Device and method for rapid separation of molasses and protein in pea starch production wastewater

Abstract

This invention discloses a device and method for rapid separation of molasses and protein in pea starch production wastewater, belonging to the field of multi-stage wastewater treatment technology. It includes a multi-stage separation tank, which, from top to bottom, consists of a counter-current cyclone destabilization section, a microbubble cyclone separation section, and a gradient screening fine separation section. This invention coaxially integrates the three core processes of destabilization, pre-separation, and fine separation into a single multi-stage separation tank, eliminating redundant intermediate pipelines and external equipment. The total residence time for the entire process is only 5-8 seconds, improving the processing cycle by two orders of magnitude compared to the traditional 3-8 hour process. It truly achieves continuous feeding and continuous discharging, eliminating inefficient processes such as intermittent sedimentation and settling. Simultaneously, the integrated design reduces the equipment footprint to only 1 / 5 of that of traditional processes, significantly reducing the civil engineering investment and site requirements of the production line. It can be flexibly adapted to pea starch production lines of different sizes through parallel expansion, exhibiting extremely high adaptability.

Description

Technical Field

[0001] This invention relates to the field of multi-stage wastewater treatment technology, specifically to a device and method for rapid separation of molasses and protein in pea starch production wastewater. Background Technology

[0002] Pea starch is an important agricultural product for intensive processing. Due to its excellent gelling, film-forming, and texture properties, it is widely used in vermicelli, snack foods, food additives, and pharmaceutical excipients. The pea starch processing industry has maintained steady growth for many years. During the wet processing of pea starch, a large amount of yellow slurry wastewater is generated. This wastewater has a solid content of 1.5%-3% and is rich in high-value-added soluble pea protein and molasses (monosaccharides, disaccharides, and oligosaccharides), while also containing small amounts of colloids and suspended solids. Its COD concentration is as high as 15,000-30,000 mg / L. Direct discharge of this wastewater would cause serious water pollution and resource waste.

[0003] Currently, the industry's treatment of pea starch slurry wastewater still focuses on achieving emission standards. Technical solutions that simultaneously recover protein and molasses resources have many insurmountable drawbacks. The mainstream technical routes are as follows: (1) Flocculation sedimentation isoelectric point sedimentation process: This is the mainstream treatment process in the industry. The pH of the wastewater is adjusted to the isoelectric point of the protein by acid and alkali, or flocculants and coagulants are added to destabilize and precipitate the protein colloids. The solid and liquid are then separated by sedimentation tank, and the clear liquid is subsequently treated by biochemical treatment to meet the discharge standards. This process has the following core defects: First, the large amount of acid, alkali and reagents used not only increases the treatment cost, but also results in the presence of reagent residues in the recovered protein, which cannot meet the food / feed grade standards and can only be disposed of as low-end solid waste. Honey is also largely adsorbed by the protein flocs, with a recovery rate of less than 40% and extremely low resource value. Second, the sedimentation process has a long residence time of 3-8 hours, the equipment occupies a large area, the treatment efficiency is extremely low, and continuous and stable operation cannot be achieved. Third, a large amount of soluble small molecule protein remains in the clear liquid after sedimentation, resulting in a very high load on subsequent biochemical treatment and high environmental treatment costs.

[0004] (2) Dissolved air flotation separation process: As an alternative to sedimentation process, microbubbles are generated by pressurized dissolved air system to adsorb protein flocs and float to achieve solid-liquid separation. Although this process shortens the processing cycle, there are still unresolved pain points: First, the bubbles generated by traditional dissolved air flotation are uneven in size and have serious turbulence. The adsorption efficiency between bubbles and proteins is less than 70%, and the floating foam will carry a large amount of molasses liquid phase, resulting in low purity of protein and molasses separation and high molasses loss rate; Second, it requires a large supporting pressurized dissolved air, release and sludge scraping system, which has large equipment investment and high energy consumption. Moreover, the release device is easily blocked by protein colloids, resulting in poor stability of continuous operation; Third, it is still necessary to add reagents in advance to achieve protein destabilization, which cannot fundamentally solve the problems of reagent pollution and limited resource utilization.

[0005] (3) Membrane separation process: Existing research uses ultrafiltration and nanofiltration membrane technology to separate proteins and molasses through pore size sieving, which can theoretically achieve high separation accuracy. However, this process has fatal flaws in industrial applications: First, static membranes are very easy to clog. Protein colloids and suspended solids in wastewater will quickly form a filter cake layer on the membrane surface, causing the membrane flux to decrease by more than 50% within 1-3 days. Frequent chemical cleaning with acids, alkalis and oxidants is required, which not only greatly shortens the service life of the membrane, but also generates secondary pollution. Second, the operating energy consumption is extremely high. High pressure feeding and high flow rate cross-flow operation are required. The energy consumption per unit treatment volume is 3-5 times that of traditional processes. Third, the requirements for feed pretreatment are extremely high. It cannot directly treat the raw wastewater. It must be equipped with pretreatment systems such as sedimentation and flotation. The overall investment cost is high and it is difficult to adapt to large-scale industrial production lines.

[0006] (4) Centrifugal separation process: Disc centrifuges and other equipment are used to separate protein flocs from the liquid phase by centrifugal force. This process can only effectively separate large protein flocs. The separation efficiency of soluble small molecule proteins and colloidal proteins, which account for a very high proportion in wastewater, is less than 60%, and it cannot achieve precise classification of proteins and molasses. At the same time, the equipment investment is extremely high, the single machine processing capacity is limited, and it still requires the addition of chemicals in advance to break down the stabilization, which cannot meet the needs of continuous industrial production.

[0007] In summary, existing pea starch wastewater treatment technologies all share common core defects: they cannot achieve chemical-free, fully physical separation, they struggle to balance separation efficiency, separation purity, and operational stability, and they cannot simultaneously achieve high-value recovery of protein and molasses. Most of them remain at the level of "wastewater treatment meeting standards," resulting in serious resource waste and environmental pressure. Summary of the Invention

[0008] The purpose of this invention is to solve the above-mentioned problems by providing a device and method for rapid separation of molasses and protein in pea starch production wastewater.

[0009] To achieve the above objectives, the present invention specifically adopts the following technical solution: A rapid separation device for molasses and protein in pea starch production wastewater includes a multi-stage separation tank, which consists of a counter-current cyclone breaking section, a microbubble cyclone separation section and a gradient sieving fine separation section from top to bottom. The inner top of the counter-current vortex destabilization section is provided with a double tangential counter-current liquid inlet pipe. The counter-current vortex destabilization section is a cone-shaped structure that is wider at the top and narrower at the bottom, and the inner wall is provided with several vortex guide vanes in a ring shape. The microbubble cyclone separation section is equipped with a conical cyclone tube that is wider at the top and narrower at the bottom. A pressure-stabilizing gas chamber is arranged on the outer side of the conical cyclone tube. Tangential and co-directional spray holes are arranged in a ring on the inner wall of the conical cyclone tube. The tangential and co-directional spray holes are connected to the pressure-stabilizing gas chamber. An air inlet pipe is arranged on the outer side of the pressure-stabilizing gas chamber. A protein concentrated phase guide pipe is arranged in the middle of the conical cyclone tube. The gradient screening and fine separation section is equipped with three layers of conical gradient screens that are wider at the top and narrower at the bottom, and a self-driving component. The aperture of the three layers of conical gradient screens decreases from top to bottom. The self-driving component uses the swirling flow above to drive the three layers of conical gradient screens to rotate.

[0010] Furthermore, connecting chambers are provided between the counter-current stabilization section and the microbubble cyclone separation section, and between the microbubble cyclone separation section and the gradient sieving fine separation section.

[0011] Furthermore, a swirling tube is annularly arranged at the bottom of the connecting chamber.

[0012] Furthermore, the gradient screening fine separation section is provided with a separation chamber and three sewage discharge chambers. The conical gradient screen is located in the separation chamber, and the three sewage discharge chambers are distributed outside the separation chamber and are all connected to the separation chamber through sewage discharge ports. The inner bottom of the sewage discharge ports is flush with the upper surface of the conical gradient screen.

[0013] Furthermore, the self-driving assembly includes a self-driving shaft rotatably mounted in the center of the separation chamber, a turbine drive impeller fixedly mounted at the top of the self-driving shaft, and the conical gradient screen fixedly mounted on the self-driving shaft.

[0014] Furthermore, the separation chamber is equipped with three sets of lifting conical liquid control hoppers, which are correspondingly arranged above three layers of conical gradient screens. The cone angle of the conical liquid control hopper is larger than that of the conical gradient screen. A liquid outlet is opened at the center of the conical liquid control hopper, and a sealing plate is set at the center of the conical gradient screen to seal the liquid outlet. A baffle ring is set at the top of the conical liquid control hopper, and the height of the baffle ring is greater than the height of the drain outlet. The bottom of the separation chamber is funnel-shaped and has a honey clear liquid outlet pipe. A sludge collection chamber is set at the bottom of the lowest sludge discharge chamber, and a sludge discharge pipe is set at the bottom of the sludge collection chamber. The three sludge discharge chambers are connected to the sludge collection chamber through three conduits. A flow meter is set at the outlet of the conduit, and the flow meter is electrically connected to the plant control system. The lifting and lowering of the conical liquid control hopper is controlled by judging the flow of the conduit.

[0015] Furthermore, a sealing chassis is provided at the bottom end of the self-driving shaft. The sealing chassis is rotatably and sealed at the bottom of the separation chamber. Three sets of lifting hydraulic cylinders are fixedly installed at the bottom of the sealing chassis. An inner support ring is provided inside the liquid inlet. The three inner support rings are staggered. The telescopic ends of the three sets of lifting hydraulic cylinders are respectively connected to the three inner support rings.

[0016] Furthermore, the bottom of the sewage discharge chamber is conical and has a structure that is narrower at the top and wider at the bottom.

[0017] Furthermore, the self-driving shaft has a hollow internal design and an inner tube rod is rotatably mounted inside. Three sets of flushing and recovery ports are opened on the outside of the self-driving shaft, and the flushing and recovery ports are respectively located directly above the corresponding sealing discs. A flushing auxiliary pipe is provided between the self-driving shaft and the conical liquid control hopper. A flushing and recovery inner port is opened on the outside of the inner tube rod. The flushing and recovery inner port and the flushing and recovery outer port are correspondingly arranged and can be staggered. A flushing main pipe is provided inside the inner tube rod. The flushing main pipe and the flushing auxiliary pipe are correspondingly arranged and can be staggered.

[0018] A rapid method for separating molasses and protein from pea starch production wastewater includes the following steps: S1. Wastewater enters the counter-current destabilization section from the top double-tangential counter-current inlet pipe. Through the vortex field of the counter-current and the gradually changing flow channel, a controllable high-frequency shear microturbulence is generated, which only destroys the stable double electric layer structure of the protein colloid, causing it to destabilize and aggregate to form 10-50μm micron-sized protein flocs. S2. After destabilization, the wastewater enters the microbubble cyclone separation section in a swirling state. Simultaneously, compressed air enters the pressure stabilizing chamber through the air inlet pipe and then enters the conical cyclone cylinder through tangential and unidirectional nozzles. Under the shearing action of the cyclone liquid, uniform microbubbles of 10-50μm are generated in situ. The bubbles and the cyclone liquid flow in the same direction, without radial impact, and do not disrupt the stability of the cyclone field. The destabilized protein flocs are highly hydrophobic and are instantly adsorbed upon collision with the microbubbles, forming a "gas-protein floc complex" with a density much lower than that of the liquid phase. Under the action of the cyclone centrifugal field, the low-density complex rapidly accumulates towards the central axis of the cylinder, forming a continuous concentrated protein phase column. The concentrated protein phase guide pipe generates negative pressure to discharge the concentrated protein phase, achieving efficient pre-separation of proteins. Meanwhile, honey, being a highly hydrophilic small molecule, is not adsorbed by the microbubbles and remains in the liquid phase. It is thrown towards the cylinder wall by the cyclone field, forming a circumferential honey liquid phase layer, which flows downward along the conical wall into the gradient sieving fine separation section, completing the pre-separation. S3. The pre-separated honey liquid phase enters the gradient sieving fine separation section, and is sieved through three layers of conical gradient screens. The high-speed rotating conical gradient screens form a dynamic sieving interface. The protein impurities trapped are thrown upwards along the conical screen surface to the cylinder wall under the action of centrifugal force. The bottom 100nm conical gradient screen achieves precise separation of protein and honey, completely trapping all residual protein and allowing only small honey molecules to pass through. Finally, the purity of the honey clear liquid is ≥98%, and the protein residue is ≤0.1%.

[0019] The beneficial effects of this invention are as follows: This invention utilizes the synergistic cooperation of a dual-tangential counter-current inlet pipe and a conical, gradually varying vortex guide vane in a counter-current destabilization section. Through the reverse counter-current vortex, a controllable high-frequency shear micro-turbulence is formed, disrupting only the stable double-layer structure of the protein colloid, causing it to destabilize and aggregate into micron-sized flocs. The entire process involves no addition of acids, alkalis, flocculants, or other chemicals, significantly reducing the cost of chemical procurement and treatment. More importantly, it completely preserves the primary structure of the protein molecules and the original quality of the molasses. The separated protein and molasses have no chemical residues and can be directly used in high-value-added fields such as food, feed, and fermentation raw materials. This truly realizes the resource utilization of pea starch wastewater, rather than simply achieving standard treatment, and completely solves the core problem of low resource value caused by chemical residues in traditional processes.

[0020] This invention integrates the three core processes of stabilization, pre-separation, and fine separation coaxially into a single multi-stage separation tank from top to bottom. There are no redundant intermediate pipelines or external equipment. The total residence time of the entire process is only 5-8 seconds, which is two orders of magnitude faster than the traditional process of 3-8 hours. It truly achieves continuous feeding and continuous discharge, eliminating inefficient processes such as intermittent sedimentation and settling. At the same time, the integrated design reduces the equipment footprint to only 1 / 5 of that of the traditional process, significantly reducing the civil engineering investment and site requirements of the production line. It can be flexibly adapted to pea starch production lines of different sizes through parallel expansion, making it highly adaptable.

[0021] This invention utilizes three sets of liftable conical liquid control hoppers, each corresponding to a three-layer conical gradient screen. Combined with a flow meter on the discharge chamber guide tube providing real-time feedback on the discharge flow rate, the height of the conical liquid control hoppers can be precisely adjusted via a lifting hydraulic cylinder. This, in turn, regulates the discharge space and screening pressure above the screen. The device can adaptively adjust the screening conditions in real-time based on influent concentration and water quality fluctuations, enabling it to stably adapt to pea starch wastewater of varying concentrations and qualities. This avoids problems such as decreased screening efficiency and screen clogging caused by water quality fluctuations. Simultaneously, the conical liquid control hoppers precisely guide wastewater to the center of the screen, ensuring uniform diffusion and screening under centrifugal force. This prevents resource waste caused by unfiltered wastewater being directly discharged into the discharge port, further improving the recovery rate of protein and molasses, and ensuring the stability and reliability of the three-layer grading screening. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the overall structure of the separation device of the present invention; Figure 2 This is a cross-sectional view of the separation device of the present invention; Figure 3 This is a schematic diagram of the internal structure of the counter-swirling destabilization section of the present invention; Figure 4 This is a schematic cross-sectional view of the anti-swirl destabilization section of the present invention; Figure 5 This is a schematic cross-sectional view of the microbubble swirl sorting section of the present invention; Figure 6 This is a schematic cross-sectional view of the gradient sieving and fine separation section of the present invention; Figure 7 This is a schematic diagram of the self-driven component structure of the present invention; Figure 8 This is a schematic diagram of the self-cleaning conical gradient screen of the present invention.

[0023] Figure reference numerals: 1. Counter-current cyclone destabilization section; 11. Double tangential counter-current liquid inlet pipe; 12. Vortex guide vane; 2. Microbubble cyclone separation section; 21. Conical cyclone cylinder; 22. Pressure stabilizing gas chamber; 23. Tangential co-directional nozzle; 24. Air inlet pipe; 25. Protein concentrated phase guide pipe; 3. Gradient sieving fine separation section; 31. Separation chamber; 32. Sewage discharge chamber; 33. Sewage outlet; 34. Sewage collection chamber; 35. Sewage pipe 36. Conduit; 37. Flow meter; 38. Honey liquid outlet pipe; 4. Connecting chamber; 41. Swirl pipe; 5. Self-driving shaft; 51. Sealed chassis; 52. Lifting hydraulic cylinder; 53. Flushing recovery outer port; 54. Flushing secondary pipe; 6. Turbine drive impeller; 7. Conical gradient screen; 8. Conical liquid control hopper; 81. Inner support ring; 9. Inner tube rod; 91. Flushing recovery inner port; 92. Flushing main pipe. Detailed Implementation

[0024] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings.

[0025] Example 1, as Figures 1-8 As shown, the rapid separation device for molasses and protein in pea starch production wastewater includes a multi-stage separation tank, which consists of a counter-current cyclone breaking section 1, a microbubble cyclone separation section 2, and a gradient screening fine separation section 3 from top to bottom. The inner top of the counter-current vortex destabilization section 1 is provided with a double tangential counter-current liquid inlet pipe 11. The counter-current vortex destabilization section 1 is a cone-shaped structure that is wider at the top and narrower at the bottom, and several vortex guide vanes 12 are arranged in a ring on the inner wall. The microbubble cyclone separation section 2 is equipped with a conical cyclone tube 21 that is wider at the top and narrower at the bottom. A pressure-stabilizing gas chamber 22 is provided on the outer side of the conical cyclone tube 21. Tangential and unidirectional nozzles 23 are arranged in a ring on the inner wall of the conical cyclone tube 21. The tangential and unidirectional nozzles 23 are connected to the pressure-stabilizing gas chamber 22. An air inlet pipe 24 is provided on the outer side of the pressure-stabilizing gas chamber 22. A protein concentrated phase guide pipe 25 is provided in the middle of the conical cyclone tube 21. The gradient screening and fine separation section 3 is equipped with a three-layer conical gradient screen 7 that is wider at the top and narrower at the bottom, and a self-driving component. The aperture of the three-layer conical gradient screen 7 decreases from top to bottom. The self-driving component uses the swirling flow above to drive the three-layer conical gradient screen 7 to rotate.

[0026] Working principle: The two feed inlets of the dual tangential counter-current inlet pipe 11 are symmetrically arranged radially along the cylinder, with completely opposite tangential feed directions. The ratio of the inlet diameter to the cylinder diameter of the counter-current vortex destabilization section 1 is 1:8, forming a counter-current vortex field, which completely solves the problems of velocity attenuation and turbulent flow in unidirectional vortex flow. Inside the cylinder of the counter-current vortex destabilization section 1, six spiral vortex guide vanes 12 are coaxially installed, evenly distributed at 60° circumferentially along the central axis of the cylinder, ensuring complete circumferential symmetry of the flow channel and no flow deviation. The vortex guide vanes 12 are also conically distributed, forming a gradually changing flow channel. Through the vortex field of the counter-current vortex and the gradually changing flow channel, controllable high-frequency shear microturbulence is generated, which only destroys the stable double electric layer structure of the protein colloid, causing it to destabilize and aggregate to form micron-sized protein flocs of 10-50μm.

[0027] After destabilization, the wastewater enters the microbubble vortex sorting section 2 in a swirling state. Simultaneously, compressed air enters the pressure stabilizing chamber 22 through the air inlet pipe 24, and then enters the conical vortex cylinder 21 through the tangential unidirectional nozzle 23. Under the shearing action of the swirling liquid, uniform microbubbles of 10-50 μm are generated in situ. The bubbles and the swirling liquid flow in the same direction, without radial impact, thus not disrupting the stability of the swirling field. The destabilized protein flocs are highly hydrophobic and are instantly adsorbed upon collision with the microbubbles, forming a "gas-protein floc" reaction. The protein-rich complex has a density much lower than that of the liquid phase. Under the action of the swirling centrifugal field, the low-density complex rapidly accumulates towards the central axis of the cylinder, forming a continuous concentrated protein column. The concentrated protein flow tube 25 generates negative pressure, discharging the concentrated protein phase and achieving efficient pre-separation of the protein. Meanwhile, honey, being a strongly hydrophilic small molecule, is not adsorbed by microbubbles and remains in the liquid phase. It is thrown towards the cylinder wall by the swirling field, forming a circumferential honey liquid phase layer, which flows downward along the cone wall into the gradient sieving fine separation section 3, completing the pre-separation.

[0028] After pre-separation, the honey liquid phase enters the gradient sieving fine separation section 3, and is sieved through three layers of conical gradient screens 7. The high-speed rotating conical gradient screens 7 form a dynamic sieving interface. The protein impurities trapped are thrown upwards along the conical screen surface towards the cylinder wall under the action of centrifugal force. The bottom 100nm conical gradient screens 7 achieve precise separation of protein and honey, completely trapping all residual protein. The three-layer conical gradient screen 7 is made of 316L stainless steel laser-drilled sintered mesh. The conical structure has the large end facing up and the small end facing down, with a cone angle of 15°. The aperture of the three layers of screen decreases from top to bottom: the upper layer is 5μm (retaining large particles and flocs), the middle layer is 1μm (retaining colloidal impurities), and the bottom layer is 100nm (retaining proteins with a molecular weight ≥10kDa, while allowing complete passage of small molecules such as honey with a molecular weight ≤1kDa). The retained protein impurities are thrown upwards along the conical screen surface towards the cylinder wall under the action of centrifugal force, and cannot be deposited and scaled on the screen surface at all, thus solving the membrane clogging problem at its root. The self-driving component is driven by the swirling residual pressure, which drives the high-speed rotation of the conical gradient screen 7 without the need for additional power.

[0029] Example 2, based on the above examples, further includes connecting chambers 4 between the counter-current stabilization section 1 and the microbubble cyclone separation section 2, and between the microbubble cyclone separation section 2 and the gradient screening fine separation section 3.

[0030] Furthermore, a swirling tube 41 is annularly arranged at the bottom of the connecting chamber 4.

[0031] The connecting chamber 4 acts as a buffer for the sewage, and the buffered sewage is discharged in a spiral manner through the vortex tube 41, forming a more uniform and stable vortex liquid, thereby improving the treatment effect.

[0032] Example 3, based on the above examples, further includes a separation chamber 31 and three sewage discharge chambers 32 inside the gradient screening fine separation section 3. The conical gradient screen 7 is located in the separation chamber 31, and the three sewage discharge chambers 32 are distributed outside the separation chamber 31 and are all connected to the separation chamber 31 through sewage discharge ports 33. The inner bottom of the sewage discharge ports 33 is flush with the upper surface of the conical gradient screen 7.

[0033] The self-driven assembly includes a self-driven shaft 5 rotatably mounted in the center of the separation chamber 31, a turbine drive impeller 6 fixedly mounted on the top of the self-driven shaft 5, and a conical gradient screen 7 fixedly mounted on the self-driven shaft 5.

[0034] The separation chamber 31 is equipped with three sets of retractable conical liquid control hoppers 8. These three sets of conical liquid control hoppers 8 are correspondingly positioned above three layers of conical gradient screens 7. The cone angle of each conical liquid control hopper 8 is greater than that of the conical gradient screen 7. A liquid outlet is located at the center of each conical liquid control hopper 8. A sealing disc is located at the center of each conical gradient screen 7 to block the liquid outlet. A baffle ring is located at the top of each conical liquid control hopper 8, with a height greater than that of the drain outlet. At a height of 33, the bottom of the separation chamber 31 is funnel-shaped and has a honey liquid outlet pipe 38 at the bottom. The bottom of the lowest sewage discharge chamber 32 has a sewage collection chamber 34, and the bottom of the sewage collection chamber 34 has a sewage discharge pipe 35. The three sewage discharge chambers 32 are connected to the sewage collection chamber 34 through three conduits 36. The outlet of the conduit 36 ​​is equipped with a flow meter 37, which is electrically connected to the plant control system. The flow of the conduit 36 ​​is used to control the raising and lowering of the conical liquid control hopper 8.

[0035] A sealing chassis 51 is provided at the bottom of the self-drive shaft 5. The sealing chassis 51 is rotary sealed and installed at the bottom of the separation chamber 31. Three sets of lifting hydraulic cylinders 52 are fixedly installed at the bottom of the sealing chassis 51. An inner support ring 81 is provided inside the liquid passage. The three inner support rings 81 are staggered. The telescopic ends of the three sets of lifting hydraulic cylinders 52 are respectively connected to the three inner support rings 81.

[0036] The bottom of the sewage discharge chamber 32 is tapered and has a narrow top and wide bottom structure, which improves the sewage discharge effect.

[0037] The swirling liquid above is driven by a turbine to rotate an impeller 6, which in turn drives a self-driven shaft 5. The self-driven shaft 5 then drives a sealed chassis 51, which in turn drives a lifting hydraulic cylinder 52 to rotate a conical liquid control hopper 8. Simultaneously, the self-driven shaft 5 drives a conical gradient screen 7 to rotate. The conical gradient screen 7 and the conical liquid control hopper 8 rotate synchronously. Wastewater first enters the uppermost conical liquid control hopper 8, then falls through the liquid outlet into the middle of the conical gradient screen 7. Under centrifugal force, the wastewater diffuses outward and is filtered through the conical gradient screen 7. The wastewater passes through three conical gradient screens 7 and conical liquid control hoppers 8 in sequence. If the wastewater concentration is high, the conical gradient screens... Excessive filtration pressure on the screen 7 will cause more wastewater to be thrown to the drain outlet 33 under centrifugal force. The wastewater enters the drain chamber 32 through the drain outlet 33 and is discharged into the collection chamber 34 through the conduit 36. The flow meter 37 provides feedback on the wastewater flow rate. At this time, the corresponding lifting hydraulic cylinder 52 is controlled to operate. The lifting hydraulic cylinder 52 drives the corresponding conical liquid control hopper 8 to descend. The conical liquid control hopper 8 adjusts the throwing space above the conical gradient screen 7 to reduce wastewater discharge and generate greater pressure between the conical liquid control hopper 8 and the conical gradient screen 7, thereby improving the wastewater filtration efficiency. By adjusting the throwing space, the device can be adapted to filter wastewater of different concentrations.

[0038] By setting the conical liquid control hopper 8, this invention can not only guide the sewage to the middle and prevent the sewage filtered above from being directly thrown to the drain outlet 33, making the three-layer filtration more stable, but also block the drain outlet 33 through the setting of the baffle ring, achieving the effect of stable control of the thrown space.

[0039] Example 4, based on the above examples, further includes a hollow internal design for the self-driving shaft 5, with an inner tube rod 9 rotatably mounted inside. Three sets of flushing and recovery external ports 53 are opened on the outer side of the self-driving shaft 5, with each flushing and recovery external port 53 located directly above the corresponding sealing disc. A flushing secondary pipe 54 is provided between the self-driving shaft 5 and the conical liquid control hopper 8. A flushing and recovery inner port 91 is opened on the outer side of the inner tube rod 9, with the flushing and recovery inner port 91 corresponding to and offset from the flushing and recovery external ports 53. A flushing main pipe 92 is provided inside the inner tube rod 9, with the flushing main pipe 92 corresponding to and offset from the flushing secondary pipe 54.

[0040] Because the conical gradient screen 7 has three layers, conventional backwashing is difficult and it is easy for contamination to occur at both the top and bottom.

[0041] Therefore, through the setup of this embodiment, when backwashing of the conical gradient screen 7 is required, the conical liquid control hopper 8 is controlled to rise, with the lower conical liquid control hopper 8 pressing against the bottom of the upper conical gradient screen 7. The sealing plate seals the liquid outlet. Since the cone angle of the conical liquid control hopper 8 is greater than that of the conical gradient screen 7, and a retaining ring is provided, a flushing space is formed between the conical liquid control hopper 8 and the upper conical gradient screen 7. Then, the inner tube rod 9 is rotated so that the flushing recovery inner port 91 and the flushing recovery outer port 53 are connected, and the flushing main pipe 92 and the flushing secondary pipe 54 are connected. At this time, the flushing water enters the flushing space through the flushing main pipe 92 and the flushing secondary pipe 54, and the flushing water backwashes the conical gradient screen 7. The flushing wastewater enters the inner tube rod 9 through the flushing recovery inner port 91 and the flushing recovery outer port 53, and is discharged through the inner tube rod 9, realizing one-time isolation backwashing of the three-layer conical gradient screen 7. The flushing is simple and will not cause cross-contamination. (See attached...) Figure 8 As shown.

[0042] Example 5: A method for rapid separation of molasses and protein in pea starch production wastewater, comprising the following steps: S1. Wastewater enters the counter-current destabilization section 1 from the uppermost double-tangential counter-current inlet pipe 11. Through the vortex field of the counter-current vortex and the gradually changing flow channel, a controllable high-frequency shear microturbulence is generated, which only destroys the stable double electric layer structure of the protein colloid, causing it to destabilize and aggregate to form micron-sized protein flocs of 10-50μm. S2. The destabilized wastewater enters the microbubble vortex sorting section 2 in a swirling state. Simultaneously, compressed air enters the pressure stabilizing chamber 22 through the air inlet pipe 24, and then enters the conical vortex cylinder 21 through the tangential and unidirectional nozzles 23. Under the shearing action of the swirling liquid, uniform microbubbles of 10-50 μm are generated in situ. The bubbles and the swirling liquid flow in the same direction, without radial impact, and do not disrupt the stability of the swirling field. The destabilized protein flocs have strong hydrophobicity and are instantly adsorbed after colliding with the microbubbles, forming a "gas and protein" interaction. The "floc complex" has a density much lower than that of the liquid phase. Under the action of the swirling centrifugal field, the low-density complex rapidly accumulates towards the central axis of the cylinder, forming a continuous concentrated protein column. The concentrated protein flow tube 25 generates negative pressure, discharging the concentrated protein phase and achieving efficient pre-separation of the protein. Meanwhile, honey, being a strongly hydrophilic small molecule, is not adsorbed by microbubbles and remains in the liquid phase. It is thrown towards the cylinder wall by the swirling field, forming a circumferential honey liquid phase layer, which flows downward along the cone wall into the gradient sieving fine separation section 3, completing the pre-separation. S3. The pre-separated honey liquid phase enters the gradient sieving fine separation section 3. After being sieved through three layers of conical gradient screens 7, the high-speed rotating conical gradient screens 7 form a dynamic sieving interface. The protein impurities trapped are thrown upwards along the conical screen surface to the cylinder wall under the action of centrifugal force. The bottom 100nm conical gradient screen 7 achieves precise separation of protein and honey, completely trapping all residual protein and allowing only small honey molecules to pass through. Finally, the purity of the honey clear liquid is ≥98%, and the protein residue is ≤0.1%.

[0043] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A device for rapid separation of honey sugar and protein in pea starch production wastewater, comprising a multi-stage separation tank, characterized in that, The multi-stage separation tank is composed of a counter-rotating flow de-stabilization section (1), a micro-bubble cyclone separation section (2) and a gradient screen fine separation section (3) from top to bottom. The counter-rotating flow de-stabilization section (1) is provided with a double-tangential counter-rotating liquid inlet pipe (11) at the top, and is provided with a tapering shape from wide top to narrow bottom, and the inner wall is annularly provided with a plurality of vortex guide vanes (12). The micro-bubble cyclone separation section (2) is internally provided with a tapering cyclone cylinder (21) with a wide top and a narrow bottom, and the outer side of the tapering cyclone cylinder (21) is provided with a pressure stabilization chamber (22), the inner wall of the tapering cyclone cylinder (21) is annularly provided with tangential and same-direction nozzles (23), the tangential and same-direction nozzles (23) are in communication with the pressure stabilization chamber (22), the outer side of the pressure stabilization chamber (22) is provided with an air inlet pipe (24), and the tapering cyclone cylinder (21) is provided with a protein dense phase guide pipe (25) in the middle. The gradient screen fine separation section (3) is internally provided with a three-layer tapering gradient screen (7) with a wide top and a narrow bottom and a self-driving assembly, the pore size of the three-layer tapering gradient screen (7) decreases from top to bottom, and the self-driving assembly drives the three-layer tapering gradient screen (7) to rotate by using the cyclone above.

2. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 1, characterized in that, The counter-rotating flow de-stabilization section (1) and the micro-bubble cyclone separation section (2) are provided with a connecting chamber (4) between them, and the micro-bubble cyclone separation section (2) and the gradient screen fine separation section (3) are provided with a connecting chamber (4) between them.

3. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 2, characterized in that, The bottom of the connecting chamber (4) is annularly provided with a cyclone pipe (41).

4. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 1, characterized in that, The gradient screen fine separation section (3) is internally provided with a separation chamber (31) and three sewage chambers (32), the tapering gradient screen (7) is located in the separation chamber (31), the three sewage chambers (32) are distributed on the outer side of the separation chamber (31), and are in communication with the separation chamber (31) through sewage outlets (33), and the inner bottom of the sewage outlet (33) is flush with the upper surface of the tapering gradient screen (7).

5. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 4, characterized in that, The self-driving assembly comprises a self-driving shaft (5) rotationally installed in the middle of the separation chamber (31), and a turbine driving impeller (6) fixedly installed at the top end of the self-driving shaft (5), and the tapering gradient screen (7) is fixedly installed on the self-driving shaft (5).

6. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 5, characterized in that, The separation chamber (31) is equipped with three sets of lifting conical liquid control hoppers (8). The three sets of conical liquid control hoppers (8) are correspondingly arranged with three layers of conical gradient screens (7) and are located above the corresponding conical gradient screens (7). The cone angle of the conical liquid control hopper (8) is greater than the cone angle of the conical gradient screen (7). A liquid outlet is opened at the center of the conical liquid control hopper (8). A sealing plate is set at the center of the conical gradient screen (7) to seal the liquid outlet. A baffle ring is set at the top of the conical liquid control hopper (8). The height of the baffle ring is greater than that of the drain outlet (33). The bottom of the separation chamber (31) is funnel-shaped and has a honey liquid outlet pipe (38) at the bottom. The bottom of the lowest sewage chamber (32) has a sewage collection chamber (34) and a sewage discharge pipe (35) at the bottom. The three sewage chambers (32) are connected to the sewage collection chamber (34) through three conduits (36). A flow meter (37) is installed at the outlet of the conduit (36). The flow meter (37) is electrically connected to the plant control system. The conical liquid control bucket (8) is raised and lowered by judging the flow of the conduit (36).

7. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 6, characterized in that, The bottom end of the self-driving shaft (5) is provided with a sealing chassis (51). The sealing chassis (51) is rotatably sealed and installed at the bottom of the separation chamber (31). Three sets of lifting hydraulic cylinders (52) are fixedly installed at the bottom of the sealing chassis (51). The inside of the liquid passage is provided with an inner support ring (81). The three inner support rings (81) are staggered. The telescopic ends of the three sets of lifting hydraulic cylinders (52) are respectively connected to the three inner support rings (81).

8. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 7, characterized in that, The bottom of the sewage discharge chamber (32) is conical and has a narrow top and wide bottom structure.

9. The device for rapid separation of honey and protein in pea starch production wastewater according to claim 8, characterized in that, The self-driving shaft (5) has a hollow interior and an inner tube rod (9) is rotatably mounted inside. Three sets of flushing and recovery ports (53) are opened on the outside of the self-driving shaft (5). The flushing and recovery ports (53) are located directly above the corresponding sealing discs. A flushing auxiliary pipe (54) is provided between the self-driving shaft (5) and the conical liquid control hopper (8). A flushing and recovery inner port (91) is opened on the outside of the inner tube rod (9). The flushing and recovery inner port (91) and the flushing and recovery outer port (53) are correspondingly arranged and can be staggered. A flushing main pipe (92) is provided inside the inner tube rod (9). The flushing main pipe (92) and the flushing auxiliary pipe (54) are correspondingly arranged and can be staggered.

10. A method for rapid separation of honey sugar and protein in pea starch production wastewater, using the rapid separation device for honey sugar and protein in pea starch production wastewater according to any one of claims 1-9, characterized in that, Includes the following steps: S1. Wastewater enters the counter-current destabilization section (1) from the top double tangential counter-current inlet pipe (11). Through the vortex field of the counter-current counter-current and the gradually changing flow channel, a controllable high-frequency shear microturbulence is generated, which only destroys the stable double electric layer structure of the protein colloid, causing it to destabilize and aggregate to form micron-sized protein flocs of 10-50μm. S2. After destabilization, the wastewater enters the microbubble swirling separation section (2) in a swirling state. At the same time, compressed air enters the pressure stabilizing chamber (22) through the air inlet pipe (24) and then enters the conical swirling cylinder (21) through the tangential unidirectional nozzle (23). Under the shearing action of the swirling liquid, uniform microbubbles of 10-50μm are generated in situ. The bubbles and the swirling liquid flow in the same direction, without radial impact, and do not disrupt the stability of the swirling field. The destabilized protein flocs have strong hydrophobicity and are instantly adsorbed after colliding with the microbubbles to form "gas". The protein flocculent complex has a density much lower than that of the liquid phase. Under the action of the swirling centrifugal field, the low-density complex rapidly accumulates towards the central axis of the cylinder, forming a continuous concentrated protein column. The concentrated protein guide tube (25) generates negative pressure to discharge the concentrated protein phase, thus achieving efficient pre-separation of the protein. Honey, being a strongly hydrophilic small molecule, is not adsorbed by microbubbles and remains in the liquid phase. It is thrown towards the cylinder wall by the swirling field, forming a circumferential honey liquid phase layer, which flows down the cone wall into the gradient sieving fine separation section (3) to complete the pre-separation. S3. The pre-separated honey liquid phase enters the gradient sieving fine separation section (3). After being sieved step by step by three layers of conical gradient screens (7), the high-speed rotating conical gradient screens (7) form a dynamic sieving interface. The protein impurities trapped are thrown upwards along the conical screen surface to the cylinder wall under the action of centrifugal force. The bottom 100nm conical gradient screens (7) realize the precise classification of protein and honey, completely trapping all residual protein and only allowing small honey molecules to pass through. Finally, the purity of the honey clear liquid is ≥98%, and the protein residue is ≤0.1%.

Images