Marine high-concentration powder carrier biological fluidized bed device

Abstract

The invention discloses a marine high-concentration powder carrier biological fluidized bed device, and aims to solve the problems of low denitrification efficiency, serious membrane pollution, carrier loss and difficult coordination of denitrification and dephosphorization in marine sewage treatment. The device adopts a vertical layered layout and is composed of a box body, a tubular membrane assembly, an aeration assembly, a hydrocyclone and an auxiliary control assembly, and a diatomite-iron carbon composite carrier is added into the box body. A gas-solid-liquid three-phase self-circulation flow field is formed through targeted aeration of an inner cavity of the tubular membrane, and the composite carrier realizes AOB / NOB enrichment and activity activation; the hydrocyclone has the functions of efficient carrier recovery (the recovery rate in 75 days is greater than or equal to 72.66%) and accurate sludge age regulation and control. The device is compact in space, low in energy consumption, high in impact resistance and suitable for ship jolting and low-temperature low-C / N-ratio water quality, the service life of the membrane is prolonged by 50%, the TN removal rate can be larger than or equal to 85% and the TP removal rate can be larger than or equal to 90% without an external carbon source, the sewage discharge standard of the international maritime organization is met, and an efficient and stable integrated solution is provided for ship sewage treatment.

Description

Technical Field

[0001] This invention relates to the field of marine sewage treatment technology, specifically to a marine high-concentration powder carrier biological fluidized bed device. Background Technology

[0002] The main pollutants in domestic wastewater treatment include chemical oxygen demand (COD), total nitrogen (TN), and total phosphorus (TP). COD removal is generally relatively easy, and TP can be stably controlled by adding chemical phosphorus removal agents. However, TN removal is more complex. In recent decades, more efficient (removal rate) and faster (reaction rate) nitrogen removal technologies have become a research hotspot in the field of domestic wastewater treatment.

[0003] The limited nitrogen removal efficiency stems primarily from the limitations of nitrification. Despite the emergence of several novel nitrogen removal metabolic pathways, nitrification-denitrification remains the most widely used process globally. The key functional bacteria in nitrification are ammonia-oxidizing bacteria (AOB) and nitrite-oxidizing bacteria (NOB), but AOB and NOB have long cultivation periods, low metabolic rates, and are more sensitive to temperature changes. Currently mature technologies include membrane bioreactors (MBR) and aerobic granular sludge systems (AGS). Both increase AOB and NOB content to improve nitrification efficiency, and by controlling dissolved oxygen (DO), they can achieve short-cut nitrification, simultaneous nitrification and denitrification, and even anaerobic ammonia oxidation. Although MBR and AGS differ in form, their core mechanism is the incremental addition of AOB and NOB—inorganic nutrient bacteria are more easily attached and cultivated.

[0004] However, in MBR engineering practice, due to the high viscosity of the mixed liquor in the reactor, the membrane is prone to fouling, requiring frequent replacement and cleaning, resulting in a short membrane lifespan. Limited by membrane replacement frequency and cleaning requirements, the reactor's operating costs are high. Furthermore, its energy consumption also contributes to high operating expenses. In addition, the formation of AGS and the membrane attachment cycle in MBR are lengthy, especially in actual wastewater treatment where AGS formation can take hundreds of days and may break down due to improper operation or external influences.

[0005] For the reasons mentioned above, it is necessary to propose a marine high-concentration powder carrier biological fluidized bed device to solve the above problems. Summary of the Invention

[0006] The purpose of this invention is to overcome the defects in the prior art and provide a marine high-concentration powder carrier biological fluidized bed device.

[0007] To achieve the above objectives, the technical solution of the present invention is as follows: A marine high-concentration powder carrier biological fluidized bed device, comprising: The housing constitutes the main body of the fluidized bed. Its interior is divided into a raw water zone, a gas-liquid mixing zone, and a tubular membrane module. The raw water zone is located at the top of the housing, the gas-liquid mixing zone is located at the bottom of the fluidized bed, and the tubular membrane module is located in the middle of the fluidized bed. The tubular membrane module divides the middle part of the fluidized bed into an upflow zone and a downflow zone. Activated sludge cultured with microorganisms and composite carrier particles with microbial biofilm are added to the housing. Tubular membrane module: includes a tube shell and a tubular membrane, with a clear water zone formed between the tube shell and the tubular membrane; the lower end of the tube shell is provided with an outlet connected to the clear water zone, and the upper end of the tube shell is provided with an air outlet connected to the clear water zone; the two ends of the tubular membrane are respectively connected to the raw water zone and the gas-liquid mixing zone, and the inside of the tubular membrane is an upflow zone for the activated sludge and carrier particles to rise and circulate. Aeration components: including aeration heads and gas regulating devices; the aeration heads are sealed and installed at the bottom of the fluidized bed, corresponding to the bottom of the tubular membrane cavity, so that the aeration is concentrated inside the tubular membrane tube; the gas regulating device is used to adjust the distance between the aeration heads and the bottom port of the tubular membrane. Hydrocyclone: ​​It includes an inlet, a supernatant outlet, and a sludge outlet. The inlet is connected to the gas-liquid mixing zone at the bottom of the housing. The supernatant outlet is connected to the bottom of the fluidized bed. The sludge outlet is connected to the downflow zone to form a reflux.

[0008] Furthermore, the composite carrier particles are diatomaceous earth and iron-carbon, the particle size of the carrier is 200-350μm, and the amount of carrier particles with microbial biofilm is 5-15% of the effective volume of the box.

[0009] Furthermore, diatomaceous earth is mixed with iron and carbon at a mass ratio of 7:3 to 8:2.

[0010] Furthermore, the aeration assembly also includes an air pump, a gas flow meter, and a pressure gauge; the aeration head is connected to the air pump via a gas regulating device and a gas flow meter, and a pressure gauge is provided at the outlet of the air pump.

[0011] Furthermore, the raw water zone is connected to the water inlet pump via an inlet pipe, and a level controller is installed in the raw water zone, which is connected to the water inlet pump.

[0012] Furthermore, the middle part of the box is also provided with an upper frame and a lower frame, and the upper and lower ends of the tubular membrane assembly are respectively set between the upper frame and the lower frame to form a fixed structure.

[0013] Furthermore, the outlet is connected to the discharge pump via an outlet pipe, and a vacuum pressure gauge is installed on the outlet pipe.

[0014] Furthermore, the air outlet is connected to an exhaust pipe, which is in communication with the outside air.

[0015] The advantages and beneficial effects of this invention are as follows: 1. High efficiency in synergistic nitrogen and phosphorus removal: The "diatomaceous earth + iron and carbon" composite carrier targets and enriches AOB / NOB and activates their activity. Combined with hydrocyclones to regulate sludge age (SRT<7 days), TN removal rate ≥85% and TP removal rate ≥90%. It is suitable for the low temperature and low C / N ratio water quality of ships and does not require the addition of external carbon sources.

[0016] 2. Significant inhibition of membrane fouling: The composite carrier reduces the concentration of suspended microorganisms and the viscosity of the mixed solution. Combined with the turbulent scouring inside the tubular membrane and the linkage control of the vacuum pressure gauge, the membrane life is extended by 50%, the backwashing frequency is reduced by 60%, and the operation and maintenance costs are greatly reduced.

[0017] 3. High efficiency in carrier recovery: The hydrocyclone is optimized for carriers of 200-350μm, with a 75-day recovery rate of ≥72.66%, avoiding the inconvenience of carrier replenishment in ship scenarios and reducing consumable costs.

[0018] 4. Strong marine adaptability: The vertically layered and compact layout occupies only 60% of the space of traditional MBR, without additional stirring devices, reducing energy consumption by 20% to 25%, and is resistant to turbulence and water ingress, meeting the space, power and maintenance needs of ships. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the process of a marine high-concentration powder carrier biological fluidized bed device according to the present invention. In the diagram: 1. Container; 2. Raw water zone; 3. Gas-liquid mixing zone; 4. ; 5. Upflow zone; 6. Downflow zone; 7. Shell; 8. Tubular membrane; 9. Clear water zone; 10. Outlet; 11. Air outlet; 12. Aerator head; 13. Gas regulating device; 14. Hydrocyclone; 15. Inlet; 16. Supernatant outlet; 17. Sludge outlet; 18. Air pump; 19. Gas flow meter; 20. Pressure gauge; 21. Inlet pipe; 22. Liquid level controller; 23. Upper frame; 24. Lower frame; 25. Outlet pipe; 26. Vacuum pressure gauge; 27. Exhaust pipe; 28. Discharge pump; 29. ​​Inlet pump. Detailed Implementation

[0020] The specific embodiments of the present invention will be further described below with reference to examples. These examples are only used to more clearly illustrate the technical solutions of the present invention and should not be construed as limiting the scope of protection of the present invention.

[0021] This invention relates to a marine high-concentration powder carrier biological fluidized bed device. Guided by the core requirements of "small size, impact resistance, easy maintenance, and low energy consumption" in marine applications, it adopts a "vertical layered layout + multi-functional component synergy" design to achieve integrated functions of "nitrogen and phosphorus removal synergy + membrane fouling control + efficient carrier recovery" in a compact space. The overall structure is built around the logic of "gas-solid-liquid three-phase self-circulation + targeted reaction + membrane separation + closed-loop reflux". Each component and functional area forms an organic whole to ensure stable and efficient operation under special marine conditions.

[0022] The housing 1 is fabricated to form a closed fluidized bed structure. The bottom of the housing 1 is conical, the middle and upper parts are cylindrical, and the top is sealed. The fluidized bed not only provides physical containment but also achieves process synergy through internal functional partitioning. Specifically, such as... Figure 1 As shown, the interior of the tank 1 is divided into a raw water zone 2, a gas-liquid mixing zone 3, and a tubular membrane 8 module installation area. The raw water zone 2 is located at the top of the tank 1, mainly responsible for receiving raw water and buffering influent fluctuations, while also providing a top return channel for the three-phase circulation. The gas-liquid mixing zone 3 is located at the bottom of the tank 1 and is the core area for aeration diffusion and initial three-phase mixing, providing power for the upflow circulation. The tubular membrane 8 module is vertically installed in the middle of the tank 1, dividing the middle of the tank 1 into an upflow zone 5 and a downflow zone 6, forming a natural circulating flow field. The middle of the tank 1 is equipped with... The upper frame 23 and the lower frame 24 provide stable support for the tubular membrane 8 assembly. The tubular membrane 8 assembly is a cylindrical structure arranged vertically between the upper frame 23 and the lower frame 24. The outer layer of the tubular membrane 8 assembly is the shell 7, and the inner layer is the tubular membrane 8. The closed annular space between the shell 7 and the tubular membrane 8 is the clear water zone 9, and the inner side of the tubular membrane 8 is the upflow zone 5. The upper frame 23 and the lower frame 24 can effectively cope with the vibration and turbulence during ship navigation, prevent the assembly from shifting or being damaged, and improve the impact resistance of the device. Inside the chamber 1, activated sludge cultured with microorganisms and composite carrier particles with microbial biofilm are added. This composite carrier is key to the device's functionality and is made by mixing diatomaceous earth and iron-carbon in a mass ratio of 7:3 to 8:2. The porous structure of diatomaceous earth has a specific surface area 1.5 to 2 times larger than that of traditional activated carbon, providing dedicated attachment sites for ammonia-oxidizing bacteria (AOB) and nitrite-oxidizing bacteria (NOB). The iron-carbon then produces Fe through a micro-electrolysis reaction. 2+ Fe 3+The weak electric field activates the activity of nitrogen metabolism-related enzymes, increasing microbial activity by more than 30%. Furthermore, the strong chemical inertness of diatomaceous earth ensures it does not affect the activity of residual sludge, making it suitable for the subsequent treatment needs of ship wastewater. The carrier particle size is strictly controlled between 200 and 350 μm. This particle size ensures stable suspension and circulation under aeration, preventing carrier deposition caused by ship turbulence, and also adapts to the separation conditions of the hydrocyclone 14, achieving efficient recovery. The carrier dosage is set at 5% to 15% of the effective volume of the tank 1, preferably 10%, and can be flexibly adjusted according to fluctuations in ship wastewater concentration to balance treatment efficiency and operating costs.

[0023] The tubular membrane module 8 is the core unit of the integrated "reaction-separation" system, consisting of a shell 7 and a tubular membrane 8. A closed clear water zone 9 is formed between the shell 7 and the tubular membrane 8 to collect the clear water that permeates through the membrane, preventing it from mixing with the raw water and ensuring stable effluent quality. The lower end of the shell 7 has an outlet 10 connected to the clear water zone 9, which is connected to a discharge pump 28 via an outlet pipe 25, enabling rapid discharge of treated clear water to meet the "small amount, multiple times" discharge requirements of ship sewage. The upper end of the shell 7 has an air outlet 11 connected to the clear water zone 9, which is connected to an exhaust pipe 27 to communicate with the outside air, allowing for timely discharge of excess gas generated by aeration, balancing the internal pressure of the tank 1, preventing pressure buildup in the ship's confined space, and preventing gas from forming airlocks on the membrane surface that would affect water production efficiency. The tubular membrane 8 has openings at both ends that connect to the raw water zone 2 and the gas-liquid mixing zone 3, respectively. An upflow zone 5 is formed inside the membrane, allowing activated sludge and carrier particles to rise and circulate under the aeration thrust. A downflow zone 6 is formed between the outer side and the inner wall of the tank 1, allowing the three-phase mixture to flow back under gravity, thus forming a complete circulation path. A vacuum pressure gauge 26 installed on the effluent pipe 25 can monitor the negative pressure inside the membrane in real time. During normal operation, it is controlled between -0.02 and -0.05 MPa. When the concentration of wastewater from the ship suddenly increases (such as a surge in pollutants due to concentrated water use by personnel), a rapid warning can be issued through changes in negative pressure, and the aeration intensity or the parameters of the hydrocyclone 14 can be adjusted accordingly to suppress membrane fouling in advance, reduce the frequency of membrane cleaning during ship navigation, and lower maintenance workload.

[0024] The aeration components are designed with "precise oxygen supply + energy-saving adaptation + shock resistance" in mind, perfectly suited to scenarios with limited ship power supply. The aeration heads 12 are sealed and installed at the bottom of the housing 1, corresponding one-to-one with the bottom of the tubular membrane 8's inner cavity. This concentrates aeration within the tubular membrane 8, creating an environment of "high oxygen concentration gradient + strong turbulent disturbance." This not only meets the aerobic requirements of AOB (Automatic Biological Oxygenation) systems but also forms a micro-anaerobic zone on the carrier surface, achieving simultaneous nitrification and denitrification, improving nitrogen removal efficiency. Simultaneously, the strong turbulence washes over the membrane surface, reducing pollutant adhesion. The gas regulating device 13 can flexibly adjust the distance between the aeration heads 12 and the lower end of the tubular membrane 8, controlling the range to 5–10 cm. This adapts to different ship navigation conditions (such as smooth navigation and turbulent navigation), ensuring uniform three-phase mixing. The aeration assembly also includes an air pump 18, a gas flow meter 19, and a pressure gauge 20. The aeration head 12 is connected to the air pump 18 via a gas regulating device 13 and the gas flow meter 19. The pressure gauge 20 at the outlet of the air pump 18 can monitor the air supply pressure in real time to prevent damage to the equipment due to excessive pressure. The gas flow meter 19 can accurately control the aeration intensity between 0.5 and 0.8 m. 3 / (m 2 •h) This method satisfies the metabolic needs of microorganisms while avoiding energy waste caused by excessive aeration, thus meeting the requirements for ship energy conservation.

[0025] The hydrocyclone 14 is the core functional component for realizing "carrier recovery + sludge age control + microbial renewal". Its inlet 15 is connected to the gas-liquid mixing zone 3 at the bottom of the housing 1, specifically in the upper part of the conical bottom of the fluidized bed; the supernatant outlet 16 is connected to the bottom of the fluidized bed, specifically near the lower tip of the conical bottom; and the sludge outlet 17 is connected to the downflow zone 6 to form a closed-loop reflux. For composite carriers of 200-350μm, the hydrocyclone 14 achieves efficient carrier recovery by optimizing the inlet pressure (0.15-0.25MPa) and the split ratio (10%-15%), with a recovery rate of 72.66%-82.50% within 75 days, avoiding increased costs and inconvenience in replenishment caused by carrier loss during ship navigation. Meanwhile, the hydrocyclone 14 utilizes centrifugal separation characteristics to quickly discharge low-activity flocculent sludge, controlling the sludge retention time to within 10 days, preferably less than 7 days, while retaining highly active attached microorganisms. This effectively resolves the contradiction between "long sludge age for nitrifying bacteria and short sludge age for phosphorus-removing bacteria," achieving synergistic nitrogen and phosphorus removal standards. Furthermore, the centrifugal shear force within the hydrocyclone can peel away the aging biofilm on the carrier surface, exposing fresh attachment sites, renewing the microbial community surface, and enhancing its adsorption and degradation capabilities, ensuring long-term stable operation of the device.

[0026] The design of auxiliary components provides crucial assurance for the stable operation of the device. Raw water zone 2 is connected to the inlet pump 29 via inlet pipe 21. The level controller 22 installed in raw water zone 2 forms a closed-loop linkage with the inlet pump 29, automatically adjusting the inlet flow rate to adapt to fluctuations in ship sewage discharge (such as changes in crew numbers or sailing times), preventing overflow due to excessively high water levels or ineffective aeration due to excessively low water levels in raw water zone 2, thus ensuring continuous and stable operation of the device. The exhaust pipe 27 promptly discharges excess gas from the clear water zone 9, balancing the pressure in tank 1 and ensuring a stable outlet flow rate, further enhancing the device's adaptability to the special environment of a ship.

[0027] This device has significant advantages in marine applications: its vertical layered layout and design without additional stirring devices reduce the space required by traditional membrane bioreactors (MBRs) to only 60%, perfectly suited to the limited installation space on ships; the linkage design of the level controller 22, gas regulating device 13, and hydrocyclone 14 effectively copes with ship turbulence, fluctuations in influent concentration, and unstable power supply, ensuring that the effluent meets standards; the membrane fouling control system and efficient carrier recovery design reduce the frequency of membrane cleaning and carrier replenishment, adapting to the characteristics of ships with "long maintenance cycles and limited personnel operation"; the self-circulating flow field and precise aeration control reduce energy consumption by 20% to 25% compared to traditional marine wastewater treatment equipment, meeting the energy-saving requirements of ships; the simultaneous nitrogen and phosphorus removal function (TN removal rate ≥85%, TP removal rate ≥90%) meets the discharge requirements of the International Maritime Organization MEPC.227(64) resolution and other relevant standards for simultaneous compliance of COD, TN, and TP in ship wastewater. Meanwhile, addressing the common low-temperature (10-15℃) and low C / N ratio (2-3) characteristics of ship wastewater, the iron-carbon components of the composite carrier can release a small amount of heat through micro-electrolysis, raising the local water temperature inside the membrane tube by 2-3℃ and promoting the permeability of microbial cell membranes. This reduces the inhibition of AOB / NOB metabolism by low temperatures. Traditional carriers experience a decrease of more than 40% in nitrifying bacteria activity at 10℃, while this device only experiences a 10% decrease. The porous structure of diatomaceous earth can adsorb trace amounts of organic carbon in the raw water and release it slowly. Combined with the degradation of recalcitrant organic matter by iron-carbon micro-electrolysis (increasing the BOD5 / COD ratio by 0.2-0.3), low-carbon wastewater can meet denitrification requirements without the need for external carbon sources, reducing operating costs by 15%-20%.

[0028] Example 1: Treatment of conventional shipboard sewage Device parameters: Box 1 is a cylindrical structure with a diameter of 1.8m, a total height of 4.5m, and an effective volume of 10m³. 3The tubular membrane module 8 is made of PVDF material, with a membrane pore size of 0.1μm, an inner diameter of 40mm, an outer diameter of 60mm, and a length of 2.2m. The tube shell 7 has an outer diameter of 80mm, an inner diameter of 70mm, and a length of 2.2m. A total of 5 modules are set up and fixed by the upper frame 23 and the lower frame 24 (spaced 2.2m apart). The lateral spacing between modules is 80mm. The composite carrier is diatomaceous earth-iron-carbon (mass ratio 7:3), with a particle size of 200-250μm and an addition rate of 1m³. 3 (Occupying 10% of the effective volume); Hydrocyclone 14: Diameter 200mm, Total height 600mm, Inlet pressure 0.15MPa, Flow split ratio 10%, Suction inlet 15: DN50, Supernatant outlet 16: DN40, Sludge outlet 17: DN32; Aeration components: 5 disc-type microporous aeration heads 12 (corresponding one-to-one with tubular membrane 8), Aeration intensity 0.5m 3 / (m 2 •h), the distance between the aeration head 12 and the lower end of the tubular membrane 8 is 5cm, and the air pump 18 is a marine silent air compressor (discharge capacity 1.0m³). 3 / min, working pressure 0.4MPa), with matching gas flow meter 19 (range 0~1.0m) 3 / (m 2 •h)) and pressure gauge 20 (range 0~0.6MPa), the outlet pressure of air pump 18 is stable at 0.3MPa; water inlet pump 29 is a marine self-priming pump (flow rate 5m 3 / h, head 15m), level controller 22 controls the level range of raw water zone 2 from 0.8 to 1.2m.

[0029] Influent water quality: COD=300~350mg / L, TN=40~45mg / L, TP=4~5mg / L, water temperature 20~25℃, C / N=5~6. The influent flow rate is controlled by the level controller 22 and the influent pump 29 to maintain the stability of the liquid level in the raw water zone 2.

[0030] Operational results: With a hydraulic retention time of 4 hours, the intramembrane negative pressure, monitored by vacuum pressure gauge 26, remained stable at -0.02 to -0.03 MPa; effluent COD = 20–25 mg / L, removal rate 92.9%–94.3%; TN = 5.2–6.8 mg / L, removal rate 84.4%–89.0%; TP = 0.3–0.4 mg / L, removal rate 90.0%–92.5%; 0.825 m³ of carrier was recovered via hydrocyclone 14 within 75 days. 3 The recovery rate reached 82.50%. No additional backwashing was required during operation. The device remained stable under conditions of smooth ship navigation and slight turbulence. The tubular membrane module 8 showed no displacement, no leakage from the seal, and no significant fluctuation in the quality of the effluent.

[0031] Example 2: Treatment of Low-Temperature, Low C / N Ratio Shipboard Domestic Wastewater Device parameters: Box 1 is a cylindrical structure with a diameter of 1.6m, a total height of 4.0m, and an effective volume of 8m³. 3 The parameters of the tubular membrane module 8 are the same as in Example 1, with a total of 4 groups. The lateral spacing between the modules is 80 mm, and they are fixed by the upper frame 23 and the lower frame 24 (spacing 2.0 m). The composite carrier is diatomaceous earth-iron-carbon (mass ratio 8:2), with a particle size of 250-350 μm and an addition rate of 0.8 m³. 3 (Occupying 10% of the effective volume); Hydrocyclone 14 has a diameter of 200mm, a total height of 600mm, an inlet pressure of 0.25MPa, a flow splitting ratio of 15%, and an interface diameter consistent with Example 1; The aeration assembly uses 4 disc-type microporous aeration heads 12 (corresponding one-to-one with the tubular membrane 8) with a diameter of 50mm, and an aeration intensity of 0.8m. 3 / (m 2 •h), the distance between the aeration head 12 and the lower end of the tubular membrane 8 is 10cm, and the air pump 18 is a marine silent air compressor (discharge capacity 1.2m³). 3 The flow rate is 100 m³ / min, and the working pressure is 0.4 MPa. It is equipped with a gas flow meter 19 and a pressure gauge 20. The outlet pressure of the air pump 18 is stable at 0.35 MPa. The inlet pump 29 is a marine self-priming pump (flow rate 4 m³ / min). 3 / h, head 15m), level controller 22 controls the level range of raw water zone 2 from 0.7 to 1.0m.

[0032] Inlet water quality: COD=180~220mg / L, TN=35~40mg / L, TP=3~4mg / L, water temperature 10~15℃, C / N=2~3, inlet water flow rate is controlled by the liquid level controller 22 in conjunction with the inlet water pump 29.

[0033] Operational results: Hydraulic retention time 6 hours; membrane negative pressure stable at -0.04 to -0.05 MPa; effluent COD 12–18 mg / L, removal rate 91.8%–94.4%; TN 5.0–6.5 mg / L, removal rate 83.8%–85.7%; TP 0.3–0.35 mg / L, removal rate 91.3%–92.5%; 0.581 m³ of carrier recovered within 75 days. 3 The recovery rate reached 72.66%, requiring only two backwashes (30 minutes each, using clean water). Energy consumption monitoring showed a 25% reduction compared to traditional marine MBRs, even during low-load operation at night (inlet flow rate reduced to 2m). 3 Even under conditions of moderate turbulence during navigation ( / h), the device maintained stable operation, with no exceedance of pollutant concentrations in the effluent and no significant loss of carriers.

[0034] The above description is only a preferred embodiment of the present invention. It should be noted that for those skilled in the art, several improvements and modifications can be made without departing from the technical principles of the present invention, and these improvements and modifications should also be considered within the scope of protection of the present invention.

Claims

1. A marine high-density powder carrier bioreactor fluidized bed apparatus, characterized by, Comprising The box constitutes the main body of the fluidized bed, which is divided into raw water area, gas-liquid mixing area and tubular membrane assembly inside. The raw water area is located at the upper part of the box, the gas-liquid mixing area is located at the bottom of the fluidized bed, and the tubular membrane assembly is located in the middle part of the fluidized bed. The tubular membrane assembly separates the middle part of the fluidized bed into upflow area and downflow area. The activated sludge cultured by microorganisms and the composite carrier particles with microbial biofilm are added into the box; The tubular membrane assembly includes a tube shell and a tubular membrane. The tube shell and the tubular membrane form a clear water area. The lower end of the tube shell is provided with a water outlet communicating with the clear water area, and the upper end of the tube shell is provided with an air outlet communicating with the clear water area. The two ends of the tubular membrane are open and communicate with the raw water area and the gas-liquid mixing area respectively. The inner side of the tubular membrane is the upflow area, which provides the activated sludge and the carrier particles for ascending circulation; The aeration assembly includes an aeration head and a gas adjusting device. The aeration head is sealingly installed at the bottom of the fluidized bed and corresponds to the position of the inner cavity bottom of the tubular membrane, so that the aeration is concentrated in the tube of the tubular membrane. The gas adjusting device is used to adjust the distance between the aeration head and the lower port of the tubular membrane. The hydrocyclone includes a suction inlet, a supernatant outlet and a sludge outlet. The suction inlet communicates with the gas-liquid mixing area at the lower part of the box, the supernatant outlet is connected to the bottom of the fluidized bed, and the sludge outlet communicates with the downflow area to form a backflow.

2. A marine high-density powder support bio-fluidized bed apparatus according to claim 1, characterized in that, The composite carrier particles are diatomite and iron-carbon. The particle size of the carrier is 200-350 μm, and the input amount of the carrier particles with microbial biofilm is 5-15% of the effective volume of the box.

3. A marine high-density powder support bio-fluidized bed apparatus according to claim 2, characterized in that, The diatomite and iron-carbon are mixed in a mass ratio of 7:3-8:

2.

4. A marine high-density powder support bio-fluidized bed apparatus according to claim 1, characterized in that, The aeration assembly further includes a gas pump, a gas flow meter and a gas pressure gauge. The aeration head is connected with the gas pump through the gas adjusting device and the gas flow meter. The outlet of the gas pump is provided with a gas pressure gauge.

5. A marine high-density powder support bio-fluidized bed apparatus according to claim 1, wherein, The raw water area is connected with the water inlet pump through the water inlet pipeline. A liquid level controller is arranged in the raw water area, and the liquid level controller is connected with the water inlet pump.

6. A marine high-density powder support bio-fluidized bed apparatus according to claim 1, characterized in that, An upper frame body and a lower frame body are further arranged in the middle part of the box. The upper and lower ends of the tubular membrane assembly are arranged between the upper frame body and the lower frame body to form fixation.

7. A marine high-density powder support bio-fluidized bed apparatus according to claim 1, characterized in that, The water outlet is connected to the discharge pump through the water outlet pipeline, and a vacuum pressure gauge is arranged on the water outlet pipeline.

8. A marine high-density powder support bio-fluidized bed apparatus according to claim 1, characterized in that, The air outlet is connected with an air exhaust pipeline which communicates with the outside air.

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