Agricultural and forestry bioactive ingredient multistage membrane separation and purification equipment

Abstract

The utility model discloses a kind of agroforestry bioactive ingredient multistage membrane separation purification equipment, it is related to separation and purification technical field, including rack, multiple material barrels arranged on the rack, multiple membrane filters fixed on the rack and booster pump installed on the rack;The beneficial effects of the utility model are as follows: by the branch pipe of upper and lower shunt pipe in mixed flow component relative arrangement, make concentrated solution and inert gas form reverse opposite flow cyclone in mixing cavity, realize the quick uniform mixing of gas-liquid two-phase by the mutual shearing of two fluids;At the same time, the high-speed turbulent field formed in mixing cavity breaks inert gas into micro-bubble, continuously scours membrane surface after entering membrane filter, delays membrane pollution and stabilizes filtration flux;Whole machine realizes once feeding multi-component synchronous separation, continuous stable operation, effectively reduces material loss and artificial maintenance cost.

Description

Technical Field

[0001] This utility model relates to the field of separation and purification technology, specifically to a multi-stage membrane separation and purification device for agricultural and forestry bioactive components. Background Technology

[0002] In the field of extraction and purification of bioactive components in agriculture and forestry, multi-stage membrane separation technology is widely used due to its mild operation and high separation efficiency. Typical equipment usually includes a feed tank, a booster pump, and multi-stage membrane modules such as microfiltration, ultrafiltration, and nanofiltration connected in series to achieve fractional retention and purification of target products with different molecular weights. To pursue higher product yields, a circulating filtration mode is commonly used in industry, where the concentrate discharged from the membrane module is returned to the feed tank, mixed with a new batch of feed, and then reintroduced into the membrane system for separation.

[0003] However, the aforementioned recirculation filtration mode has shortcomings. In existing equipment, the concentrate is typically returned directly to the top or side wall of the feed tank via a single pipeline. Due to the high concentration of the returned liquid and the significant concentration gradient and temperature difference between it and the bulk feed liquid in the tank, relying solely on natural diffusion within the tank is insufficient to achieve uniform macroscopic mixing. This leads to continuous fluctuations in the concentration and composition of the feed liquid entering the booster pump and membrane module, resulting in excessively high local concentrations on the membrane surface, i.e., severe concentration polarization. The consequences include accelerated membrane flux decline, increased transmembrane pressure difference, and increased cleaning frequency, which restricts the continuous operating efficiency of the membrane module and affects the batch stability and overall separation yield of the final product. Utility Model Content

[0004] To address the shortcomings of existing technologies, this utility model provides a multi-stage membrane separation and purification device for agricultural and forestry bioactive components.

[0005] To achieve the above objectives, the technical solution of this utility model is as follows: A multi-stage membrane separation and purification device for agricultural and forestry bioactive components includes a frame, multiple material tanks arranged on the frame, multiple membrane filters fixed on the frame, and a booster pump installed on the frame. The clarified liquid outlet of each membrane filter is provided with a connecting pipe extending into the corresponding material tank. The inlet of the booster pump is connected to the outlet of the corresponding material tank via an inlet pipe. The device also includes a mixing assembly, which comprises: A mixing chamber, the mixing chamber being a longitudinally placed tubular structure, the lower end of which is connected to the outlet of the booster pump through an inlet pipe, and the upper end of which is connected to the inlet of the membrane filter through an outlet pipe; Two branch pipes are provided, with their top ends spaced apart vertically, and each has at least two branch pipes, all of which extend tangentially to the wall of the mixing chamber. The bottom end of the top-mounted diverter is connected to the concentrate outlet of the membrane filter, and the bottom end of the bottom-mounted diverter is fixedly connected to an aeration pump for conveying inert gas. The branch pipes located in different diverter pipes are arranged opposite to each other in the axial direction of the mixing chamber, and the tangential injection directions of the branch pipes located in different diverter pipes are opposite, so that the concentrate and inert gas form opposing swirling flows in the mixing chamber, so that the raw material liquid, concentrate and inert gas are mixed and then sent into the membrane filter through the outlet pipe.

[0006] Preferably, the end of the branch pipe extending into the inner cavity of the mixing chamber is provided with a jet nozzle, and the angle between the axis of the jet nozzle and the axis of the mixing chamber is 15° to 45°.

[0007] Preferably, both of the diversion pipes are expanded diameter pipes, the cross-sectional area of ​​the internal flow channel of the diversion pipe is larger than the cross-sectional area of ​​the internal flow channel of the inlet pipe, and the cross-sectional area of ​​the internal flow channel of the inlet pipe is smaller than the cross-sectional area of ​​the internal flow channel of the outlet pipe.

[0008] Preferably, a pressure regulating valve is provided on the connecting pipe between the air outlet of the aeration pump and the diversion pipe located below.

[0009] Preferably, a pressure sensor and / or a temperature sensor are provided on the inner wall of the mixing chamber, and a controller is mounted on the frame. The pressure sensor and / or temperature sensor, as well as the booster pump, are signal-connected to the controller. The controller adjusts the operating frequency of the booster pump according to the feedback signal from the pressure sensor and / or temperature sensor.

[0010] Preferably, the plurality of membrane filters are connected in series along the liquid flow direction, and the filtration pore size of each membrane filter decreases step by step along the liquid flow direction, namely, microfiltration membrane filter, ultrafiltration membrane filter and nanofiltration membrane filter.

[0011] Compared with the prior art, the beneficial effects of this utility model are as follows: By setting the branches of the upper and lower diversion pipes in the mixing component opposite to each other, the concentrate and inert gas form a counter-current swirling flow in the mixing chamber. The mutual shearing of the two fluids achieves rapid and uniform mixing of the gas and liquid phases, effectively solving the technical problem of uneven mixing between the concentrate and the feed liquid during the return of the concentrate, which leads to concentration polarization on the membrane surface. At the same time, the high-speed turbulent field formed in the mixing chamber breaks the inert gas into microbubbles, which continuously flush the membrane surface after entering the membrane filter, delaying membrane fouling and stabilizing the filtration flux. Combined with the series gradient separation of the multi-stage membrane filter and the feedback regulation of the booster pump by the controller, the whole machine achieves synchronous separation of multiple components with one feed and continuous and stable operation, effectively reducing material loss and manual maintenance costs. Attached Figure Description

[0012] The disclosure of this utility model is illustrated with reference to the accompanying drawings. It should be understood that the drawings are for illustrative purposes only and are not intended to limit the scope of protection of this utility model. In the drawings, the same reference numerals are used to refer to the same parts. Wherein: Figure 1 This is a schematic diagram of the structure of the present invention. Figure 1 ; Figure 2 This is a schematic diagram of the structure of the present invention. Figure 2 ; Figure 3 This is a partial structural schematic diagram of the present invention; Figure 4 This is a schematic diagram of the structure of the mixing component in this utility model; Figure 5 This is a schematic diagram of the connection of the mixing cavity in this utility model; Figure 6 This is a cross-sectional view of the mixing cavity in this utility model.

[0013] The diagram shows the following components: 1. Frame; 2. Feed tank; 3. Membrane filter; 31. Connecting pipe; 32. Microfiltration membrane filter; 33. Ultrafiltration membrane filter; 34. Nanofiltration membrane filter; 4. Booster pump; 41. Feed pipe; 5. Mixing assembly; 51. Mixing chamber; 511. Liquid inlet pipe; 512. Liquid outlet pipe; 52. Diverter pipe; 521. Branch pipe; 53. Aeration pump; 531. Pressure regulating valve; 54. Temperature sensor; 55. Pressure sensor; 56. Jet nozzle; 6. Controller. Detailed Implementation

[0014] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only a part of the embodiments of the present utility model, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of the present utility model without creative effort are within the scope of protection of the present utility model.

[0015] In the description of this utility model, it should be noted that the terms "upper," "lower," "vertical," "horizontal," "top," and "bottom," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0016] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model according to the specific circumstances.

[0017] Example like Figures 1 to 6 As shown, this utility model provides a multi-stage membrane separation and purification device for agricultural and forestry bioactive components, including a frame 1, multiple material tanks 2 arranged on the frame 1, multiple membrane filters 3 fixed on the frame 1, and a booster pump 4 installed on the frame 1. The frame 1 serves as the mounting foundation for the entire device, providing stable support for each functional component. The multiple material tanks 2 are arranged sequentially along the length of the frame 1, and are used to temporarily store different stages of the liquid to be processed or the separated products. Each membrane filter 3 is fixedly installed on the frame 1 and cooperates with its corresponding material tank 2. The booster pump 4 is installed at an appropriate position on the frame 1 to provide power for the liquid transport of the entire system, ensuring that the liquid can overcome pipeline resistance and membrane filtration resistance and flow smoothly.

[0018] Specifically, the clear liquid outlet of the membrane filter 3 is provided with a connecting pipe 31 extending into the corresponding material tank 2. During operation, the feed liquid flows through the membrane module under pressure. Small molecule target active ingredients (i.e., clear liquid) that can permeate the membrane pores are discharged through the clear liquid outlet and flow into the corresponding material tank 2 for temporary storage via the connecting pipe 31. The inlet of the booster pump 4 is connected to the outlet of the corresponding material tank 2 via the inlet pipe 41. The booster pump 4 extracts and pressurizes the feed liquid to be treated from the material tank 2 and then delivers it to the subsequent membrane filter 3 for separation and purification.

[0019] The device also includes a mixing component 5, which is located between the outlet of the booster pump 4 and the inlet of the membrane filter 3. It is used to mix the fresh feed liquid from the booster pump 4, the concentrated liquid returned after filtration by the membrane filter 3, and the inert gas supplied from the outside to form a uniform gas-liquid two-phase flow before sending it into the membrane filter 3, so as to improve the hydrodynamic conditions in the membrane filtration process and alleviate membrane fouling and concentration polarization.

[0020] The mixing assembly 5 includes a mixing chamber 51 and two branch pipes 52.

[0021] The mixing chamber 51 has a longitudinally arranged tubular structure with an internal cavity. Its lower end is connected to the outlet of the booster pump 4 via an inlet pipe 511, and its upper end is connected to the inlet of the membrane filter 3 via an outlet pipe 512. The internal cavity of the mixing chamber 51 provides ample mixing space for the feed liquid, concentrate, and inert gas. The feed liquid output from the booster pump 4 enters the mixing chamber 51 through the inlet pipe 511. After being fully mixed with the concentrate and inert gas in the mixing chamber 51, it is discharged from the outlet pipe 512 at the top of the mixing chamber 51 and sent to the membrane filter 3. The longitudinal design of the mixing chamber 51 allows the three fluids to have a longer mixing stroke in the direction of gravity, which is beneficial to improving the mixing uniformity.

[0022] The top ends of the two branch pipes 52 are spaced vertically apart, meaning they are arranged at different heights in the vertical direction within the mixing chamber 51, respectively for conveying concentrated liquid and inert gas. Each branch pipe 52 has at least two branch pipes 521 at its top end, with each branch pipe 521 extending tangentially to the wall of the mixing chamber 51. In other words, one end of each branch pipe 521 is connected to the branch pipe 52, and the other end passes through the wall of the mixing chamber 51 and extends into the internal cavity of the mixing chamber 51. The extension direction of the branch pipe 521 is tangentially inclined at a certain angle to the radial direction of the mixing chamber 51, causing the fluid entering the mixing chamber 51 through the branch pipe 521 to be ejected tangentially along the inner wall of the mixing chamber 51, thereby creating a swirling effect inside the mixing chamber 51. Each branch pipe 52 is provided with at least two branch pipes 521. The two branch pipes 521 are evenly distributed in the circumference of the mixing chamber 51. For example, when there are two branch pipes 521, they are symmetrically arranged on opposite sides of the mixing chamber 51, so that the fluid injected simultaneously through the two branch pipes 521 can form a symmetrical and stable swirling field after entering the mixing chamber 51, avoiding the deflection or unstable flow caused by unilateral inflow.

[0023] The bottom end of the top-mounted diversion pipe 52 is connected to the concentrate outlet of the membrane filter 3. During the filtration and separation of the feed liquid, large molecular impurities (including coarse fibers, large molecular proteins, polysaccharides, etc.) that cannot pass through the membrane pores, along with some unfiltered feed liquid, form a concentrate, which is discharged through the concentrate outlet of the membrane filter 3. This concentrate is transported via the top-mounted diversion pipe 52 to its branch pipes 521, and then tangentially fed into the mixing chamber 51 from each branch pipe 521. Because the diversion pipe 52 is located above the mixing chamber 51, and the branch pipes 521 extend tangentially into the mixing chamber 51, the concentrate flows tangentially along the inner wall of the mixing chamber 51 after entering the mixing chamber 51, forming a downward swirling flow. The concentrated liquid is refluxed back into the mixing chamber 51 and mixed with the fresh feed liquid before entering the membrane filter 3 for filtration. This can significantly improve the total recovery rate of the target active ingredient and reduce the loss of effective ingredients. At the same time, the reflux of the concentrated liquid increases the flow rate and velocity of the fluid in the mixing chamber 51 and subsequent pipelines, which is beneficial to increase the crossflow velocity on the membrane surface and delay membrane fouling.

[0024] An aeration pump 53 for conveying inert gas is fixedly connected to the bottom end of a branch pipe 52 located at the top. The aeration pump 53 is connected to an external gas tank (not shown in the figure) to pressurize the inert gas (preferably nitrogen to avoid oxidative damage to heat-sensitive or easily oxidized active ingredients) and send it into the branch pipe 52 located at the bottom. From there, the gas is delivered tangentially into the mixing chamber 51 through the branch pipes 521 of the branch pipe 52. Because the branch pipe 52 is located below the mixing chamber 51, and the branch pipes 521 extend tangentially into the mixing chamber 51, the inert gas flows tangentially along the inner wall of the mixing chamber 51 after entering, forming upward-swirling bubbles. The inert gas is dispersed in the liquid within the mixing chamber 51 in the form of microbubbles, forming a gas-liquid two-phase flow. When bubbles flow at high speed within the membrane tube, they exert a strong shearing and scouring effect on the membrane surface, effectively removing the filter cake layer deposited there. Simultaneously, the movement of the bubbles disrupts the concentration boundary layer on the membrane surface, breaking down concentration polarization, thereby increasing membrane filtration flux and extending the continuous operating time of the membrane module. Furthermore, the anaerobic environment created by the inert gas helps protect easily oxidized active ingredients, improving the quality of the final product.

[0025] like Figure 6As shown, branch pipes 521 located on different branch pipes 52 are arranged opposite each other in the axial direction of the mixing chamber 51. Specifically, the branch pipe 521 located on the upper branch pipe 52 (for conveying concentrated liquid) and the branch pipe 521 located on the lower branch pipe 52 (for conveying inert gas) are positioned vertically opposite each other in the axial direction of the mixing chamber 51. During operation, the concentrated liquid enters the mixing chamber 51 tangentially downward through the upper branch pipe 521, forming a downward swirling flow, while the inert gas enters the mixing chamber 51 tangentially upward through the lower branch pipe 521, forming upward swirling bubbles. The tangential injection directions of the branch pipes 521 located on different branch pipes 52 are opposite, and the two fluids meet in the middle region of the mixing chamber 51, forming opposing swirling flows. This counter-current swirling structure offers the following synergistic effects: First, the opposing swirling currents generate intense turbulence and shear force upon meeting, breaking large bubbles of inert gas into smaller ones, increasing the gas-liquid contact area and improving mixing efficiency. Second, the strong disturbance generated by the counter-current flow ensures rapid and uniform macroscopic mixing of the concentrate, feed solution, and inert gas, preventing excessively high local concentrations on the membrane surface due to uneven mixing. Third, the mixed gas and liquid phases flow uniformly into the membrane filter 3 via the outlet pipe 512, ensuring effective flushing and concentration reduction across the entire filtration cross-section, thus improving the stability and consistency of filtration efficiency. After thorough mixing in the mixing chamber 51, the feed solution, concentrate, and inert gas are sent to the membrane filter 3 via the outlet pipe 512 for membrane separation and purification.

[0026] Furthermore, the end of the branch pipe 521 extending into the inner cavity of the mixing chamber 51 is equipped with a jet nozzle 56. The jet nozzle 56 is a nozzle structure capable of ejecting fluid in the form of a high-speed jet. It has a gradually narrowing flow channel inside, causing the fluid velocity to increase sharply as it passes through the jet nozzle 56, thus being ejected into the mixing chamber 51 as a high-speed jet. The high-speed jet has greater kinetic energy and penetrating power, enabling it to more effectively impact and break up air bubbles, while simultaneously enhancing the stirring and mixing effect on the fluid. The angle between the axis of the jet nozzle 56 and the axis of the mixing chamber 51 is between 15° and 45°. This angle range is optimized: if the angle is less than 15°, the tangential component of the fluid is insufficient, making it difficult to form an effective swirling flow; if the angle is greater than 45°, the axial component of the fluid is too large, weakening the tangential swirling effect and hindering the formation of a stable swirling field within the mixing chamber 51. Preferably, the included angle is 30°. At this angle, the fluid has both sufficient tangential velocity to form a stable swirling flow and moderate axial velocity to ensure that the fluid has sufficient residence time in the mixing chamber 51 for thorough mixing, resulting in the optimal overall mixing effect.

[0027] Furthermore, both diverter pipes 52 are expanded diameter pipes, with the internal flow channel cross-sectional area of ​​the diverter pipe 52 being larger than that of the inlet pipe 511, and the internal flow channel cross-sectional area of ​​the inlet pipe 511 being smaller than that of the outlet pipe 512. This expanded diameter design of the diverter pipes 52 reduces the flow velocity and increases the pressure of the concentrated liquid and inert gas as they flow through them, facilitating a more stable entry of the two fluids into the mixing chamber 51 and reducing pulses and fluctuations caused by excessively high flow velocities. The cross-sectional area of ​​the inlet pipe 511 is smaller than that of the outlet pipe 512, which results in a higher flow velocity in the inlet pipe 511 under the condition that the output flow rate of the booster pump 4 is constant. This is beneficial for quickly sending the raw material liquid into the mixing chamber 51 to participate in the mixing. On the other hand, the cross-sectional area of ​​the outlet pipe 512 is larger, which results in the flow velocity of the mixed gas-liquid two-phase flow in the mixing chamber 51 being appropriately reduced and the pressure tending to be stable before entering the membrane filter 3. This avoids the fluid containing air bubbles impacting the membrane surface at an excessively high flow velocity, causing membrane damage. At the same time, it stabilizes the fluid state entering the membrane filter 3, which is beneficial for improving the stability and separation effect of membrane filtration.

[0028] Furthermore, a pressure regulating valve 531 is installed on the connecting pipe between the air outlet of the aeration pump 53 and the lower branch pipe 52. The pressure regulating valve 531 is used to regulate the pressure and flow rate of the inert gas delivered by the aeration pump 53 into the mixing chamber 51. By adjusting the opening of the pressure regulating valve 531, the operator can flexibly adjust the gas injection volume according to actual process requirements (such as feed concentration, membrane fouling degree, characteristics of target active ingredients, etc.) to optimize the enhancement effect of gas-liquid two-phase flow. The setting of the pressure regulating valve 531 makes the equipment have a wider range of process applications, and can flexibly adjust the optimal gas-liquid ratio for agricultural and forestry raw material extracts of different sources and properties to achieve a balance between optimal filtration effect and minimum energy consumption.

[0029] Furthermore, a pressure sensor 55 and / or a temperature sensor 54 are installed on the inner wall of the mixing chamber 51. A controller 6 is mounted on the frame 1, and the pressure sensor 55 and / or temperature sensor 54, as well as the booster pump 4, are connected to the controller 6. The pressure sensor 55 monitors the pressure inside the mixing chamber 51 in real time. This pressure value reflects the transmembrane pressure difference and membrane fouling degree of the membrane filter 3. When the pressure continues to rise, it indicates that membrane fouling is aggravated and membrane flux is reduced. The temperature sensor 54 monitors the temperature of the feed solution inside the mixing chamber 51 in real time. For heat-sensitive agricultural and forestry active ingredients, excessively high temperatures will cause the active ingredients to degrade and deteriorate, while excessively low temperatures will affect the flowability of the feed solution and the membrane filtration efficiency. The controller 6 adjusts the operating frequency of the booster pump 4 based on the feedback signals from the pressure sensor 55 and / or temperature sensor 54. Specifically, when pressure sensor 55 detects that the pressure inside mixing chamber 51 exceeds a preset threshold, controller 6 reduces the operating frequency of booster pump 4, decreasing the feed pressure and flow rate of membrane filter 3 to slow down membrane fouling, protect the membrane assembly from high pressure damage, and extend membrane lifespan by operating at low pressure. When the pressure is below the preset threshold, controller 6 can appropriately increase the operating frequency of booster pump 4 to maintain normal filtration flux. When temperature sensor 54 detects that the temperature inside mixing chamber 51 exceeds a preset range, controller 6 can reduce the heat input generated by high-speed pump operation by reducing the operating frequency of booster pump 4, thereby controlling the feed liquid temperature within a suitable range. Pressure sensor 55 and temperature sensor 54 can be set individually or both simultaneously. When both pressure sensor 55 and temperature sensor 54 are set simultaneously, controller 6 integrates the feedback signals from both to coordinately adjust booster pump 4, achieving optimal filtration efficiency while ensuring the activity of active ingredients.

[0030] In addition, the pipeline system composed of multiple membrane filters 3 is connected in series along the liquid flow direction, and the filtration pore size of each membrane filter 3 decreases progressively along the liquid flow direction, namely microfiltration membrane filter 32, ultrafiltration membrane filter 33, and nanofiltration membrane filter 34. Specifically, along the flow direction of the feed liquid, the first-stage membrane filter 3 is a microfiltration membrane filter 32, which has the largest membrane pore size and is used to intercept larger impurities such as coarse fibers, cell debris, and large particulate suspended matter in the feed liquid, while allowing small molecule active ingredients and large molecule proteins to pass through; the second-stage membrane filter 3 is an ultrafiltration membrane filter 33, whose membrane pore size is between that of microfiltration and nanofiltration, and is used to intercept medium-sized impurities such as large molecule proteins and polysaccharides, while allowing lower molecular weight target active ingredients (such as peptides, flavonoids, polyphenols, etc.) to pass through; the third-stage membrane filter 3 is a nanofiltration membrane filter 34, which has the smallest membrane pore size and is used to finely separate the feed liquid after the first two stages of filtration, further remove small molecule impurities, and achieve concentration and desalination of target active ingredients. Through the series gradient setting of the three-stage membrane filters 3, the clarified liquid from the previous stage membrane filter 3 enters the next stage feed tank 2, and is then drawn out by the next stage booster pump 4 and sent to the next stage membrane filter 3. The agricultural and forestry raw material extract can achieve simultaneous fractional separation and purification of target active ingredients within different molecular weight ranges in a single feeding process. The clarified liquid outlet of each stage membrane filter 3 is connected to the corresponding feed tank 2 via a connecting pipe 31, allowing the products obtained from each stage to be collected in different feed tanks 2 for convenient subsequent separate processing and utilization. Simultaneously, the multi-stage series membrane filters 3, combined with the reflux design of the mixing component 5, ensure that each stage membrane filter 3 operates under optimal feeding conditions, effectively controlling the fouling rate of each membrane module and significantly extending the continuous operating time of the entire equipment.

[0031] The technical scope of this utility model is not limited to the content described above. Those skilled in the art can make various modifications and variations to the above embodiments without departing from the technical concept of this utility model, and all such modifications and variations should fall within the protection scope of this utility model.

Claims

1. A multi-stage membrane separation and purification device for agricultural and forestry bioactive components, comprising a frame, multiple material tanks arranged on the frame, multiple membrane filters fixed on the frame, and a booster pump installed on the frame, wherein the clarified liquid outlet of each membrane filter is provided with a connecting pipe extending into the corresponding material tank, and the feed inlet of the booster pump is connected to the discharge outlet of the corresponding material tank through the feed pipe; characterized in that, It also includes a mixing component, the mixing component comprising: A mixing chamber, the mixing chamber being a longitudinally placed tubular structure, the lower end of which is connected to the outlet of the booster pump through an inlet pipe, and the upper end of which is connected to the inlet of the membrane filter through an outlet pipe; Two branch pipes are provided, with their top ends spaced apart vertically, and each has at least two branch pipes, all of which extend tangentially to the wall of the mixing chamber. The bottom end of the top-mounted diverter is connected to the concentrate outlet of the membrane filter, and the bottom end of the bottom-mounted diverter is fixedly connected to an aeration pump for conveying inert gas. The branch pipes located in different diverter pipes are arranged opposite to each other in the axial direction of the mixing chamber, and the tangential injection directions of the branch pipes located in different diverter pipes are opposite, so that the concentrate and inert gas form opposing swirling flows in the mixing chamber, so that the raw material liquid, concentrate and inert gas are mixed and then sent into the membrane filter through the outlet pipe.

2. The multi-stage membrane separation and purification equipment for agricultural and forestry bioactive components according to claim 1, characterized in that: The end of the branch pipe that extends into the inner cavity of the mixing chamber is provided with a jet nozzle, and the angle between the axis of the jet nozzle and the axis of the mixing chamber is 15° to 45°.

3. The multi-stage membrane separation and purification equipment for agricultural and forestry bioactive components according to claim 2, characterized in that: Both of the aforementioned diversion pipes are expansion pipes, and the cross-sectional area of ​​the internal flow channel of the diversion pipe is larger than that of the internal flow channel of the inlet pipe, while the cross-sectional area of ​​the internal flow channel of the inlet pipe is smaller than that of the internal flow channel of the outlet pipe.

4. The multi-stage membrane separation and purification equipment for agricultural and forestry bioactive components according to claim 1, characterized in that: A pressure regulating valve is provided on the connecting pipe between the air outlet of the aeration pump and the diversion pipe located at the bottom.

5. The multi-stage membrane separation and purification equipment for agricultural and forestry bioactive components according to claim 1, characterized in that: The inner wall of the mixing chamber is equipped with a pressure sensor and / or a temperature sensor, and a controller is mounted on the frame. The pressure sensor and / or temperature sensor, as well as the booster pump, are connected to the controller via signals. The controller adjusts the operating frequency of the booster pump based on the feedback signals from the pressure sensor and / or temperature sensor.

6. The multi-stage membrane separation and purification equipment for agricultural and forestry bioactive components according to claim 1, characterized in that: Multiple membrane filters are connected in series along the liquid flow direction, and the pore size of each membrane filter decreases progressively along the liquid flow direction, namely, microfiltration membrane filter, ultrafiltration membrane filter and nanofiltration membrane filter.

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