A mobile bed biofilm sewage treatment device

Abstract

The application discloses a mobile bed biofilm sewage treatment device; the upper water level of the facultative zone is communicated with the upper water level of the multifunctional zone through a facultative zone water outlet pipe; the bottom of the multifunctional zone is provided with a suction device, the suction device is communicated with the facultative zone reflux pipe and the lower water level of the facultative zone through the facultative zone water inlet pipe and the facultative zone lower water level; the upper water level of the aerobic zone is communicated with the lower water level of the sedimentation zone through a flow channel, and the upper end of the flow channel is closed with an aerobic zone filler interception plate; the upper water level of the aerobic zone is communicated with the upper water level of the multifunctional zone through a nitrification liquid reflux pipe. By adopting the scheme, the power of the water pump and the power of the air-water mixed bubbles can be utilized to form a circulating flow from the bottom to the top, so that the sewage is fully contacted with the microorganisms and oxygen on the filler, and the pollutants such as BOD, COD and ammonia nitrogen in the sewage are removed; and the circulating flow formed by the jet aerator is used for hydraulic stripping, so that the filler sinks to the bottom, the unevenness of the filler is avoided, and the suspension of the filler is ensured.

Description

Technical Field

[0001] This invention relates to the field of water environment management technology, specifically to a moving bed biofilm wastewater treatment device. Background Technology

[0002] Currently, integrated wastewater treatment systems primarily employ processes such as AAO, MBBR, and SBR. To meet the needs of different process stages, they are often equipped with a large variety and quantity of equipment, such as mixing equipment, aeration equipment, and reflux equipment. Ensuring the normal operation of these devices often requires the construction of auxiliary buildings. In actual operation, backup failures frequently occur, leading to inconsistent effluent quality. Furthermore, the large number of devices increases initial construction investment, operation and maintenance costs, and overall complexity.

[0003] Among the aforementioned processes, the MBBR process, with its advantages of high volumetric loading, good reaction efficiency, good sludge settling performance, and high volume utilization, has become one of the important processes for integrated wastewater treatment plants and upgrades in recent years. Ensuring the suspension and uniformity of the packing material and preventing its aggregation and loss at the effluent outlet are core factors in ensuring the MBBR process fully realizes its effectiveness. To achieve suspension and uniformity of the packing material, the current conventional practice is to use submersible mixers for stirring, or to simultaneously achieve a mixed suspension state through aeration pipes / discs. Although some engineering measures have been taken, the uniformity and mixing degree of the packing material still have certain problems, resulting in poor fluidization and easy local enrichment of the packing material, especially in the effluent zone. At the effluent outlet of the MBBR membrane reactor, grids, meshes, or perforated pipes are often installed to prevent packing material loss, but these are prone to clogging and require regular manual cleaning. Some designs also use backflushing devices such as air pipes to prevent clogging, but these are energy-intensive and ineffective.

[0004] In biological treatment processes, aeration and recirculation systems are crucial components. Currently, conventional integrated wastewater treatment plants primarily use blowers for aeration. Blower selection typically involves rotary blowers, Roots blowers, or centrifugal blowers. Regardless of the type of blower chosen, blower aeration generally presents the following problems: ① Blowers are usually located in a blower room, requiring additional space. ② Blowers have high installed power and consume a large amount of electricity; the electricity cost generated by aeration blowers accounts for approximately 30-40% of the operating costs of township wastewater treatment plants, resulting in high operating costs. ③ Blowers generate noise during operation. Currently, conventional integrated wastewater treatment plants mainly use recirculation pumps or airlift recirculation systems. Recirculation pump recirculation requires a dedicated recirculation pump, increasing the number of devices and energy consumption. Airlift recirculation requires an air source device, and air enters the anaerobic and anoxic zones through the recirculation pipe, making it difficult to create anaerobic and anoxic environments, thus affecting nitrogen and phosphorus removal efficiency. Summary of the Invention

[0005] To address the shortcomings of existing technologies, this invention aims to provide a moving bed biofilm wastewater treatment device. This solution utilizes the power of a water pump and the energy of air-water mixture bubbles to create an upward-sloping circulation, ensuring sufficient contact between the wastewater and the microorganisms and oxygen formed on the packing material. This removes pollutants such as BOD, COD, and ammonia nitrogen from the wastewater. Furthermore, the circulation formed by the jet aerator and hydraulic blowing cause the packing material to sink to the bottom, preventing uneven packing and ensuring its suspension.

[0006] This invention is achieved through the following technical solution:

[0007] A moving bed biofilm wastewater treatment device includes a facultative anaerobic zone, a multifunctional zone, a sedimentation zone, and an aerobic zone arranged sequentially and adjacently.

[0008] Both the facultative and aerobic zones are filled with packing material; the upper water level of the facultative zone is connected to the upper water level of the multifunctional zone through the facultative zone outlet pipe, and the inlet end of the facultative zone outlet pipe is connected to the facultative zone packing material interception pipe.

[0009] The bottom of the multi-functional area is equipped with a suction device. The suction device is connected to the facultative zone return pipe and the lower water level of the facultative zone, and to the aerobic zone inlet pipe and the lower water level of the aerobic zone. The aerobic zone inlet pipe is also equipped with a first jet aerator, and the facultative zone return pipe is also equipped with a second jet aerator.

[0010] The upper water level of the aerobic zone is connected to the lower water level of the sedimentation zone through a flow channel. The sedimentation zone is used to settle sludge and collect clean water. The upper end of the flow channel is sealed with an aerobic zone packing interceptor plate.

[0011] The upper water level of the aerobic zone is connected to the upper water level of the multifunctional zone through the nitrification liquid return pipe, and the inlet end of the nitrification liquid return pipe is equipped with an aerobic zone packing interceptor pipe.

[0012] Compared to existing technologies, although some engineering measures have been taken, the uniformity and mixing degree of the packing material still have certain problems, resulting in poor fluidization and easy local enrichment of the packing material, especially in the effluent zone. At the effluent of the MBBR membrane reactor, grids, meshes, or perforated pipes are often installed to prevent packing material loss, but these are prone to clogging and require regular manual cleaning. Some designs also use backflushing devices such as air pipes to prevent clogging, but these are energy-intensive and ineffective. This solution provides a moving bed biofilm wastewater treatment device. Specifically, the wastewater treatment device is divided into an anaerobic zone, a multifunctional zone, a sedimentation zone, and an aerobic zone. The anaerobic and aerobic zones are filled with packing material to enhance the treatment effect. A suction device, preferably a submersible pump, is installed at the bottom of the multifunctional zone in the middle. The submersible pump pumps the pre- and post-treated wastewater and sends it to the lower water levels of the anaerobic and aerobic zones through the return pipe to the anaerobic zone and the inlet pipe to the aerobic zone, respectively. During the transportation process, the wastewater passes through jet aerators on the pipeline. The system is connected to a first air pipe and a second air pipe connected to a second jet aerator. The wastewater to be treated is mixed with air through the jet aerator to form an air-water mixture. This mixture then enters the bottom of the MBBR reactor through the return pipe to the anaerobic zone and the inlet pipe to the aerobic zone. There can be two inlet pipes for the aerobic zone, symmetrically arranged on both sides. Jet aerators are installed on all three pipes. Powered by a water pump, air is introduced into the anaerobic and aerobic zones for aeration and suspension mixing of the packing material. By utilizing the power of the water pump and the air-water mixture, a circulation is formed from the bottom upwards, fully mixing with the packing material in the MBBR tank to create a fluidized state with full contact between gas, solid, and liquid. This allows the wastewater to fully contact the microorganisms and oxygen formed on the packing material to remove pollutants such as BOD, COD, and ammonia nitrogen from the wastewater. Furthermore, an anaerobic zone outlet pipe is installed at the upper water level of the anaerobic zone to transport wastewater to the multi-functional zone, and a nitrification liquid return pipe is installed at the upper water level of the aerobic zone to transport wastewater to the multi-functional zone. By utilizing the same side of the inlet and outlet for optimized vertical arrangement, the overall circulation dynamics are strengthened. The aerobic zone is then connected to the lower water level of the sedimentation zone through a flow channel, allowing part of the wastewater from the aerobic zone to return to the multi-functional zone through the upper nitrification liquid return pipe, and part to enter the sedimentation zone by gravity flow. The sedimentation process in the sedimentation zone collects clear water. A perforated sludge discharge pipe is installed at the bottom of the sedimentation zone to discharge excess sludge. Finally, the wastewater is collected and discharged by the triangular weir outlet collection trough located in the clear water zone of the sedimentation zone.

[0013] In addition, in the above scheme, the facultative zone effluent pipe, the inlet end of the facultative zone effluent pipe, the inlet end of the nitrification liquid return pipe, and the upper end of the flow channel are respectively equipped with facultative zone packing interception pipe, aerobic zone packing interception pipe, and aerobic zone packing interception plate to intercept the packing and prevent it from entering the multi-functional zone and sedimentation zone. In order to optimize the combination of the aforementioned jet aeration and MBBR process, the MBBR process outlet and packing interception plate are set at the upper part of the jet aeration inlet, 0.5~0.8m below the liquid level. This arrangement of the inlet and outlet positions enhances the circumferential fluidization effect formed by jet aeration. At the same time, the packing interception plate and packing interception pipe are set at the above-mentioned outlet position, so as to effectively utilize the scouring effect of the circumferential flow formed by jet aeration to blow off the packing on the interception plate and interception pipe, avoiding blockage. The blown-off packing is remixed into the reaction tank by the power of the bottom inlet jet, ensuring the secondary uniformity of the system packing. This involves using the circulating flow created by the jet aerator to hydraulically blow away the packing material, causing it to sink to the bottom. The packing material is then mixed again by the jet aerator at the bottom inlet, forming a circulating fluidized state. This avoids uneven packing material distribution and ensures the suspension of the packing material.

[0014] Further optimization involves connecting the upper water level of the facultative anoxic zone to the main inlet pipe, with a slag-blocking grid installed at the outlet of the main inlet pipe. External sewage can enter the facultative anoxic zone through the main inlet pipe and is prevented from entering by foreign objects through the slag-blocking grid.

[0015] Further optimization involves providing a first diffuser at the outlet end of the aerobic zone inlet pipe and a second diffuser at the outlet end of the return pipe to the facultative zone; and setting a diffuser at the outlet of the pipe entering the MBBR reactor to ensure that the gas-water mixed wastewater can be quickly and fully mixed before entering the reactor.

[0016] Further optimization involves installing a first valve on the return pipe to the facultative anoxic zone; by installing the first valve on the pipe entering the facultative anoxic zone, with the first valve located before the jet aerator, the flow rate and aeration volume entering the facultative and aerobic zones can be controlled by distributing the valve opening.

[0017] Further optimization involves installing a second valve on the nitrification liquid return pipe to control the water level difference between the aerobic zone and the multifunctional zone, or between the sedimentation zone and the multifunctional zone.

[0018] Further optimization involves tilting the aerobic zone packing interceptor plate, with its lower end tilted towards one side of the aerobic zone; this reduces packing accumulation.

[0019] Further optimization involves the flow channel comprising a vertical section and an inclined section connected sequentially from top to bottom, with the lower end of the inclined section angled inward toward the sedimentation zone to prevent gas from entering the sedimentation zone and affecting solid-liquid separation.

[0020] Further optimization involves providing a perforated sludge discharge pipe, an inclined pipe, and a water collection trough in the sedimentation zone from bottom to top, with the perforated sludge discharge pipe located at the bottom of the sedimentation zone; this is used to promote efficient separation of sludge and water in the sedimentation zone.

[0021] Further optimization involves connecting the lower water level of the sedimentation zone to the lower water level of the multi-functional zone via a sludge return pipe; the sludge return pipe is a short, tapering pipe, with the opening at one end closer to the sedimentation zone being larger than the opening at the other end; this is used to return the sludge in the sludge storage area at the bottom of the sedimentation zone.

[0022] Further optimization involves arranging the sedimentation zone in a funnel shape to improve space utilization.

[0023] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0024] (1) The present invention provides a moving bed biofilm wastewater treatment device, which improves treatment efficiency and reduces the volume of treatment device through optimized process flow and layout.

[0025] (2) The present invention provides a moving bed biofilm wastewater treatment device, which reduces the number of equipment and lowers investment and operation and maintenance costs and difficulties by optimizing the pipeline control system and the connection arrangement between each process section.

[0026] (3) The present invention provides a moving bed biofilm wastewater treatment device, which adopts a system combination of submersible pump + jet aerator and MBBR process, including the use of submersible pump as influent pump, combination of influent and jet aerator, diffuser set at the outlet, and the air-water mixture formed by jet aeration forming a fluidized state of MBBR in a rectangular tank.

[0027] (4) The present invention provides a moving bed biofilm wastewater treatment device in an MBBR tank, wherein the jet aerator inlet is at the bottom and the outlet is at the top on the same side. This arrangement enhances the fluidization effect of the jet aerator in the rectangular tank and facilitates the removal of the effluent packing material, without the need for extra energy consumption and equipment.

[0028] (5) The present invention provides a moving bed biofilm wastewater treatment device, which is based on the combination of jet aeration and MBBR tank. A perforated plate type inclined packing interceptor is set at the effluent end. The packing is flushed and blown off by the combination of the jet aerator and the inclined angle (60°) of the interceptor. This combination mode does not require additional power.

[0029] (6) The present invention provides a moving bed biofilm wastewater treatment device that integrates and innovates the MBBR process. By setting up an anaerobic zone (MBBR packing zone), a multifunctional zone, an aerobic zone (MBBR packing zone), and a sedimentation zone, the sedimentation zone is located between the multifunctional zone and the aerobic zone. It uses one water pump and a matching pipeline system to realize the functions of internal reflux of nitrification liquid, external reflux of sludge, and mixing and stirring of packing in the anaerobic and aerobic zones.

[0030] (7) The moving bed biofilm wastewater treatment device provided by this invention optimizes the MBBR process by introducing a jet aerator, which is combined with the aforementioned single water pump to achieve aeration and oxygenation of the aerobic zone of the MBBR, while simultaneously creating a fluidized state. This eliminates the need for a blower and supporting facilities, simplifying the wastewater treatment device's piping system. This device uses only one submersible pump. Through innovative process combination and piping design, a single pump can fulfill functions such as reflux, aeration, and mixing, minimizing the number of equipment and reducing investment and maintenance costs.

[0031] (8) The moving bed biofilm wastewater treatment device provided by the present invention uses one pump to realize the above-mentioned activated sludge reaction return function. The pump outlet pipe is divided into three paths. One path mainly returns sludge and part of nitrification liquid to the facultative anaerobic zone (MBBR packing zone) with a flow rate of 1Q. The other two paths enter the aerobic zone (MBBR packing zone) with a flow rate of 3.5Q~6Q. The nitrification liquid in the aerobic zone is returned by the pump through the water level difference formed between the multifunctional zone and the aerobic zone, with a flow rate of 2Q~4Q. The sludge in the sedimentation zone is returned by the pump through the liquid level difference formed between the multifunctional zone and the sedimentation zone, with a flow rate of 0.5Q~1Q.

[0032] (9) The present invention provides a moving bed biofilm wastewater treatment device, including the above-mentioned combined process and the combined biochemical reaction aeration, sludge return, digestate return, pipeline control system and the connection arrangement between each process section.

[0033] (10) The present invention provides a moving bed biofilm wastewater treatment device, which forms an integrated wastewater treatment device with a sedimentation zone arranged between an anaerobic zone (or anoxic zone or other functional zones) and an aerobic zone.

[0034] (11) The present invention provides a moving bed biofilm wastewater treatment device, which adopts a flow channel connection method from a biochemical tank to a sedimentation tank. Through the inclined flow channel arrangement, the mixed fluid entering the sedimentation tank is separated into solid, liquid and gas phases, which enhances the sedimentation effect and improves the quality of the effluent. Attached Figure Description

[0035] To more clearly illustrate the technical solutions of the exemplary embodiments of the present invention, the accompanying drawings used in the embodiments will be briefly described below. It should be understood that the following drawings only show some embodiments of the present invention and should not be considered as a limitation of the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort. In the drawings:

[0036] Figure 1 A schematic diagram of a wastewater treatment device according to an embodiment of the present invention;

[0037] Figure 2 This is a front view of a wastewater treatment device according to an embodiment of the present invention;

[0038] Figure 3 An axonometric view of a wastewater treatment device according to an embodiment of the present invention;

[0039] Figure 4 Another axial view of a wastewater treatment device according to an embodiment of the present invention.

[0040] The attached diagram shows the markings and corresponding component names:

[0041] Ⅰ-Anoxic zone, Ⅱ-Multifunctional zone, Ⅲ-Aerobic zone, Ⅳ-Sedimentation zone, 1-Inlet pipe, 2-Sludge bar, 3-Anoxic zone packing interception pipe, 4-Anoxic zone outlet pipe, 5-Suction device, 6-Aerobic zone inlet pipe, 7-Return pipe to anoxic zone, 8-First jet aerator, 9-Second jet aerator, 10-First valve, 11-First air pipe, 12-Second air pipe, 13-First diffuser, 14-Second diffuser, 15-Aerobic zone packing interception pipe, 16-Nitrified liquid return pipe, 17-Second valve, 18-Aerobic zone packing interception plate, 19-Flow channel, 20-Sludge return pipe, 21-Perforated sludge discharge pipe, 22-Third valve, 23-Inclined pipe, 24-Outlet water collection tank, 25-Outlet pipe, 26-Fourth valve. Detailed Implementation

[0042] To make the objectives, technical solutions, and advantages of the present invention clearer, the present invention will be further described in detail below with reference to the embodiments and accompanying drawings. The illustrative embodiments and descriptions of the present invention are only used to explain the present invention and are not intended to limit the present invention.

[0043] Example 1: This Example 1 provides a moving bed biofilm wastewater treatment device, such as... Figures 1-4 As shown, it includes an anaerobic zone I, a multifunctional zone II, a sedimentation zone IV, and an aerobic zone III arranged in sequence.

[0044] Packing material is added to both the facultative zone I and the aerobic zone III; the upper water level of the facultative zone I is connected to the upper water level of the multifunctional zone II through the facultative zone outlet pipe 4, and the inlet end of the facultative zone outlet pipe 4 is connected to the facultative zone packing interception pipe 3.

[0045] The bottom of the multi-functional zone II is equipped with a suction device 5. The suction device 5 is connected to the lower water level of the anoxic zone I through the return pipe 7 to the facultative zone, and to the lower water level of the aerobic zone III through the inlet pipe 6 of the aerobic zone. The aerobic zone inlet pipe 6 is also equipped with a first jet aerator 8, and the return pipe 7 to the facultative zone is also equipped with a second jet aerator 9.

[0046] The upper water level of aerobic zone III is connected to the lower water level of sedimentation zone IV through flow channel 19. Sedimentation zone IV is used to settle sludge and collect clean water. The upper end of flow channel 19 is sealed with aerobic zone packing interceptor plate 18.

[0047] The upper water level of aerobic zone III is connected to the upper water level of multifunctional zone II through nitrification liquid return pipe 16. The inlet end of nitrification liquid return pipe 16 is equipped with aerobic zone packing interception pipe 15.

[0048] Compared to existing technologies, although some engineering measures have been taken, the uniformity and mixing degree of the packing material still have certain problems, resulting in poor fluidization and a tendency for local enrichment of the packing material, especially in the effluent zone. At the effluent of the MBBR membrane reactor, grids, meshes, or perforated pipes are often installed to prevent packing material loss, but these are prone to clogging and require regular manual cleaning. Some designs also incorporate backflushing devices such as air pipes to prevent clogging, but these are energy-intensive and ineffective. This solution provides a moving bed biofilm wastewater treatment device. For details, please refer to [link to specific solution]. Figure 1The wastewater treatment device is divided into an anaerobic zone I, a multifunctional zone II, a sedimentation zone IV, and an aerobic zone III. Ananaerobic zones I and III are filled with packing material to enhance the treatment effect. A suction device 5, preferably a submersible pump, is located at the bottom of the multifunctional zone II in the middle. The pump sucks up the pre- and post-treatment wastewater and delivers it to the lower water levels of ananaerobic zones I and III via the return pipe 7 to the ananaerobic zone and the inlet pipe 6 to the aerobic zone. During transport, the wastewater is mixed with air by jet aerators on the pipes. A first jet aerator 8 is connected to a first air pipe 11, and a second jet aerator 9 is connected to a second air pipe 12. These jet aerators mix the wastewater with air to form an air-water mixture. The wastewater then enters the bottom of the MBBR reactor through the facultative zone return pipe 7 and the aerobic zone inlet pipe 6. There can be two aerobic zone inlet pipes 6, symmetrically arranged on both sides. Jet aerators are installed on all three pipes. The air is brought into the facultative zone I and aerobic zone III by the power provided by the water pump for aeration and suspension and mixing of the packing. That is, by using the power of the water pump and the power of the air-water mixture bubbles, a circulation is formed from the bottom to the top, which fully mixes with the packing in the MBBR tank, forming a fluidized state in which gas, solid and liquid are fully in contact. This allows the wastewater to fully contact the microorganisms and oxygen formed on the packing to remove pollutants such as BOD, COD and ammonia nitrogen from the wastewater. Furthermore, an anaerobic zone outlet pipe 4 is installed at the upper water level of anaerobic zone I to transport wastewater to multifunctional zone II, and a nitrification liquid return pipe 16 is installed at the upper water level of aerobic zone III to transport wastewater to multifunctional zone II. By utilizing the same side upper and lower optimization of the inlet and outlet, the overall circulation dynamics are strengthened. Aerobic zone III is then connected to the lower water level of sedimentation zone IV through flow channel 19, so that part of the wastewater in aerobic zone III flows back to multifunctional zone II through the upper nitrification liquid return pipe 16, and part enters sedimentation zone IV by gravity flow. Clear water is collected through sedimentation in sedimentation zone IV. A perforated sludge discharge pipe 21 is installed at the bottom of the sedimentation zone to discharge the remaining sludge. Finally, the wastewater is collected and discharged by the triangular weir outlet collection trough 24 located in the clear water zone of sedimentation zone IV.

[0049] In addition, in the above scheme, on the outlet pipes forming the circulation, namely the inlet end of the facultative zone outlet pipe 4, the inlet end of the nitrification liquid return pipe 16, and the upper end of the flow channel 19, there are respectively a facultative zone packing interception pipe 3, an aerobic zone packing interception pipe 15, and an aerobic zone packing interception plate 18, to intercept the packing and prevent it from entering the multifunctional zone II and the sedimentation zone IV. In order to make the aforementioned jet aeration and MBBR process better integrated, the system is combined with the MBBR process outlet and packing interception plate set at the upper part of the jet aeration inlet end, 0.5~0.8m below the liquid level. This arrangement of the inlet and outlet positions above and below strengthens the circumferential circulation fluidization effect formed by jet aeration. At the same time, the packing interception plate and packing interception pipe are set at the above outlet position, so as to effectively utilize the scouring effect of the circumferential flow formed by jet aeration to blow off the packing on the interception plate and interception pipe, avoiding blockage. The blown-off packing is mixed back into the reaction tank by the power of the inlet jet at the bottom, ensuring the secondary uniformity of the system packing. This involves using the circulating flow created by the jet aerator to hydraulically blow away the packing material, causing it to sink to the bottom. The packing material is then mixed again by the jet aerator at the bottom inlet, forming a circulating fluidized state. This avoids uneven packing material distribution and ensures the suspension of the packing material.

[0050] The above scheme aims to achieve the following: This process integrates the characteristics of suspended activated sludge and attached biofilm processes, leveraging the advantages of both while compensating for their disadvantages. Its main principle is that wastewater continuously flows through the reactor's packing material, forming a biofilm on the carrier. Microorganisms proliferate and grow on the biofilm, simultaneously degrading organic pollutants in the wastewater, thus purifying it. Its main features are as follows: ① High volumetric loading: Compared to the activated sludge process, adding biological packing material to the bioreactor significantly increases the effective biomass. Compared to the biofilm process, fluidized packing material significantly improves mass transfer. ② Simultaneous enhanced nitrogen and phosphorus removal: The MBBR process can achieve sludge age separation for different functional microorganisms within the same reactor. Suspended organisms are predominantly heterotrophic microorganisms with a shorter sludge age, which is beneficial for the removal of organic matter and phosphorus. Attached organisms are predominantly autotrophic microorganisms with a longer sludge age, which is beneficial for ammonia nitrification. ③ Strong resistance to shock loads: Firstly, the MBBR process has a large biomass, thus exhibiting strong resistance to shock loads. Secondly, the packing material does not flow across zones with the water flow, ensuring that the attached microorganisms remain in specialized conditions with high biological activity and reaction rates, which is beneficial for resisting shock loads. Thirdly, each reaction zone is a completely mixed area, and pollutants are immediately diluted upon entry, greatly reducing the impact of high-load pollutants. Fourthly, the flowing packing material increases the substrate mass transfer rate, thereby increasing the reaction rate. ④ Strong adaptability to harsh conditions: MBBR facilitates the screening and enrichment of various microorganisms and helps maintain bacterial activity. Macroscopically, the MBBR process still has good treatment effects under harsh water quality conditions such as low temperature, high salinity, and low substrate. ⑤ Good sludge settling performance: Due to the high proportion of inorganic matter in the aged and shed biofilm, the MBBR process has a high density and is easy to settle. Furthermore, the extracellular polymers of the biological materials are higher than those in activated sludge, resulting in contact flocculation effects, improving sludge aggregation and settling performance.

[0051] Please see Figure 2 In this embodiment, the upper water level of the anoxic zone I is connected to the main inlet pipe 1, and a slag-blocking grid 2 is provided at the outlet of the main inlet pipe 1; external sewage can enter the anoxic zone I through the main inlet pipe 1, and is blocked by the slag-blocking grid 2 to prevent foreign objects from entering.

[0052] Please see Figure 3 In this embodiment, a first diffuser 13 is provided at the outlet end of the aerobic zone inlet pipe 6, and a second diffuser 14 is provided at the outlet end of the facultative zone return pipe 7; a diffuser port is provided at the outlet of the pipe entering the MBBR reactor so that the gas-water mixed wastewater can be quickly and fully mixed and enter the reactor.

[0053] Example 2: This Example 2 is a further optimization based on Example 1, and can be used to adjust the liquid level difference between various regions.

[0054] Please see Figure 3 and Figure 4 As a specific implementation method for controlling the flow rate and aeration volume entering the facultative anaerobic zone I and the aerobic zone III, the following configuration is provided: a first valve 10 is provided on the return pipe 7 to the facultative anaerobic zone; in this embodiment, by installing the first valve 10 on the pipe entering the facultative anaerobic zone I, the first valve 10 is located in front of the jet aerator, thereby distributing the flow rate and aeration volume entering the facultative anaerobic zone I and the aerobic zone III by the opening degree.

[0055] Please see Figure 3 and Figure 4 Since the water levels in aerobic zone III and sedimentation zone IV are basically the same, to control the water level difference between aerobic zone III and multifunctional zone II, or between sedimentation zone IV and multifunctional zone II, a second valve 17 is installed on the nitrification liquid return pipe 16. In this embodiment, the second valve 17 is installed on the nitrification liquid return pipe 16, and the water level difference can be controlled by controlling the opening of the second valve 17. After a water level difference is formed between sedimentation zone IV and multifunctional zone II, the bottom sludge will spontaneously flow into multifunctional zone II through the sludge return pipe 20. According to the hydraulic orifice submerged outflow model, the relationship between the return flow rate and the water level difference is as follows:

[0056] ;

[0057] Wherein, Q—return sludge volume (m³) 3 / s); μ—flow coefficient, taken as 0.62 for submerged orifice outflow; A—orifice cross-sectional area (m²) 2 g—acceleration due to gravity, taken as 9.8 m / s² 2 H—Liquid level difference (m);

[0058] The liquid level difference H between sedimentation zone IV and multifunctional zone II can also be adjusted by regulating the pump's suction capacity, thereby controlling the amount of sludge returned, Q.

[0059] Example 3: In conventional integrated wastewater treatment devices, the wastewater (a three-phase mixture of gas, liquid, and solid) in aerobic zone III usually enters sedimentation zone IV through pipelines. The gas in the sedimentation zone IV cannot be separated in a timely and effective manner before entering the sedimentation zone IV. If the gas directly enters the sedimentation zone IV, it will cause sludge to float, which will affect the sedimentation effect and thus affect the effluent quality and the operating efficiency of sedimentation zone IV.

[0060] Therefore, this embodiment 3 is a further optimization based on embodiment 2, providing a specific optimized method for three-phase separation before sedimentation zone IV, gas separation through flow channel 19, and solid-liquid separation within sedimentation zone IV.

[0061] Please see Figure 2As a specific implementation method to reduce the enrichment of packing material, the aerobic zone packing interceptor plate 18 is set at an inclination, with the lower end of the aerobic zone packing interceptor plate 18 tilted toward the side of aerobic zone III. In this embodiment, the aerobic zone packing interceptor plate 18 is an orifice plate that closes the upper end of the flow channel 19. Its orifice diameter is φ16mm~φ20mm. The orifice plate is set at an inclination angle of 60° to reduce the enrichment of packing material at the orifice plate.

[0062] Please continue reading. Figure 2 As a specific implementation method to prevent gas from entering the sedimentation zone IV and affecting solid-liquid separation, the flow channel 19 is configured as follows: From top to bottom, the flow channel 19 includes a vertical section and an inclined section connected sequentially, with the lower end of the inclined section inclined towards the inside of the sedimentation zone IV. In this embodiment, the specific gas separation process is as follows: During the operation of the wastewater treatment device, the carrier packing in the aerobic zone III is intercepted by the packing interceptor plate. A portion of the solid (sludge), liquid (wastewater), and gas (bubbles formed by wastewater aeration) mixture passes through the packing interceptor plate and enters the sedimentation zone IV via the flow channel 19. The flow channel 19 is divided into a vertical section and an inclined section. Wastewater, activated sludge, and gas flow downwards. Most of the gas, due to its vertical upward velocity (which is greater than the downward velocity of the mixed fluid), gradually moves upwards and escapes through the holes in the packing interceptor plate. The baffle extended at the end of the flow channel 19 further blocks the remaining gas in the three-phase mixed fluid, causing it to escape along the upper interface of the flow channel 19, further preventing gas from entering the sludge storage area and buffer zone of the sedimentation zone IV and affecting solid-liquid separation. In practical applications, a typical device with a processing capacity of Q=250m³ / d is designed as follows:

[0063] The design flow rate of the wastewater treatment reactor is Q = 250 m³ / d, the reactor width is W = 3 m, and the width of the flow channel 19 is d = 0.2 m.

[0064] The calculated cross-sectional area of ​​channel 19 is S = W•d = 0.6㎡;

[0065] The flow velocity in channel 19 is V1 = Q•1000 / (24•3600•S) = 4.83 mm / s;

[0066] According to Stokes' law, when the bubble diameter is 0.05~0.01cm, the vertical upward velocity is 0.173~0.691cm / s, and the vertical upward flow velocity of the bubble is taken as v0=3mm / s;

[0067] The tilt angle of flow channel 19 is selected as α=33.7° (controlled within 30~45°);

[0068] The extension length L = V1•(S / tan(RADIANSα)) / (V0•cos(RADIANSα)) = 0.6m.

[0069] Please see Figures 2-4 As a specific implementation method to promote efficient mud-water separation in sedimentation zone IV, sedimentation zone IV is provided with perforated sludge discharge pipe 21, inclined pipe 23, and effluent collection tank 24 from bottom to top, with perforated sludge discharge pipe 21 located at the bottom of sedimentation zone IV; in this embodiment, sedimentation zone IV is divided into sludge storage zone, buffer zone, inclined pipe sedimentation zone, and clear water zone from bottom to top, and the specific solid-liquid separation process is as follows:

[0070] As the fluid flows downwards along channel 19, the activated sludge in the mixed fluid sheds the air bubbles formed by aeration, gradually undergoing flocculation, sedimentation, and concentration. Through this device, the heavier flocs settle and slide down the lower interface of channel 19, directly settling into the sludge storage area at the bottom of sedimentation zone IV. This reduces the impact on solid-liquid separation in the middle buffer zone. Simultaneously, due to the slow downward flow of the fluid, it does not affect sludge sedimentation in the storage zone. After entering the storage zone, the remaining suspended solid-liquid mixture flows upwards into the buffer zone. Under gravity, the solid and liquid gradually separate, forming a sludge buffer suspension layer in the buffer zone, which effectively flocculates and intercepts a portion of the sludge, causing it to form large flocs that settle downwards. The fluid continues to flow upwards through the inclined tube sedimentation zone, where further sedimentation occurs. The settled sludge flows downwards from the buffer zone back to the storage zone. After sedimentation, the wastewater is finally collected and discharged from the effluent collection tank 24 located in the clear water zone. Ultimately, a portion of the sludge is returned to the multi-functional zone II via the sludge return pipe 20, while the remaining sludge is discharged through the perforated sludge discharge pipe 21 at the bottom of the sludge storage zone. This scheme ensures efficient gas separation in the mixed fluid entering the sedimentation zone IV from the aerobic zone III, and utilizes the three-phase separation principle to form a suspended sludge layer, promoting efficient sludge-water separation in the sedimentation zone IV.

[0071] Please see Figure 3 and Figure 4 As a specific implementation method for sludge recirculation in the sludge storage area at the bottom of sedimentation zone IV, the following configuration is adopted: the lower water level of sedimentation zone IV is connected to the lower water level of multi-functional zone II through sludge recirculation pipe 20; the sludge recirculation pipe 20 is a short tapered pipe, with the opening at one end of the sludge recirculation pipe 20 closer to sedimentation zone IV being larger than the opening at the other end; in this embodiment, several sludge recirculation pipes 20 are set in the sludge storage area, and the sludge recirculation pipes 20 are connected to multi-functional zone II. Generally, 3 to 5 recirculation pipes are set at the bottom of sedimentation zone IV, using short tapered pipes. The side openings of the tank wall are relatively large to reduce clogging during the sludge recirculation process; the outlet openings are relatively small to increase the flow velocity, which is more conducive to the mixing of recirculated sludge with wastewater in multi-functional zone II; increasing the flow velocity also increases the head loss, which is more conducive to the formation of a liquid level difference.

[0072] Please see Figure 2As a specific implementation method to improve space utilization, the sedimentation zone IV is configured as follows: In this embodiment, the wastewater treatment device is divided into an anaerobic zone I, a multifunctional zone II, an aerobic zone III, and a sedimentation zone IV according to the process flow. Each process section is arranged horizontally and linearly. Through innovative design, the sedimentation zone IV is placed between the multifunctional zone II and the aerobic zone III. The side of the sedimentation zone IV is funnel-shaped. This combination allows the multifunctional zone II and the aerobic zone III to utilize the space on both sides of the lower part of the sedimentation zone IV, meeting the functional requirements of the sedimentation zone IV while improving space utilization. This process adds packing material to the anaerobic zone I and the aerobic zone III to improve treatment efficiency, increase process stability, and reduce reactor volume.

[0073] Working principle:

[0074] A moving bed biofilm wastewater treatment device includes a tank body composed of various process sections and a pipeline control system. The process flow is sequentially divided into an anoxic zone I, a multifunctional zone II, an aerobic zone III, and a sedimentation zone IV. Packing material is added to the anoxic zone I and aerobic zone III to provide a carrier for biofilm formation. Wastewater first enters the upper sludge-blocking screen 2 of the anoxic zone I through the main inlet pipe 1. The screen has a 3mm gap and mixes with the wastewater returning from the multifunctional zone II after sludge removal. The return wastewater pipe to the anoxic zone I is located at the lower part of the anoxic zone I, and its port is equipped with a perforated diffuser, i.e., a second diffuser 14, with an aperture of φ16mm~φ20mm. The anoxic zone effluent pipe 4 is located at the upper part of the anoxic zone I and is equipped with a perforated pipe, i.e., an anoxic zone packing material interception pipe 3, to intercept the packing material, with an aperture of φ16mm~φ20mm. After passing through the anoxic zone packing material interception pipe 3, the wastewater from the anoxic zone I enters the multifunctional zone II through the anoxic zone effluent pipe 4. Meanwhile, the flow entering the multifunctional zone II also includes wastewater returning from the aerobic zone III through the nitrification liquid return pipe 16 and sludge returning from the sedimentation zone IV. The submersible sewage pump located at the bottom of the multifunctional zone II, i.e. the suction device 5, sends the wastewater to the facultative zone I and the aerobic zone III by pressure flow. The submersible sewage pump outlet pipe 25 is divided into three pipes: one is the return pipe 7 to the facultative zone, and the other two are the inlet pipes 6 to the aerobic zone. The jet aerators installed on the three pipes, namely the first jet aerator 8 and the second jet aerator 9, bring air into the facultative zone I and the aerobic zone III respectively under the action of the outlet pressure flow. The first valve 10 is installed on the return pipe 7 to the facultative zone, and the flow rate and aeration rate entering the facultative zone I and the aerobic zone III can be controlled by adjusting the valve size. The aerobic zone inlet pipe 6 is located at the bottom, with a perforated diffuser device (first diffuser 13) at its port, with an orifice diameter of φ16mm~φ20mm. The outlet is located at the top, using an orifice plate (aerobic zone packing interceptor plate 18) for water outlet. The orifice is located in the upper half of the inclined plate, with an orifice diameter of φ16mm~φ20mm. The orifice plate is inclined at a 60° angle to reduce packing accumulation at the orifice plate. The nitrification liquid return pipe 16 is located above the outlet orifice plate, using a perforated pipe (aerobic zone packing interceptor pipe 15) to intercept the packing, with an orifice diameter of φ16mm~φ20mm. A second valve 17 is installed on the nitrification liquid return pipe 16 to control the return flow and the water level in aerobic zone III. Under the combined action of water and air flow, facultative zone I and aerobic zone III achieve aeration while simultaneously creating a circulating flow state. This suspends and agitates the packing material, and also flushes the packing material at the outlet, preventing it from accumulating at the outlet. Aerobic zone III enters sedimentation zone IV through a downward-sloping channel 19, which provides some gas-liquid separation. The separated gas can escape through the holes above the outlet orifice plate, preventing air blockage. This gas separation promotes sedimentation in sedimentation zone IV. A specially designed sludge return pipe 20 at the bottom of sedimentation zone IV returns sludge to multi-functional zone II under the influence of water level difference. A perforated sludge discharge pipe 21, with an orifice diameter of approximately φ18mm, is located at the bottom of the sludge storage hopper in sedimentation zone IV and is equipped with a third valve 22 for discharging excess sludge.The water entering the sedimentation zone IV flows upward from the buffer zone through the inclined pipe 23. Under the action of gravity, the solid and liquid gradually separate. A water collection tank 24 is set in the clear water zone above the sedimentation zone IV to collect the treated clear water. Finally, it is discharged through the water outlet pipe 25, and a fourth valve 26 is set on the water outlet pipe 25.

[0075] 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.

Claims

1. A moving bed biofilm wastewater treatment device, characterized in that, It includes the facultative anaerobic zone (Ⅰ), multifunctional zone (Ⅱ), precipitation zone (Ⅳ) and aerobic zone (Ⅲ) arranged in sequence. Both the facultative anoxic zone (Ⅰ) and the aerobic zone (Ⅲ) are filled with packing material; the upper water level of the facultative anoxic zone (Ⅰ) is connected to the upper water level of the multifunctional zone (Ⅱ) through the facultative anoxic zone outlet pipe (4), and the inlet end of the facultative anoxic zone outlet pipe (4) is connected to the facultative anoxic zone packing material interception pipe (3). The bottom of the multifunctional zone (II) is provided with a suction device (5). The suction device (5) is connected to the lower water level of the facultative zone (I) through the return pipe (7) to the facultative zone, and to the lower water level of the aerobic zone (III) through the inlet pipe (6) to the aerobic zone. The inlet pipe (6) to the aerobic zone is also provided with a first jet aerator (8), and the return pipe (7) to the facultative zone is also provided with a second jet aerator (9). The upper water level of the aerobic zone (Ⅲ) is connected to the lower water level of the sedimentation zone (Ⅳ) through the flow channel (19). The sedimentation zone (Ⅳ) is used to settle sludge and collect clean water. The upper end of the flow channel (19) is sealed with an aerobic zone packing interceptor plate (18). The upper water level of the aerobic zone (III) is connected to the upper water level of the multifunctional zone (II) through the nitrification liquid return pipe (16). The inlet end of the nitrification liquid return pipe (16) is provided with an aerobic zone packing interceptor pipe (15). The upper water level of the anoxic zone (Ⅰ) is connected to the main inlet pipe (1), and a slag-blocking grid (2) is provided at the outlet of the main inlet pipe (1). The outlet end of the aerobic zone inlet pipe (6) is provided with a first diffuser (13), and the outlet end of the facultative zone return pipe (7) is provided with a second diffuser (14). The return pipe (7) to the anoxic zone is equipped with a first valve (10); A second valve (17) is provided on the nitrated liquid return pipe (16); The flow channel (19) includes a vertical section and an inclined section connected in sequence from top to bottom, with the lower end of the inclined section inclined toward the inside of the sedimentation zone (Ⅳ).

2. The moving bed biofilm wastewater treatment device according to claim 1, characterized in that, The aerobic zone packing interceptor plate (18) is inclined, and the lower end of the aerobic zone packing interceptor plate (18) is inclined toward one side of the aerobic zone (Ⅲ).

3. The moving bed biofilm wastewater treatment device according to claim 1, characterized in that, The sedimentation zone (Ⅳ) is provided with a perforated sludge discharge pipe (21), an inclined pipe (23) and an outlet water collection tank (24) from bottom to top. The perforated sludge discharge pipe (21) is located at the bottom of the sedimentation zone (Ⅳ).

4. The moving bed biofilm wastewater treatment device according to claim 1, characterized in that, The lower water level of the sedimentation zone (Ⅳ) is connected to the lower water level of the multifunctional zone (Ⅱ) through the sludge return pipe (20); the sludge return pipe (20) is a short tapering pipe, and the opening of the sludge return pipe (20) near the sedimentation zone (Ⅳ) is larger than the opening of the other end.

5. A moving bed biofilm wastewater treatment device according to claim 1, characterized in that, The sedimentation zone (Ⅳ) is funnel-shaped.

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