Hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device and its application

Abstract

This invention relates to the field of water treatment technology, specifically disclosing a hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device and its application. The device includes an influent system, an effluent system, a reactor shell, a membrane module, and an aeration module. A first baffle is installed inside the reactor shell, dividing the interior into an anoxic zone and an aerobic zone. A multi-stage flow guiding mechanism is vertically arranged within the anoxic zone to change the flow direction of the sludge-water mixture. The aeration module is located at the bottom of the aerobic zone, enabling the sludge-water mixture to circulate between the anoxic and aerobic zones. The membrane module is located within the aerobic zone and positioned above the nano-aeration disc. This invention achieves favorable hydraulic conditions under continuous flow, creating a driving force for granulation and enabling rapid formation and stable operation of aerobic granular sludge. The combination of aerobic granular sludge and membrane module filtration improves effluent quality, reduces membrane fouling, shortens the process flow, and reduces floor space requirements.

Description

Technical Field

[0001] This invention relates to the field of water treatment technology, specifically to a hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device and its application. Background Technology

[0002] With the continuous growth of the global population, water consumption and wastewater discharge have surged, leading not only to water pollution but also to water scarcity, posing a series of challenges to water security and sustainable development. Several national policies have explicitly proposed stricter requirements for pollutant emission control, emphasizing the need to accelerate the resource utilization of urban domestic sewage and promote coordinated carbon emission control in water environment governance to achieve synergistic effects in pollution reduction and carbon reduction. As the most widely used wastewater treatment technology, the activated sludge process has a history of over 100 years of research and engineering application and remains the primary technology used for treating urban domestic sewage and industrial wastewater in many cities. However, traditional activated sludge processes suffer from common problems such as low pollutant treatment capacity, high energy and material consumption, large carbon emissions, high residual sludge production, large land area requirements, and complex process flows. Therefore, under the dual pressures of water scarcity and carbon peaking, there is an urgent need to address the bottlenecks in water purification mechanisms by starting from the source, developing and applying next-generation urban wastewater treatment technologies to improve effluent quality and achieve "green, economical, efficient, and low-carbon" wastewater treatment.

[0003] In recent years, numerous studies have demonstrated that aerobic granular sludge and ceramic membrane bioreactors offer significant advantages in improving effluent quality, reducing sludge production, lowering energy and material consumption, shortening process flow, reducing land area, and minimizing carbon emissions. They hold promise as a next-generation technology for urban wastewater treatment, potentially replacing the traditional activated sludge process. Due to its rapid settling and high solids concentration, aerobic granular sludge technology integrates sedimentation units into the treatment unit, eliminating the need for large secondary sedimentation tanks and energy-intensive recirculation facilities. It not only simultaneously removes or recovers pollutants such as carbon, nitrogen, and phosphorus but also significantly reduces land area, earning it the reputation as a promising new biological wastewater treatment technology for future engineering applications.

[0004] However, currently, aerobic granular sludge is primarily cultivated in sequencing batch reactors (SBRs), making it difficult to integrate into existing continuous flow wastewater treatment plants that rely on secondary sedimentation tanks for solid-liquid separation. Furthermore, its stability and start-up time are challenging to control and resolve in existing continuous flow wastewater treatment plants, hindering its widespread application. In contrast, continuous flow reactors offer simpler operation and control systems, lower installation and operating costs, and the ability to handle large volumes of wastewater.

[0005] Therefore, research on aerobic granular sludge under continuous flow conditions will be more beneficial for the upgrading and transformation of existing continuous flow wastewater treatment plants, and has significant application value. Currently, the main technical challenges of continuous flow aerobic granular sludge technology lie in the development of the continuous flow reactor configuration, the creation of hydraulic conditions and granulation driving forces under continuous flow conditions, and the rapid start-up and stable operation of aerobic granular sludge under continuous flow conditions. Related research is still in the laboratory pilot and pilot-scale stages, and there are no reports globally on the practical application of continuous flow aerobic granular sludge technology in large-scale wastewater treatment plants.

[0006] Membrane bioreactor (MBR) technology is a highly competitive novel water treatment process. It uses membrane modules instead of traditional biological secondary sedimentation tanks, offering advantages such as a short process flow, small footprint, stable and high-quality effluent, and low sludge production. It is recognized worldwide as one of the most advanced wastewater treatment technologies. However, membrane fouling is currently the main bottleneck limiting the widespread application of MBRs. Summary of the Invention

[0007] The purpose of this invention is to provide a hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device and its application. This integrated device, through a special structural design, can achieve good hydraulic conditions under continuous flow, create granulation driving force, and realize the rapid formation and stable operation of aerobic granular sludge. By combining aerobic granular sludge with membrane module filtration, the invention aims to improve effluent quality, reduce membrane fouling, shorten the process flow, reduce floor space, and reduce carbon emissions and sludge generation.

[0008] This invention is achieved through the following technical solution:

[0009] A hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device includes an influent system, an effluent system, a reactor shell, membrane modules, and aeration modules;

[0010] A first baffle is installed inside the reactor shell, which divides the internal space of the reactor shell into an anoxic zone and an aerobic zone; the top and bottom of the first baffle have gaps with the top and bottom of the reactor shell, respectively.

[0011] The anoxic zone is equipped with a multi-stage flow guiding mechanism in the vertical direction to change the flow direction of the mud-water mixture.

[0012] The aeration components are located at the bottom of the aerobic zone to enable the mud-water mixture to form a circumferential movement between the anoxic and aerobic zones;

[0013] The membrane module is placed within the aerobic zone and above the nano-aeration disc of the aeration module;

[0014] The water inlet system is connected to the anoxic zone and is used to introduce water to be treated into the anoxic zone. The water to be treated is sewage / wastewater.

[0015] The effluent system is connected to the membrane module and is used to export the filtered effluent from the membrane module to the reactor shell, or to backwash the membrane module.

[0016] This invention utilizes aeration components to provide power to create a circumferential motion of the sludge-water mixture between the anoxic and aerobic zones, providing suitable habitat conditions for the growth and enrichment of various microorganisms. Furthermore, by setting up multi-stage flow guiding mechanisms in the anoxic zone, favorable hydraulic conditions are formed, regularly creating multiple vortices, increasing the collision opportunities and shear force of the sludge-water mixture, and promoting the granulation of flocculent sludge. In other words, this invention can achieve favorable hydraulic conditions under continuous flow conditions, create granulation driving force, and realize the rapid formation and stable operation of aerobic granular sludge.

[0017] This invention combines aerobic granular sludge with a ceramic membrane bioreactor, which can complement each other's advantages and achieve the goals of improving effluent quality, reducing membrane fouling, shortening the process flow, reducing land area, reducing carbon emissions and sludge generation.

[0018] Furthermore, after the flocculent sludge is granulated, it forms aerobic granular sludge. Aerobic granular sludge has the characteristics of large size, good settling properties and low soluble extracellular polymers, which can alleviate the problem of membrane module fouling.

[0019] Furthermore, the multi-stage flow guiding mechanism includes at least two flow guiding plates from top to bottom; the flow guiding plates are inclined, and the two sides of the flow guiding plates are connected to the inner wall of the reactor shell. The upper and lower ends are respectively separated from the inner wall of the reactor shell and the first baffle. The inclination directions of the two adjacent flow guiding plates are opposite, so that the lower end of the previous flow guiding plate and the upper end of the next flow guiding plate are on the same side.

[0020] The two ends of the air deflector specifically refer to the upper (high end) and lower (low end) of both ends, while the two sides of the air deflector specifically refer to the attached... Figure 1 The front and rear sides of the baffle plate are connected to the inner wall of the reactor shell, thus fixing the baffle plate inside the reactor shell.

[0021] Furthermore, the multiple guide plates are arranged in two ways. In one way, the high end of the guide plate is close to the inner wall of the reactor shell, and the low end of the guide plate is close to the first baffle. In the other way, the high end of the guide plate is close to the first baffle, and the low end of the guide plate is close to the inner wall of the reactor shell. The guide plates in the two ways are arranged alternately from top to bottom, and the high end of the topmost guide plate is close to the inner wall of the reactor shell.

[0022] Furthermore, the high end of the bottommost guide vane is connected to the bottom of the first baffle.

[0023] Furthermore, the distance between the high end of the guide plate and the inner wall of the first baffle or reactor shell is 1 / 2 of the distance between the low end of the guide plate and the inner wall of the first baffle or reactor shell.

[0024] Furthermore, the minimum longitudinal spacing between two adjacent guide vanes is 50% to 60% of the guide vane length.

[0025] Furthermore, the tilt angle of the deflector is 40° to 50°.

[0026] Furthermore, a second baffle is also provided inside the reactor shell; the second baffle is arranged parallel to the first baffle, and the top and bottom of the second baffle have gaps with the top and bottom of the reactor shell, respectively; the first baffle and the second baffle divide the internal space of the reactor shell into anoxic zone, aerobic zone and settling zone. Under the action of the aeration components, the mud-water mixture forms a circumferential motion between the anoxic zone and the aerobic zone, and between the aerobic zone and the settling zone.

[0027] Furthermore, a third baffle is provided within the settling zone. The top of the third baffle is connected to the top of the reactor shell, and there is a gap between the bottom of the third baffle and the bottom of the reactor shell. The third baffle causes the settling zone to form a first settling zone and a second settling zone. The first settling zone is located between the third baffle and the second baffle, and the second settling zone is located between the third baffle and the reactor shell. A sludge discharge port connected to the second settling zone is provided on the reactor shell.

[0028] This invention achieves alternating and cyclical operation of multiple compartments by setting up a first baffle, a second baffle, and a third baffle, providing suitable habitat conditions for the growth and enrichment of various microorganisms.

[0029] The multi-chamber alternating circulation operation, the multi-stage flow guiding mechanism, and the formation of vertical double settling zones in this invention create a selective pressure for sludge settling velocity, thereby achieving sludge screening. These three factors work together to create a good driving force for the formation of granular sludge under continuous flow conditions.

[0030] Applications of hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated devices include granular sludge cultivation and wastewater treatment.

[0031] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0032] 1. Through the ingenious design of a multi-stage flow guiding mechanism, this invention creates multiple vortex flow patterns within the reactor shell, providing better shear force and hydraulic conditions for the formation of granular sludge in the system, and achieving better hydraulic drive. In addition, the multi-stage flow guiding mechanism enables a longer vertical water flow path for the sludge-water mixture under anoxic conditions, prolonging the residence time in the anoxic zone, enhancing the enrichment and growth of denitrifying bacteria, and strengthening nitrogen removal.

[0033] 2. Based on the difference in settling rate between granular sludge and flocculent sludge, this invention adds a third baffle in the reactor to form a vertical double settling zone, selects aggregates with good settling performance and eliminates flocculent sludge with poor settling performance, thus creating a good settling selectivity for sludge granulation.

[0034] 3. The multi-stage flow guiding mechanism combined with the design of the dual settling zone in this invention provides multiple driving forces for sludge granulation, realizes the rapid cultivation and stable operation of aerobic granular sludge under continuous flow conditions, solves the technical problem of the difficulty in forming aerobic granular sludge under current continuous flow conditions, and has promotional significance for the treatment of large flow sewage / wastewater under continuous flow conditions.

[0035] 4. This invention combines the advantages of both aerobic granular sludge and membrane filtration. Through the special structure of the device, it achieves hydraulic continuity between the two promising processes. The system can realize the rapid formation of granular sludge and the efficient and stable operation of the system, thereby improving the quality of effluent, reducing membrane fouling, shortening the process flow, reducing sludge generation, and reducing the footprint, providing a "green and low-carbon" treatment solution for wastewater. Attached Figure Description

[0036] The accompanying drawings, which are included to provide a further understanding of embodiments of the invention and form part of this application, do not constitute a limitation thereof. In the drawings:

[0037] Figure 1 This is a schematic diagram of the planar structure of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device of the present invention;

[0038] Figure 2 This is a 3D structural schematic diagram of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device of the present invention.

[0039] Figure 3 This is a velocity cloud map of the internal flow field of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device of the present invention, simulated using a hydraulic model.

[0040] Figure 4 The image shows aerobic granular sludge cultivated using the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device of the present invention in the embodiment.

[0041] Figure 5 This is a diagram illustrating the effect of using the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device of the present invention to treat wastewater in an embodiment of the present invention.

[0042] The attached diagram shows the markings and corresponding component names:

[0043] 1-Inlet tank, 2-Inlet pipe, 3-Float valve, 4-Reactor shell, 5-No. 1 guide plate, 6-No. 2 guide plate, 7-No. 3 guide plate, 8-No. 4 guide plate, 9-First baffle, 10-Nano aeration disc, 11-Air inlet pipe, 12-Check valve, 13-Gas flow meter, 14-Aerator, 15-Membrane module, 16-Second baffle, 17-Outlet pipe, 18-Pressure sensor, 19-Paperless recorder, 20-Peristaltic pump, 21-Outlet tank, 22-Dissolved oxygen probe, 23-Multi-parameter combination probe, 24-Multi-parameter transmitter, 25-Third baffle, 26-Sludge discharge port, 27-Sludge discharge pipe, 28-Sludge discharge pump, 29-Excess sludge collector. Detailed Implementation

[0044] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to embodiments. The illustrative embodiments and descriptions of this invention are for illustrative purposes only and are not intended to limit the invention. The embodiments described below are some, but not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0045] In the following description, numerous specific details are set forth to provide a thorough understanding of the invention. However, it will be apparent to those skilled in the art that these specific details are not necessary to practice the invention. In other embodiments, well-known structures, materials, or methods are not specifically described to avoid obscuring the invention. Unless otherwise specified, the materials, instruments, and reagents used in the following embodiments are commercially available. Unless otherwise specified, the techniques used in the embodiments are conventional methods well known to those skilled in the art.

[0046] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this application, "multiple" means two or more, unless otherwise explicitly specified.

[0047] Example 1:

[0048] like Figure 1 , Figure 2 As shown, the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device includes an influent system, an effluent system, a reactor shell 4, a membrane module 15, and an aeration module.

[0049] A first baffle 9 is vertically arranged inside the reactor shell 4. The first baffle 9 divides the internal space of the reactor shell 4 into an anoxic zone and an aerobic zone. When the device is running, the mud-water mixture fills the entire reactor shell 4. The top and bottom of the first baffle 9 have gaps with the top and bottom of the reactor shell 4, respectively. The vertical circumferential circulation of the mud-water mixture in the anoxic zone and the aerobic zone is achieved through the gaps between the top and bottom.

[0050] The anoxic zone is equipped with a multi-stage flow guiding mechanism in the vertical direction to change the flow direction of the mud-water mixture. Specifically, the multi-stage flow guiding mechanism includes at least two guide plates from top to bottom. The guide plates are inclined, and both ends of the guide plates have gaps between them and the inner wall of the reactor shell 4 and the first baffle 9, respectively. The two sides of the guide plates are connected to the inner wall of the reactor shell 4, thus fixing the guide plates inside the reactor shell 4. The two ends of the guide plates specifically refer to the high end and the low end, and the two sides specifically refer to the upper and lower ends. Figure 1 The guide plates are arranged in two ways: one is that the high end of the guide plate is close to the inner wall of the reactor shell 4, and the low end of the guide plate is close to the first baffle 9; the other is that the high end of the guide plate is close to the first baffle 9, and the low end of the guide plate is close to the inner wall of the reactor shell 4. The guide plates in the two arrangements are staggered from top to bottom, and the high end of the top guide plate is close to the inner wall of the reactor shell 4. Preferably, the high end of the bottom guide plate is connected to the bottom of the first baffle 9.

[0051] In a specific case, such as Figure 1 , Figure 2 As shown, the multi-stage flow guiding mechanism consists of four guide plates, which are, from top to bottom, guide plate 1 (5), guide plate 2 (6), guide plate 3 (7), and guide plate 4 (8). The high ends of guide plate 1 (5) and guide plate 3 (7) are close to the inner wall of the reactor shell 4, i.e., guide plate 1 (5) and guide plate 3 (7) are inclined downward toward the first baffle 9. The high ends of guide plate 2 (6) and guide plate 4 (8) are close to the first baffle 9, i.e., guide plate 2 (6) and guide plate 4 (8) are inclined downward toward the reactor shell 4. The high end of guide plate 4 (8) is connected to the bottom of the first baffle 9.

[0052] In a preferred embodiment, the distance between the high end of the guide plate and the inner wall of the first baffle 9 or the reactor shell 4 is half the distance between the low end of the guide plate and the inner wall of the first baffle 9 or the reactor shell 4. This distance avoids the generation of dead zones in the water flow.

[0053] In a preferred embodiment, the minimum longitudinal spacing between two adjacent guide vanes is 50% to 60% of the guide vane length, meaning that adjacent guide vanes do not intersect. Specifically, the minimum longitudinal spacing refers to the vertical distance between the lower end of the upper guide vane and the upper end of the next guide vane. For example, in a specific case, the minimum longitudinal spacing of 5cm between the bottom of guide vane 1 (5) and the upper end of guide vane 2 (6) is determined based on fluid dynamics analysis. The staggered arrangement of multiple guide vanes in the anoxic zone creates an S-shaped flow channel in the longitudinal direction of the anoxic zone.

[0054] In a preferred embodiment, the angle of the deflector is 40° to 50°, specifically 45°.

[0055] The aeration assembly is located at the bottom of the aerobic zone to enable the mud-water mixture to move in a circular motion between the anoxic and aerobic zones. Specifically, the aeration assembly consists of an aerator 14, an air inlet pipe 11, a gas flow meter 13, a check valve 12 on the outside of the reactor shell 4, and a nano-aeration disc 10 inside the reactor shell 4. The aerator 14 is connected to the nano-aeration disc 10 through the air inlet pipe 11. The gas flow meter 13 and the check valve 12 are installed on the air inlet pipe 11. The aeration flow rate is adjusted based on online dissolved oxygen concentration monitoring and is controlled at 3-4 mg / L by the gas flow meter 13.

[0056] The membrane module 15 is disposed within the aerobic zone and positioned above the nano-aeration disc 10, for membrane filtration of the mud-water mixture within the aerobic zone. The membrane module 15 is preferably made of a hollow flat-plate ceramic membrane with a pore size <0.1 μm and an effective membrane area of ​​0.1 m². 2 The membrane flux is 17.1 L / h / m 2 The membrane performance and operating parameters are not limited to those described in this embodiment. In this embodiment, a flat ceramic membrane is used. Compared with organic membranes, it has high mechanical strength, a flat structure, and is easy to clean and regenerate the membrane surface, which can effectively reduce membrane fouling and extend the service life of the membrane. The combination of aerobic granular sludge and ceramic membrane bioreactor can complement each other's advantages, improve the quality of effluent and reduce membrane fouling.

[0057] The water inlet system is connected to the anoxic zone and is used to supply sewage / wastewater to the anoxic zone. The water inlet system mainly consists of a float valve 3, an inlet pipe 2, and an inlet tank 1. The float valve 3 is installed at the upper end of the anoxic zone. The float valve 3 is connected to the inlet tank 1, which is located on the outside of the reactor shell 4, through the inlet pipe 2. The inlet tank 1 stores sewage / wastewater to be treated, and the effective height of the liquid level is controlled to be 50cm by the float valve 3.

[0058] The effluent system is connected to the membrane module 15 and is used to discharge the filtered effluent from the membrane module 15 to the reactor shell 4, or to backwash the membrane module 15. The effluent system consists of an effluent pipe 17, a pressure sensor 18, a paperless recorder 19, a peristaltic pump 20, and an effluent tank 21. The membrane module 15 is connected to the effluent tank 21, which is located outside the reactor shell 4, via the effluent pipe 17. The pressure sensor 18 and the peristaltic pump 20 are mounted on the effluent pipe 17. The paperless recorder 19 is electrically connected to the pressure sensor 18. The peristaltic pump 20 draws water to provide pressure for water production. The pump-stop ratio of the peristaltic pump 20 is 7:3 per minute, and one water production cycle is 10 minutes. During operation, by switching the rotation direction of the peristaltic pump 20, water is drawn from the effluent tank 21 to perform online backwashing of the membrane module 15. Backwashing lasts for 1 minute within one water production cycle, and the backwash flow rate is twice the influent flow rate. When the pressure sensor 18 shows that the transmembrane pressure difference reaches 30 kPa or more, it is considered that the membrane fouling is severe, and one operating cycle of the reactor ends. The fouled membrane module 15 is removed from the reactor, cleaned by physical cleaning and chemical soaking, and then put back into the reactor for reuse.

[0059] In a preferred embodiment, a second baffle 16 is also provided inside the reactor shell 4; the second baffle 16 is arranged parallel to the first baffle 9, and the top and bottom of the second baffle 16 have gaps with the top and bottom of the reactor shell 4, respectively; the first baffle 9 and the second baffle 16 divide the internal space of the reactor shell 4 into anoxic zone, aerobic zone and settling zone. Under the action of the aeration components, the mud-water mixture forms a circumferential motion between the anoxic zone and the aerobic zone, and between the aerobic zone and the settling zone.

[0060] Because the sludge-water mixture forms a circumferential motion between the aerobic zone and the settling zone, the sludge-water mixture that circulates back from the lower end of the settling zone enters the aerobic zone. Under the influence of aeration and water flow impact, it generates vortices of larger size and higher velocity, which significantly increases the water flow shear force and promotes sludge granulation.

[0061] In a preferred embodiment, a third baffle 25 is provided within the settling zone. The top of the third baffle 25 is connected to the top of the reactor shell 4, and a gap exists between the bottom of the third baffle 25 and the bottom of the reactor shell 4. The third baffle 25 forms a first settling zone and a second settling zone. The first settling zone is located between the third baffle 25 and the second baffle 16, and the second settling zone is located between the third baffle 25 and the reactor shell 4. A sludge discharge port 26 connected to the second settling zone is provided on the reactor shell 4. The sludge discharge port 26 is used to periodically discharge sludge from the second settling zone. The sludge discharge port 26, together with the sludge discharge pipe 27, the sludge discharge pump 28, and the residual sludge collector 29, constitute a sludge discharge system. The sludge discharge port 26 is connected to the residual sludge collector 29 located outside the reactor shell 4 via the sludge discharge pipe 27. The sludge discharge pump 28 is located on the sludge discharge pipe 27. Preferably, multiple sludge discharge ports 26 are provided from top to bottom on the side wall of the second settling zone. The multiple sludge discharge ports 26 allow for the selective removal of sludge with poor settling performance based on the actual operation of the reactor. The sludge is then periodically pumped out by the sludge discharge pump 28, promoting microbial metabolic growth and maintaining the activity of the system's microorganisms.

[0062] In this embodiment, a dual settling zone (a first settling zone and a second settling zone) is formed by setting a third baffle 25. The dual settling zone can effectively eliminate flocculent sludge with poor settling performance, providing a competitive advantage for the growth and further aggregation of sludge with faster settling speed. On the other hand, after the sludge-water mixture circulates back through the lower end of the dual settling zone into the aerobic zone, it also generates vortices with larger size and speed under aeration and water flow impact, which significantly improves the water flow shear force and promotes sludge granulation.

[0063] In this embodiment, an automatic monitoring and control system may also be included. The automatic monitoring and control system mainly consists of an online pH meter, dissolved oxygen meter, ORP meter, thermometer, pressure sensor, paperless recorder, and multi-parameter transmitter 24. It can realize online monitoring of multiple parameters such as pH, dissolved oxygen, ORP, temperature, and pressure. The dissolved oxygen probe 22 of the dissolved oxygen meter is inserted into the aerobic zone, and the probes of the pH meter, ORP meter, and thermometer are multi-parameter combination probes 23.

[0064] In a specific case

[0065] The reactor shell 4 is equipped with a first baffle 9, a second baffle 16 and a third baffle 25, which divide the reactor shell 4 into multiple compartments. The left side is the anoxic zone with a volume of 4.6L; the middle is the aerobic zone with a volume of 6.5L; and the right side is the dual settling zone, with the first settling zone having a volume of 1.7L and the second settling zone having a volume of 0.9L.

[0066] Four guide plates are installed in the anoxic zone channel and arranged at intervals from top to bottom, with two plates on each side. The guide plates 5 and 7 on the left side are inclined at a 45° angle to the inner wall of the reactor shell 4. This angle is based on fluid dynamics analysis. The lateral distance between the guide plates 5 and 7 and the inner wall of the reactor shell 4 is 0.5 cm, and the lateral distance between them and the first baffle 9 is 1 cm. This spacing avoids the formation of dead zones in the water flow.

[0067] The No. 2 guide plate 6 and the No. 4 guide plate 8 on the right side are inclined at a 45° angle to the first baffle 9 in the longitudinal direction. This angle is set based on fluid dynamics analysis. The lateral distance between the No. 2 guide plate 6 and the first baffle 9 is 0.5 cm, and the lateral distance between the No. 2 guide plate 6 and the inner wall of the reactor shell 4 is 1 cm. The No. 4 guide plate 8 is connected to the lower end of the first baffle 9, and the lateral distance between the No. 4 guide plate 8 and the inner wall of the reactor shell 4 is 1 cm. This distance setting avoids the generation of dead zones in the water flow.

[0068] Adjacent guide vanes do not intersect. The lower end of each guide vane is 5cm apart from the upper end of the next guide vane. Specifically, the lower end of guide vane 1 (lower end) and the upper end of guide vane 2 (higher end) are 5cm apart, the lower end of guide vane 2 (6) and the upper end of guide vane 3 (7) are 5cm apart, and the lower end of guide vane 3 (7) and the upper end of guide vane 4 (7) are 5cm apart. This size setting is based on fluid dynamics analysis. The spaced arrangement of multiple guide vanes in the anoxic zone forms an S-shaped flow channel in the longitudinal direction of the anoxic zone.

[0069] Under conditions of an influent flow rate of 1.71 L / h, an aeration rate of 2 L / min in the aerobic zone, and a sludge concentration of 5 g / L, with a longitudinal spacing of 5 cm between the guide vanes and each guide vane inclined at a 45° angle to the longitudinal direction, fluid dynamics analysis shows that the sludge-water mixture can form multiple vortices with a height of approximately 5 cm between the guide vanes. Figure 3 As shown.

[0070] The dual settling zone is mainly composed of the reactor outer shell 4, the second baffle 16, and the third baffle 25. The horizontal distance between the second baffle 16 and the third baffle 25 is 2.5 cm, and the horizontal distance between the third baffle 25 and the right side wall of the reactor outer shell 4 is 1.5 cm. The area between the second baffle 16 and the third baffle 25 is the first settling zone, and the area between the third baffle 25 and the right side wall of the reactor outer shell 4 is the second settling zone.

[0071] The working principle of this embodiment:

[0072] The influent enters the anoxic zone through the float valve 3, where it mixes thoroughly with the mud-water mixture flowing out from the top of the aerobic zone. When the mud-water mixture collides with the first guide plate 5, its flow direction and velocity change, forming a vortex between the first guide plate 5 and the first baffle 9. Subsequently, it flows through the gap between the first guide plate 5 and the first baffle 9 into the area of ​​the second guide plate 6, where a vortex is formed between the second guide plate 6 and the reactor shell 4. This process repeats continuously, with countless hydraulic vortices forming between the guide plates. Under the influence of gravity and the power generated by the continuous aeration in the aerobic zone, the water flows downwards along the S-shaped flow channels formed by the guide plates to the bottom of the aerobic zone.

[0073] In the anoxic zone, without guide plates, the sludge-water mixture moves vertically due to gravity and the power generated by aeration, resulting in a relatively fast flow velocity. This embodiment uses a multi-stage guide mechanism to alter the flow pattern of the sludge-water mixture. When the mixture impacts the guide plates, its flow direction and velocity change, causing it to flow in a directional and regular vortex pattern between the guide plates. Under continuous aeration, the sludge-water mixture continuously flows from the top of the aerobic zone into the anoxic zone, generating kinetic energy. This cycle repeats, creating numerous vortex flow patterns. When the fluid movement is circumferential, the hydraulic shear force in the fluid can remain relatively stable. In this relatively stable environment, flocculent sludge easily collides and aggregates, gradually forming granular sludge. Therefore, hydraulic vortices are the core force driving the aggregation of flocculent sludge, promoting granulation of the flocculent sludge.

[0074] However, vortices disappear from their formation over time. Vortices formed by a single guide vane gradually vanish with the flow of water and the passage of time, which does not promote the formation and stabilization of nascent particles. The multi-stage guide mechanism can continuously create vortices, better optimize the flow field environment, and facilitate particle formation and stabilization. Therefore, this device is equipped with a multi-stage guide mechanism in the anoxic zone.

[0075] Furthermore, the spacing between the guide vanes also needs to be rigorously calculated and verified. In this implementation case, when the longitudinal spacing between adjacent guide vanes is greater than 5cm, vortices cannot be continuously generated, and the flow field environment cannot be optimized; when the longitudinal spacing between adjacent guide vanes is less than 5cm, the flow field is in a full vortex state, and excessive power will cause the formed primary particles to disperse, and the vortices between guide vanes will come into contact and disperse, affecting the vortex effect of the flow field and hindering the collision and aggregation of microorganisms. A longitudinal spacing of 5cm between adjacent guide vanes is the most appropriate spacing parameter required to achieve single vortex generation and shedding, and can form a Karman vortex street in the model reaction zone that facilitates the collision and aggregation of flocculent sludge. Therefore, the longitudinal spacing between the guide vanes in this device is 5cm. When the guide vanes are tilted at a 45° angle to the longitudinal direction, the mud-water mixture can collide with the guide vanes in the forward direction, generating better vortices. Therefore, in this implementation case, the guide vanes are tilted at a 45° angle to the longitudinal direction.

[0076] The smaller cross-sectional area at the bottom of the anoxic zone allows the sludge-water mixture to enter the bottom of the aerobic zone at a higher flow rate. Continuous aeration generates large-sized and high-velocity vortices, significantly increasing the shear force of the water flow and accelerating the granulation of flocculent sludge. Furthermore, the continuous aeration provides upward kinetic energy for the sludge-water mixture, causing the sludge at the bottom of the aerobic zone to rise rapidly to the top level with the air bubbles. This increases the flow area, causing the sludge-water mixture to disperse horizontally in all directions. Some of the mixture flows into the anoxic zone, mixes with the influent, and returns to the bottom of the aerobic zone via a multi-stage guiding mechanism, thus forming a large vertical circulation between the anoxic and aerobic zones. A portion of the mixture also flows horizontally into the dual settling zone.

[0077] The aeration components have three main functions: 1) The airflow generated by aeration can agitate the sludge in the aerobic zone, ensuring uniform mixing and eliminating dead zones. It also provides the power to propel the sludge upwards into the anoxic zone and the dual settling zone, thus creating an infinite vertical circulation between the aerobic zone and the anoxic and dual settling zones, generating better shear force; 2) It increases the dissolved oxygen concentration of the sludge in the aerobic zone, providing sufficient dissolved oxygen to accelerate the decomposition of pollutants by aerobic microorganisms; 3) When the airflow rises, it washes over the membrane components, causing the sludge deposits on the membrane components to fall off, reducing concentration polarization and mitigating membrane fouling.

[0078] The sludge-water mixture entering the dual settling zone from the aerobic zone settles into the first settling zone under a strong downward vertical force. In the first settling zone, sludge with good settling properties flows downwards back to the bottom of the aerobic zone under the influence of gravity and water flow. However, some sludge with poor settling properties is suspended at the bottom of the third baffle 25 and enters the second settling zone. In the second settling zone, some sludge is pumped out by the sludge discharge pump 28, while some sludge, driven by hydraulic pressure, returns to the bottom of the aerobic zone along with the sludge-water mixture in the first settling zone. Under continuous operation and aeration, a vertical circulation loop is also formed between the aerobic zone and the dual settling zone. Therefore, the dual settling zone effectively eliminates flocculent sludge with poor settling performance, providing a competitive advantage for the growth and further aggregation of sludge with faster settling speed. On the other hand, the sludge-water mixture circulating back through the lower end of the dual settling zone enters the aerobic zone, where it generates vortices of larger size and speed under aeration and water flow impact, significantly increasing the water flow shear force and promoting sludge granulation.

[0079] The unique structure and operation mode of the device of this invention enable multiple compartments, creating diverse habitat conditions and providing suitable growth environments for different types of microorganisms, thus promoting their growth. The ingenious design of this reactor has also been validated through reactor flow field analysis. Figure 3 .Depend on Figure 3It is evident that multiple vortices form between the guide plates, and large-sized, high-velocity vortices are also formed at the bottom of the aerobic zone, providing good shear force and creating favorable hydraulic conditions for the formation of granular sludge. Furthermore, under continuous flow operation and sustained aeration, an infinite vertical circulation is formed between the aerobic zone, the anoxic zone, and the dual settling zone. The inherent power provided by continuous aeration stably generates hydraulic vortices, creating an excellent fluid dynamic environment for granular sludge formation.

[0080] Example 2:

[0081] This embodiment is an application case of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device in Embodiment 1. Specifically, the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device is used for granular sludge cultivation.

[0082] In this embodiment, the influent is artificially synthesized wastewater. The wastewater components mainly include carbon source, nitrogen source, phosphorus source, calcium chloride, magnesium chloride, and trace elements (Fe, Zn, Mn, Co, Cu, etc.). The specific water quality is shown in Table 1.

[0083] Table 1 Influent Water Quality

[0084] Components Concentration (mg / L) Components Concentration (mg / L) <![CDATA[CH3COONa]]> 640.6 <![CDATA[FeCl3·6H2O]]> 3 <![CDATA[NH4Cl]]> 95.5 <![CDATA[H3BO3]]> 0.5 <![CDATA[CaCl2]]> 26.0 <![CDATA[CuSO4·5H2O]]> 0.25 <![CDATA[MgCl2]]> 37.95 KI 0.2 <![CDATA[K2HPO4·3H2O]]> 25.16 <![CDATA[MnSO4·H2O]]> 0.5 <![CDATA[KH2PO4]]> 7.2 <![CDATA[ZnSO4·7H2O]]> 0.3 <![CDATA[NiCl2·6H2O]]> 0.2 <![CDATA[CoCl2·6H2O]]> 0.5 <![CDATA[Na2Mo7O 24 .2H2O]]> 0.2 <![CDATA[AlCl3·6H2O]]> 0.2

[0085] The activated sludge from the end of the biochemical tank of a municipal wastewater treatment plant was used as the inoculum sludge for this device. The inoculum sludge was yellowish-brown, loose and cotton-like, with MLVSS / MLSS = 0.57, sludge particle size <100μm, and initial sludge concentration of 5g / L.

[0086] After inoculating the sludge, artificially synthesized wastewater was used to cultivate the sludge. Sodium acetate was used as the carbon source, with a COD of approximately 500 mg / L; K₂HPO₄·3H₂O and KH₂PO₄ were used as phosphorus sources, and NH₄Cl was used as the nitrogen source, with a COD:N:P ratio of 100:5:1. Simultaneously, to meet the needs of microbial growth, trace elements such as Fe, Cu, Mn, and Zn were also added to the synthesized wastewater. The pH was maintained at approximately 7.0, and the temperature at approximately 25℃.

[0087] Water enters the system via float valve 3, maintaining an effective liquid level of 50 cm. The hydraulic retention time is set to 8 hours, the influent pH is approximately 7.0, and the dissolved oxygen in the aerobic zone is 3–4 mg / L. The effluent is produced using a hollow flat-plate ceramic membrane with an effective membrane area of ​​0.1 m². 2 The membrane pore size is 0.1 μm, and the water is discharged in constant flow mode with a peristaltic pump stop-start ratio of 7:3 per minute. The effluent membrane flux is 17.1 L / (m²). 2 *h).

[0088] The influent first enters the upper part of the anoxic zone. Under the action of the multi-stage flow guiding mechanism, the sewage forms a large number of hydraulic vortices between the guide plates. Under the synergistic effect of gravity flow, it enters the bottom of the aerobic zone through the lower part of the anoxic zone.

[0089] Under continuous aeration, the sludge-water mixture rapidly vortexes in the lower part of the aerobic zone and rises quickly with the bubbles. Upon reaching the horizontal surface, the bubbles burst, and the sludge-water mixture disperses horizontally and flows out. Part of the sludge-water mixture mixes with the influent and re-enters the anoxic zone, while another part enters the dual settling zone. The continuous influent and aeration create multiple hydraulic vortices within the system, simultaneously forming an infinite vertical circulation between the aerobic, anoxic, and dual settling zones, providing continuous and stable hydraulic conditions and shear forces for the formation of aerobic granular sludge. Furthermore, the sludge selection effect of the dual settling zone creates favorable settling selective pressure for granular sludge formation. Through the device's unique structure, favorable hydraulic conditions and multiple driving forces are created, enabling the rapid formation and stable operation of aerobic granular sludge.

[0090] After 30 days of cultivation, aerobic granular sludge was successfully cultivated in a hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device, such as... Figure 4 As shown, 50% of the sludge particles have a diameter >371 μm, and 10% have a diameter >1420 μm. This indicates that the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device of Example 1 can efficiently form aerobic granular sludge under continuous flow conditions. Furthermore, the formation of granular sludge significantly reduces the rate of membrane fouling.

[0091] Example 3:

[0092] This embodiment is an application case of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device in Embodiment 1, specifically, the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device is used for sewage treatment.

[0093] The influent is the aforementioned synthetic wastewater. The influent water quality is shown in Table 1. The influent COD is 500 mg / L, and NH4+ is... + -N is 25 mg / L, TN is 25 mg / L, and TP is 5 mg / L. Influent enters the system via a float valve, maintaining an effective liquid level of 50 cm. The hydraulic retention time is set to 8 hours, the influent pH is approximately 7.0, and the DO in the aerobic zone is 3–4 mg / L. The effluent is produced using a hollow flat-plate ceramic membrane with an effective membrane area of ​​0.1 m². 2 The membrane pore size is 0.1 μm, and the water is discharged in constant flow mode with a peristaltic pump stop-start ratio of 7:3 per minute. The effluent membrane flux is 17.1 L / (m²). 2 *h).

[0094] Influent first enters the anoxic zone through float valve 3. Under the influence of water flow and gravity, the wastewater vortexes downwards to the bottom of the aerobic zone. In the anoxic zone, microorganisms utilize the carbon source in the wastewater for denitrification, achieving NO3 reduction. - -N and NO2 - -N removal. The multi-stage flow guiding mechanism enables a longer vertical water flow path for the mud-water mixture under anoxic conditions, increasing the residence time in the anoxic zone and enhancing the denitrification process.

[0095] After the wastewater enters the aerobic zone from the anoxic zone, under aerobic conditions, microorganisms further oxidize and decompose organic matter. Simultaneously, ammonia-oxidizing bacteria, under aerobic conditions, reduce NH4+ in the wastewater. + -N was converted to NO3. - -N and NO2 - -N, polyphosphate-accumulating bacteria undergo phosphorus uptake under aerobic conditions. Under continuous aeration, containing NO3... - -N and NO2 - -N wastewater rises rapidly with the bubbles and flows horizontally from the top of the aerobic zone into the anoxic zone for denitrification. Some phosphorus-absorbing sludge enters the dual settling zone from the top of the aerobic zone, while sludge with poor settling properties is discharged through the sludge outlet of the second settling zone.

[0096] With continuous water intake and operation, the system utilizes the internal power provided by aeration to create an internal circulation between multiple compartments, enriching and cultivating bacteria that efficiently remove C, N, and P. Driven by the hydraulic system and under granulation selective pressure, this abundant bacterial community is granulated, forming aerobic granular sludge with an aerobic exterior, an anoxic interior, and an anaerobic interior, achieving simultaneous nitrogen and phosphorus removal. Based on this aerobic granular sludge, most pollutants in the wastewater are efficiently removed. Finally, the filtration effect of the flat-plate ceramic membrane retains suspended solids and colloidal substances, further improving the effluent quality. Simultaneously, in the alternating aerobic and anoxic environment, the apparent yield coefficient of microorganisms decreases, thus significantly reducing sludge production.

[0097] The system ran stably for 30 days under these conditions, and the results are shown in the attached diagram. Figure 5 The average removal rates were 97.9% for COD, 85.1% for TN, and 92.1% for TP. The effluent COD remained consistently below 15 mg / L, and NH4... + With N below 0.8 mg / L, TN below 13 mg / L, and TP below 2 mg / L, the effluent, except for TP and TN, consistently meets the Class IV surface water standard. This result demonstrates that the device of this invention has a highly efficient wastewater treatment capacity.

[0098] Example 4:

[0099] This embodiment is an evaluation of the shock load resistance of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device in Example 1.

[0100] The influent was synthetic wastewater from Example 2, and its quality is shown in Table 1. By adjusting the influent flow rate, the reactor was operated under different hydraulic retention times and organic loads (reactor operating parameters for each time period are shown in Table 2) to investigate the system's resistance to shock loads. The influent was introduced into the device via float valve 3, with the effective liquid level controlled at 50 cm. The influent pH was approximately 7.0, and the DO in the aerobic zone was 3–4 mg / L. The effluent was produced using a hollow flat-plate ceramic membrane with an effective membrane area of ​​0.1 m². 2 The membrane pore size is 0.1μm, and the water is discharged in constant flow mode with a peristaltic pump pumping-stop ratio of 7:3 per minute.

[0101] The system operated stably for 10 days under various conditions. The results showed that the system could achieve good treatment efficiency under different organic loads, with COD consistently below 20 mg / L and NH4+ below 20 mg / L. + With -N below 1 mg / L, TN below 15 mg / L, and TP below 3 mg / L, the effluent, except for TP and TN, consistently meets the Class IV surface water standard. This result indicates that the device of this invention has good resistance to shock loads and promising application prospects.

[0102] Table 2 Reactor operating parameters at different time periods

[0103]

[0104] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above description is only a specific embodiment of the present invention and is not intended to limit the scope of protection of the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

[0105] It should be noted that the structures, proportions, sizes, etc., illustrated in the accompanying drawings are merely for illustrative purposes to aid those skilled in the art and are not intended to limit the scope of the invention. Therefore, they have no substantial technical significance. Any modifications to the structure, changes in proportions, or adjustments to size, without affecting the effectiveness and purpose of the invention, should still fall within the scope of the disclosed technical content. Furthermore, terms such as "upper," "lower," "left," "right," and "middle" used in this specification are merely for clarity and not intended to limit the scope of the invention. Changes or adjustments to their relative relationships, without substantially altering the technical content, should also be considered within the scope of the invention.

Claims

1. A hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device, characterized in that, It includes an inlet system, an outlet system, a reactor shell (4), a membrane module (15), and an aeration module; A first baffle (9) is provided inside the reactor shell (4). The first baffle (9) divides the internal space of the reactor shell (4) into an anoxic zone and an aerobic zone. The top and bottom of the first baffle (9) have gaps with the top and bottom of the reactor shell (4), respectively. The anoxic zone is equipped with a multi-stage flow guiding mechanism in the vertical direction to change the flow direction of the mud-water mixture. The aeration component is located at the bottom of the aerobic zone, which is used to make the mud-water mixture form a circumferential movement between the anoxic zone and the aerobic zone; The membrane module (15) is disposed in the aerobic zone and placed above the nano-aeration disc (10) of the aeration module; The water inlet system is connected to the anoxic zone; The water outlet system is connected to the membrane module (15); The multi-stage flow guiding mechanism includes at least two flow guiding plates from top to bottom; the flow guiding plates are inclined, and the two sides of the flow guiding plates are connected to the inner wall of the reactor shell (4). The upper and lower ends are respectively separated from the inner wall of the reactor shell (4) and the first baffle (9). The inclination directions of two adjacent flow guiding plates are opposite, so that the lower end of the previous flow guiding plate and the upper end of the next flow guiding plate are on the same side. The multiple guide plates are arranged in two ways. In one way, the high end of the guide plate is close to the inner wall of the reactor shell (4), and the low end of the guide plate is close to the first baffle (9). In the other way, the high end of the guide plate is close to the first baffle (9), and the low end of the guide plate is close to the inner wall of the reactor shell (4). The guide plates in the two ways are arranged alternately from top to bottom, and the high end of the topmost guide plate is close to the inner wall of the reactor shell (4).

2. The hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device according to claim 1, characterized in that, The high end of the bottom guide plate is connected to the bottom of the first baffle (9).

3. The hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device according to claim 1, characterized in that, The distance between the high end of the guide plate and the inner wall of the first baffle (9) or the reactor shell (4) is 1 / 2 of the distance between the low end of the guide plate and the inner wall of the first baffle (9) or the reactor shell (4).

4. The hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device according to claim 1, characterized in that, The minimum longitudinal spacing between two adjacent guide vanes is 50% to 60% of the length of the guide vane.

5. The hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device according to claim 1, characterized in that, The tilt angle of the guide plate is 40°~50°.

6. The hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device according to claim 1, characterized in that, A second baffle (16) is also provided inside the reactor shell (4); the second baffle (16) is arranged parallel to the first baffle (9), and the top and bottom of the second baffle (16) have gaps with the top and bottom of the reactor shell (4), respectively; the first baffle (9) and the second baffle (16) divide the internal space of the reactor shell (4) into an anoxic zone, an aerobic zone and a settling zone. Under the action of the aeration component, the mud-water mixture forms a circumferential motion between the anoxic zone and the aerobic zone, and the mud-water mixture forms a circumferential motion between the aerobic zone and the settling zone.

7. The hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device according to claim 6, characterized in that, A third baffle (25) is provided in the settling zone. The top of the third baffle (25) is connected to the top of the reactor shell (4), and there is a gap between the bottom of the third baffle (25) and the bottom of the reactor shell (4). The third baffle (25) makes the settling zone form a first settling zone and a second settling zone. The first settling zone is located between the third baffle (25) and the second baffle (16), and the second settling zone is located between the third baffle (25) and the reactor shell (4). A sludge discharge port (26) connected to the second settling zone is provided on the reactor shell (4).

8. The application of the hydraulically driven continuous flow aerobic granular sludge-membrane filtration integrated device as described in any one of claims 1-7, characterized in that, This includes granular sludge cultivation and wastewater / sewage treatment.

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