] At the same time, adjacent compartments 2 are connected through at least one orifice 3, which can be: one end of the two adjacent compartments 2 is connected through the orifice 3, or both ends are connected through the orifice 3, or multiple orifices 3 are connected between the two compartments 2. Each orifice 3 can be set in different styles to change the size and shape of the flow cross section, which is inconsistent with the size and shape of the compartment cross section. At the same time, the size of the adjacent two compartments can be changed, and the flow rate can be changed (accelerated or slowed down). When both ends of the two adjacent compartments 2 are connected through the orifice 3, the liquid in the two compartments exists in a two-way circulating flow state, forming a flow slowing area 4, and the flow rate of the flow slowing area can be slowed down. Different orifices can be set to form different scale reaction pool effects.

[0063] The front, back, left, right, top and bottom of each compartment 2 can be connected to another compartment 2, which can make the structure more compact, and multiple compartments can be connected in parallel or in series, etc. The flow channel in the reactor cavity 1 is similar to a maze structure, and the liquid state is more variable.

[0064] At the same time, the side of the shell is provided with a plurality of intermediate openings, which are connected with the reactor cavity 1 and can be used as a dosing port or a detection port. The dosing port facilitates the injection of liquid medicine, and the dosing port can be arranged on the side or end of the compartment according to the use requirement. The detection port can extract the detection liquid, and the related sensor can be directly placed in the detection port to monitor the reaction in the reactor.

[0065] The liquid flows into the compartment from the reactor inlet, and the following situations may occur during the flow process:

[0066] ① Some liquid directly turns back in the forward channel: when the flow direction needs to change sharply by 180°, the inertia of the liquid will resist such change, and the fluid will try to maintain the original flow direction. The fluid near the turning wall is forced to slow down, turn, or even stop, while the fluid in the center continues to advance or tries to "squeeze" through the turning point under the action of inertia and pressure gradient.

[0067] The sharp change in momentum will cause a strong adverse pressure gradient, which will lead to flow separation and form a reverse flow area; at the same time, flow separation and energy dissipation will produce a large amount of vortex and high turbulence, and the unsteady characteristics (formation, shedding, swinging, breaking) of the separation area and vortex are the core source of pressure fluctuation. In the curve turning, the secondary flow interacts with the above process, making the problem more complex.

[0068] Therefore, when the liquid directly turns back within the forward channel, it generates turbulence, eddies, reverse flow, and pressure fluctuations. Essentially, this is the result of the fluid inevitably undergoing a highly unstable, unsteady, and complex flow process with separation as it overcomes the enormous momentum and energy conversion required to overcome the sudden change in direction. The fundamental cause is the intense interaction between inertia, pressure gradients, and viscous forces.

[0069] ② Part of the liquid turns 90 degrees + 90 degrees, flowing from orifice 3 into the next compartment 2. Fluids have inertia and tend to maintain their original direction and velocity. When the fluid makes its first 90-degree turn and enters the narrow orifice, it is forced to change direction and accelerate (because the orifice's cross-sectional area is typically smaller than the compartment, the velocity increases).

[0070] The core of the liquid impacts the wall opposite the gap due to inertia and is "squeezed" and accelerated within the gap. When it makes a second 90-degree turn and flows out of the gap into the next compartment, the flow direction changes dramatically again, and the cross-section expands again. The continuous sharp turns and cross-section changes significantly disrupt the fluid's momentum.

[0071] When the liquid passes through two consecutive orifices connected by 90-degree turns, its flow essentially undergoes a series of violent fluid dynamic shocks:

[0072] The sudden change in momentum and localized acceleration disrupt the flow, leading to strong adverse pressure gradients that cause flow separation and the formation of large-scale recirculation zones / separation bubbles at key locations (inside and outside corners of the notch exit). The continuous curves induce and intensify secondary vortices, which superimpose with the large vortices generated in the separation zone to form a complex, often paired, vortex system (double vortex flow). The interaction of separation, secondary flow, velocity gradients (shear), and vortices results in enormous energy dissipation and intense turbulence. Typical low-pressure, low-velocity, countercurrent flow (low-pressure recirculation state) forms within the separation / recirculation zone.

[0073] In summary, this embodiment utilizes orifices of varying sizes and shapes to connect cavities of varying dimensions, resulting in multimodal motion patterns of varying scales, including laminar flow, eddy flow, double vortex flow, countercurrent flow, return pressure fluctuations, vortices, turbulence, flow separation, and backflow. This multimodal motion pattern significantly improves the mixing rate and uniformity of fluids through physical fragmentation, energy transfer, and multiscale coupling. Field verification has shown that the coagulant path length is reduced by over 50%, energy consumption is also reduced by over 50%, space usage is reduced (approximately 60%), and manufacturing costs are significantly reduced (approximately 40%).

[0074] Example 2

[0075] The embodiment is the same structure as that of embodiment 1, the difference is that the orifice 3 is provided with a slidable adjusting plate 5 to adjust the size or shape of the flow passage section of the orifice 3. Before use, the user can adjust the size of the orifice according to the sewage condition:

[0076] Small orifice: suitable for treating high-concentration and difficult-to-degrade organic matter (long residence time + strong mixing);

[0077] Increased flow rate and enhanced turbulence: reduced gap → reduced flow passage area → accelerated fluid (continuity equation) → increased shear force → intensified vortex shedding and turbulent pulsation → enhanced mixing (breaks concentration / temperature boundary layer).

[0078] Extended effective residence time: increased local pressure drop → increased resistance of fluid passing through the gap → reduced overall flow rate → extended hydraulic residence time (HRT) in the reaction chamber → increased contact time of pollutants with microorganisms / agents.

[0079] Low-pressure area promotes micro-mixing: low-pressure area formed downstream of the contraction section intensifies vortex motion (such as Karman vortex street), producing micro-scale mixing effect.

[0080] Large orifice: suitable for low influent load and easily degradable pollutants;

[0081] Reduced flow resistance: increased flow area → reduced local flow rate (sudden expansion effect) → significantly reduced pressure loss → decreased total flow resistance of the system;

[0082] Increased flux: under the same pumping power, the total flow of the system increases → the amount of sewage treated per unit time increases (speeds up the treatment rate).

[0083] Alternatively, in addition to setting a slidable adjusting plate 5 on the orifice 3 to change the size and shape of the orifice 3, a spoiler with different hole diameters and different hole shapes can also be set on the orifice 3. Fluid passing through the small hole forms a high-speed jet beam → jet collision and shearing between holes → micro-scale turbulent vortex group is generated (enhancing micro-mixing). At the same time, the special-shaped hole guides the flow (such as airfoil, spiral hole) will force the fluid to rotate or deflect at a specific angle → induce large-scale secondary flow (Dean vortex / spiral flow) → increase the range of transverse flow, enhance mixing efficiency.

[0084] Embodiment 3

[0085] This embodiment relies on the design principle of embodiment 1, the shell is a square shell, the square shell is provided with a reactor inlet 11, a reactor outlet 12 and at least one intermediate port; one or more square cavities 14 can be arranged in the square shell.

[0086] A plurality of parallel partition plates 15 are arranged in each square cavity 14, and the partition plates 15 are fixed on the side wall of the square cavity 14 to form a plurality of adjacent partitions 2, and the partitions 2 can also be arranged at different intervals. The length of the partition plate 15 can be set to be different, so that the size of the orifice 3 between the adjacent two partitions is different.

[0087] At the same time, an adjustable adjusting plate can also be arranged on the partition plate 15 to further adjust the size of the orifice. The adjusting plate can be realized through conventional sliding structures such as sliding grooves, long slot holes, fasteners and the like.

[0088] Embodiment 4

[0089] This embodiment relies on the design principle of embodiment 1. The shell is a square shell, and a plurality of parallel square pipes 6 are arranged in the square shell. The square pipes 6 are arranged at opposite positions of adjacent square pipes 6 to form intercommunicating orifices 3, so that the adjacent square pipes 6 are connected. At the same time, the square pipes 6 are welded together to form a group of pipe type reactor cavities 7, and the inside of the pipe becomes the reaction partition 2.

[0090] At the same time, a plurality of parallel pipe type reactor cavities 7 can be arranged in one shell, and the adjacent pipe type reactor cavities 7 can be connected through pipelines. The pipe type reactor cavity 7 is a flat structure, and the volume is relatively small after a plurality of groups are connected in series, and the floor area is also small.

[0091] Embodiment 5

[0092] This embodiment relies on the design principle of embodiment 1. This embodiment has a cylindrical shell 8, and a cylindrical cavity is arranged in the cylindrical shell 8. A plurality of axial circular partition plates 81 are arranged in the cylindrical cavity, so as to form circular partitions 82 stacked up and down, and at least one orifice 3 is arranged between the adjacent two circular partitions 82. A spiral flow channel 83 is arranged in each circular partition 82, and the spiral flow channel is an equidistant spiral structure or a variable-pitch spiral structure. The orifice 3 can be alternatively arranged at the center of the spiral flow channel 83 or the outermost circle, so as to connect all the circular partitions 82.

[0093] The reactor inlet 11 and the reactor outlet 12 of this embodiment are arranged in the tangential direction of the cylindrical shell, so that the liquid enters the circular partition 82 from the tangential direction, flows along the spiral flow channel 83 to the orifice at the center, and part of the liquid flows into the next layer of circular partition 82 through the orifice, and part of the liquid returns after impact, thereby generating a strong fluid dynamics impact.

[0094] Embodiment 6

[0095] The structure of this embodiment is the same as that of embodiment 5, and the difference lies in that the reactor inlet 11 and the reactor outlet 12 of this embodiment are arranged on the upper and lower end surfaces of the cylindrical shell 8, and the liquid vertically enters the circular partition 82, thereby increasing the impact force.

[0096] The above merely describes the preferred embodiments of the present application, and the protection scope of the present application is not limited to the above-described embodiments. Any technical solution falling within the concept of the present application shall fall within the protection scope of the present application. It should be noted that, for ordinary skilled persons in the art, some improvements and refinements without departing from the principles of the present application shall also be considered as falling within the protection scope of the present application.

Claims

1. A fluid material mixing system based on multi-state motion, characterized by: The invention comprises a reactor chamber, wherein a plurality of adjacent compartments are provided in the reactor chamber, wherein different compartments have flow cross-sections of the same or different sizes and shapes; two adjacent compartments are connected by at least one orifice, and each orifice has a flow cross-section of the same or different sizes and shapes; during the flow of liquid into the compartment from the inlet, part of the liquid in the compartment is directly turned back in the forward channel, and part of the liquid turns 90 degrees to flow into the orifice, and then turns 90 degrees to flow into the next compartment; Each compartment can be provided with another compartment in front, back, left, right, top or bottom, and the two compartments are connected through openings; One end of two adjacent compartments is connected through an orifice, or both ends are connected through orifices, or the middle is connected through multiple orifices.

2. A fluid material mixing system based on multi-state motion according to claim 1, characterized in that: The liquid in the compartment has a laminar flow, and the flow directions of the laminar flows in two adjacent compartments differ by 180 degrees; When the liquid is directly turned back in the forward channel, the liquid in the compartment will have turbulence, vortex, reverse flow and / or return pressure fluctuation state; When the liquid turns 90 degrees to flow into the orifice and then turns 90 degrees to flow into the next compartment, the liquid will experience turbulence, vortex, double vortex flow, flow separation and / or low-pressure reflux at the orifice.

3. A fluid material mixing system based on multi-state motion according to claim 1, characterized in that: The orifice is provided with a slidable adjustment plate to adjust the size or shape of the flow cross section of the orifice; or, the orifice is provided with spoilers with different apertures and different hole shapes.

4. A fluid material mixing system based on multi-state motion according to any one of claims 1 to 3, characterized in that: The reactor cavity is a square cavity, and horizontal or vertical partition plates are set in the reactor cavity to form adjacent cavities; the partition plates are provided with openings connecting the cavities on both sides, or the ends of the partition plates are spaced from the inner wall of the square cavity to form openings.

5. A fluid material mixing system based on multi-state motion according to any one of claims 1 to 3, characterized in that: The reactor cavity is a square cavity. A plurality of parallel square pipes are arranged in the reactor cavity. A through hole is provided between adjacent square pipes, and the hole communicates with two adjacent square pipes.

6. A fluid material mixing system based on multi-state motion according to any one of claims 1 to 3, characterized in that: The reactor cavity is a cylindrical cavity, in which a plurality of axially arranged circular compartments are provided, and at least one orifice is provided between two adjacent circular compartments; a flow channel is provided in each circular compartment, and the flow channel is connected to the orifice.

7. A fluid material mixing system based on multi-state motion according to claim 6, characterized in that: The flow channel in the circular compartment is an equidistant spiral structure or a variable pitch spiral structure.

8. A fluid material mixing system based on multi-state motion according to claim 6, characterized in that: The inlet and outlet on the cylindrical cavity are arranged along a tangential direction, or perpendicular to the upper and lower end surfaces.

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