Integrated system for water pretreatment process

Abstract

The utility model relates to water supply treatment technical field especially relates to a kind of water supply pretreatment process integrated system, including the communication of buffer pool, granular sludge pool, reaction pool and biological fluidized pool in proper order, and the buffer pool is provided with water inlet, and the biological fluidized pool is provided with water outlet;The buffer pool is connected with powdered carbon dosing device, and the reaction pool is connected with ozone generator and hydrogen peroxide dosing device, and the top of reaction pool is provided with ozone collection device, and the ozone collection device collects the ozone tail gas of the top of reaction pool and is introduced into the bottom of buffer pool.The utility model is through the multistage cooperation of "biology-physical chemistry-biology", realizes the efficient removal of pollutants in cascade, reduces energy consumption and reagent cost simultaneously, improves system stability and effluent quality.

Description

Technical Field

[0001] This utility model relates to the field of water supply treatment technology, and in particular to an integrated system for water supply pretreatment process. Background Technology

[0002] Drinking water treatment is one of the major challenges facing the water treatment industry today. Traditional processes of coagulation, sedimentation, filtration, and disinfection are insufficient to meet increasingly stringent water supply demands. Current advanced treatment processes often suffer from high energy consumption, large footprints, and unsatisfactory treatment results. Furthermore, the removal of pollutants such as ammonia nitrogen and organic matter often requires multiple complex processes, and the lack of effective synergy and optimization between these processes leads to persistently high overall energy consumption, making it difficult to meet the demands for energy conservation, environmental protection, and high-quality water supply.

[0003] Aerobic granular sludge (AGS), as an emerging biological treatment technology, is widely used in wastewater treatment, but it also shows great potential in water treatment (especially in the pretreatment stage of slightly polluted water sources). It has high biomass and rich biological community, and can efficiently degrade organic matter through microbial metabolism. It can achieve simultaneous nitrification of ammonia nitrogen through the outer nitrifying bacteria community. In addition, the extracellular polymers (EPS) on the surface of the particles can adsorb some heavy metals (such as lead and cadmium) through ion exchange or complexation, which helps to improve water quality. However, existing innovations in water treatment technology are mostly focused on the optimization of a single process. For example, the patent "A Water Treatment Method Based on Granular Sludge Coupled with Biofilm Method for Flocculent Sludge" (authorization publication number CN116477794A) proposes a biological treatment system using granular sludge coupled with biofilm method. By using immobilized microorganism technology to increase sludge concentration, it achieves effective degradation of ammonia nitrogen and some biodegradable organic matter. However, this technology has the following defects: (1) the construction of microbial community lacks directional regulation, resulting in insufficient co-metabolism capacity of complex pollutants; (2) the three-phase mass transfer efficiency is limited, which restricts reaction kinetics; and (3) the retention rate of hydrophobic and difficult-to-degrade organic micropollutants is less than 40%.

[0004] Ozone catalytic oxidation and biochar granular sludge fluidized bed technology are currently the most mainstream advanced water purification processes. A patent for a drinking water pretreatment ozone oxidation device (authorization publication number CN220550044U) provides a drinking water pretreatment ozone oxidation device, including a reactor, a powdered carbon dosing system, and an ozone dosing system. It can remove pollutants and effectively control bromate formation; however, it only possesses activated carbon adsorption, catalysis, and advanced ozone oxidation effects, and its removal capacity for small molecule organic matter is insufficient, and ozone energy consumption is relatively high. A patent for a biological fluidized bed coupled with ozone oxidation water purification process for slightly polluted water sources (authorization publication number CN119161062A) first treats the water in a biological fluidized bed, then performs ozone oxidation, then enters an aeration tank, and subsequently enters the conventional treatment process. After biological treatment, ozone acts as a pre-sterilizer, preventing bacteria from entering subsequent stages. Furthermore, the biological treatment coupled with ozone oxidation can preferentially degrade organic matter while pretreating particulate matter. However, biological fluidized beds are sensitive to fluctuations in influent water quality. If the concentration or type of micropollutants changes significantly, it may lead to a decrease in the metabolic efficiency of microorganisms, affecting the degradation of organic matter. Furthermore, the aeration tank after biological treatment requires additional equipment support, which may increase construction and operation and maintenance costs. Utility Model Content

[0005] To address the shortcomings of existing technologies, the purpose of this utility model embodiment is to provide an integrated system for water pretreatment processes.

[0006] To achieve the above objectives, the present invention provides the following technical solutions:

[0007] An integrated water pretreatment system includes a buffer tank, a granular sludge tank, a reaction tank, and a biological fluidized bed connected in sequence. The buffer tank is provided with an inlet, and the biological fluidized bed is provided with an outlet. The buffer tank is externally connected to a powdered carbon dosing device, and the reaction tank is externally connected to an ozone generator and a hydrogen peroxide dosing device. An ozone collection device is provided at the top of the reaction tank, which collects ozone exhaust gas from the top of the reaction tank and circulates it into the bottom of the buffer tank.

[0008] Optionally, the inlet is located at the upper part of the buffer tank, the buffer tank and the granular sludge tank are completely separated, the lower part of the buffer tank and the lower part of the granular sludge tank are connected through a first pipeline, and a first inlet pump is installed on the first pipeline.

[0009] Optionally, a partition is provided between the granular sludge tank and the reaction tank, and the upper side of the partition has a gap, through which water from the granular sludge tank flows into the reaction tank.

[0010] Optionally, the bottom of the reaction tank and the bottom of the biological fluidized tank are connected by a second pipeline, the second pipeline is equipped with a second inlet pump, and the outlet is located at the top of the biological fluidized tank.

[0011] Optionally, the ozone generator and the hydrogen peroxide dosing device are both connected to the inlet of the jet injector, the inlet of the jet injector is also connected to the outlet of the jet pump, and the inlet of the jet pump and the outlet of the jet injector are both connected to the granular sludge tank.

[0012] Optionally, an aeration disc is provided at the bottom of the buffer tank, and the ozone collection device is connected to the aeration disc via a pipeline.

[0013] Optionally, the granular sludge tank is provided with a first support layer, and the upper part of the first support layer is filled with granular sludge.

[0014] Optionally, the bottom of the biological fluidized bed is provided with a second support layer, and the upper part of the second support layer is filled with a composite filler of coconut shell charcoal and coal charcoal.

[0015] Optionally, the first and second support layers are pebble support layers.

[0016] Optionally, the granular sludge has a particle size of 1.5-3.0 mm, a static filling height of 20-40 cm, a fluidization height of 1.0-1.5 m, and the compound filler has a particle size of 0.6-1.0 mm and a filling thickness of 1.5-3.0 m.

[0017] One or more technical solutions provided in the embodiments of this utility model have at least the following technical effects or advantages:

[0018] 1. This utility model's integrated water pretreatment system consists of a buffer tank, a granular sludge tank, a reaction tank, and a biological fluidized bed connected in series. Water flows into the buffer tank from the inlet and out of the biological fluidized bed. An external powdered carbon dosing device is connected to the buffer tank to add powdered carbon to the water as nuclei for the granular sludge. An external ozone generator and hydrogen peroxide dosing device are connected to the reaction tank to catalytically oxidize and degrade pollutants. An ozone collection device at the top of the reaction tank transports unreacted ozone exhaust gas to the aeration discs at the bottom of the buffer tank for exhaust gas reuse. This constructs a deeply coupled system of aerobic granular sludge-ozone catalytic oxidation-biochar fluidized bed, establishing a "biochemical-physicochemical oxidation-biochemical" cyclic metabolic treatment mode. In this system, powdered carbon is added as nuclei for aerobic granular sludge, and ozone exhaust gas aeration provides high dissolved oxygen, gradually forming aerobic granular sludge under upward hydraulic action. Aerobic granular sludge can simultaneously achieve ammonia nitrogen oxidation and biodegradable organic matter degradation, realizing the efficient cascade removal of pollutants. Furthermore, it can reduce the treatment load of the subsequent ozone biological fluidized bed process, decrease ozone dosage, extend the service life of biological activated carbon, and achieve energy conservation and consumption reduction. In addition, extracellular polymers and trace dissolved organic matter that may be generated during the metabolism of aerobic granular sludge can be removed in the subsequent ozone biological fluidized bed stage, avoiding the risk of disinfection byproducts and further improving system stability and effluent quality. The effective coupling and synergistic effect of aerobic granular sludge, ozone catalytic oxidation, and biochar granular sludge tank is highly practical and energy-saving.

[0019] 2. Adding powdered carbon to raw water can not only adsorb certain suspended substances, but also act as a nucleus for granular sludge in the aerobic granular sludge treatment stage, improving the degree of sludge granulation. In the ozone catalytic oxidation reaction stage, it can act as an ozone catalyst, improving the pollutant removal rate.

[0020] 3. Aerobic granular sludge can directly contact the microorganisms in the raw water, and the microbial population can be continuously renewed and proliferated. Compared with traditional biological fluidized beds, granular sludge ponds have higher biomass and more diverse species, and are more efficient at removing biodegradable pollutants.

[0021] 4. Aerobic granular sludge can further adsorb suspended matter in the raw water, replenish its own sludge volume, avoid excessive sludge loss affecting the operation, and avoid clogging problems in the subsequent biological fluidized bed caused by high concentration of suspended matter in the influent, thus reducing the backwashing frequency of biochar.

[0022] 5. Unreacted ozone exhaust gas from the ozone catalytic oxidation stage is directly recycled to the influent buffer stage, reducing waste while increasing dissolved oxygen in the raw water and ensuring stable metabolic reactions of aerobic granular sludge.

[0023] 6. Extracellular polymers and trace amounts of dissolved organic matter that may be generated from the metabolism of aerobic granular sludge can be removed in the subsequent ozone biological fluidized bed stage, avoiding the risk of disinfection byproducts and ensuring the stability of system operation.

[0024] 7. The microorganisms in the aerobic granular sludge utilize dissolved oxygen in the raw water to efficiently convert ammonia nitrogen into harmless substances such as nitrate through biological processes such as nitrification. It can also achieve preliminary and effective removal of biodegradable organic pollutants. As the concentration of pollutants in the influent decreases in the subsequent reaction tank, the amount of ozone added can be reduced accordingly (saving about 20% to 30%), and the regeneration frequency of the biological fluidized bed can also be reduced, further reducing operating costs.

[0025] 8. This invention achieves efficient removal of pollutants in stages through multi-level synergy of "biological-physicochemical-biological" processes, while reducing energy consumption and reagent costs, improving system stability and effluent quality. It is especially suitable for the pretreatment of water sources with high organic matter, high ammonia nitrogen, or trace pollutants, as well as for the upgrading and renovation of existing water plants.

[0026] Additional advantages of this invention will be set forth in the description which follows, and in part will be obvious from the description or may be learned by practice of the invention. Attached Figure Description

[0027] The accompanying drawings, which form part of this specification, are used to provide a further understanding of this utility model. The illustrative embodiments and descriptions of this utility model are used to explain this utility model and do not constitute an undue limitation thereof. Furthermore, the spacing or dimensions between components are exaggerated to show their positions; the schematic diagrams are for illustrative purposes only.

[0028] Figure 1 This is a schematic diagram of the integrated water pretreatment process system provided in this embodiment of the utility model;

[0029] In the diagram: 1. Inlet; 2. Powdered activated carbon dosing device; 3. Aeration disc; 4. Buffer tank; 5. First inlet pump; 6. Ozone generator; 7. Jet pump; 8. Jet ejector; 9. Second inlet pump; 10. Hydrogen peroxide dosing device; 11. Granular sludge tank; 12. Reaction tank; 13. Ozone collection device; 14. Air compressor; 15. Second support layer; 16. Biological fluidized bed; 17. Outlet; 18. First support layer; Detailed Implementation

[0030] It should be noted that the following detailed description is illustrative and intended to provide further explanation of the present invention. Unless otherwise specified, all technical and scientific terms used in this invention have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0031] like Figure 1 As shown, this embodiment proposes an integrated water pretreatment process system, including a buffer tank 4, a granular sludge tank 11 (granular sludge fluidized bed), a reaction tank 12, and a biological fluidized bed 16 connected in sequence. The buffer tank 4 is provided with an inlet 1, and the biological fluidized bed 16 is provided with an outlet 17. The buffer tank 4 is externally connected to a powdered activated carbon dosing device 2, and the reaction tank 12 is externally connected to an ozone generator 6 and a hydrogen peroxide dosing device 10. An ozone collection device 13 is provided at the top of the reaction tank 12, which collects the ozone exhaust gas at the top of the reaction tank 12 and introduces it into the bottom of the buffer tank 4. The powdered activated carbon dosing device 2, the ozone generator 6, the hydrogen peroxide dosing device 10, and the ozone collection device 13 all adopt existing structures and are obtained through external purchase.

[0032] This embodiment is based on the synergistic effect of "adsorption-physicochemical-biochemical" processes. Through deep coupling of multiple technology units and precise parameter control, a highly efficient drinking water pretreatment process system for removing pollutants is constructed. Its technical principle is as follows:

[0033] Raw water enters buffer tank 4, where powdered activated carbon is added. Ozone aeration generates sufficient dissolved oxygen. The water then enters granular sludge tank 11 for treatment. Under upward hydraulic action, the sludge utilizes the powdered activated carbon as nuclei and forms aerobic granular sludge under sufficient dissolved oxygen conditions. This aerobic granular sludge specifically adsorbs hydrophobic organic pollutants through hydrophobic interactions, and is coated with nitrifying and heterotrophic bacteria, forming an "adsorption-co-metabolism" coupled degradation pathway, simultaneously achieving ammonia nitrogen oxidation and biodegradable organic matter degradation. The treated water flows into reaction tank 12, where ozone and a catalyst decompose or mineralize organic pollutants. It then enters biological fluidized bed 16, where it is further purified through the synergistic effect of biochar adsorption and biodegradation. Finally, residual impurities are removed in the conventional treatment module, resulting in high-quality water supply.

[0034] Among them, the powdered charcoal is coconut shell charcoal (wood 200 mesh), and the dosage is 1.0-5.0 mg / L. The ozone collection device 13 maintains the dissolved oxygen in the buffer tank 4 to be greater than 10 mg / L. The granular sludge tank 11 uses aerobic granular sludge as the biological fixation "medium". The granular sludge is maintained in a fluidized state under the hydraulic action of upward flow. The upward flow velocity is controlled at 15-25 m / h, and the hydraulic retention time (HRT) is 4-12 min.

[0035] The inlet 1 is located at the upper part of the buffer tank 4. The buffer tank 4 and the granular sludge tank 11 are completely separated. The lower part of the buffer tank 4 is connected to the lower part of the granular sludge tank 11 through a first pipeline, on which a first inlet pump 5 is installed. Water entering from the upper part of the buffer tank 4 reduces water flow disturbance and ensures uniform dispersion of the powdered carbon. Water exiting from the lower part is pumped to the granular sludge tank 11 by the inlet pump, ensuring stable hydraulic conditions. The completely separated design prevents back-mixing of pollutants between the buffer tank 4 and the granular sludge tank 11, protecting the environment for granular sludge formation.

[0036] A partition is provided between the granular sludge tank 11 and the reaction tank 12. The upper side of the partition has gaps, through which water from the granular sludge tank 11 flows into the reaction tank 12. Utilizing gravity flow reduces energy consumption, maintains the hydraulic gradient, helps the granular sludge tank 11 remain in a fluidized state, and promotes sludge maturation.

[0037] The bottom of the reaction tank 12 and the bottom of the biological fluidized bed 16 are connected by a second pipeline, on which a second inlet pump 9 is installed. The outlet 17 is located at the top of the biological fluidized bed 16. Water effluent from the bottom of the reaction tank 12 is pumped up to the bottom of the biological fluidized bed 16 by the inlet pump, forming an upward flow that fully fluidizes the packing material. The outlet 17 at the top of the biological fluidized bed 16 facilitates the collection of purified water and prolongs the contact time between the water flow and the packing material, thereby improving adsorption and biodegradation efficiency.

[0038] The ozone generator 6 and the hydrogen peroxide dosing device 10 are both connected to the inlet of the jet injector 8. The inlet of the jet injector 8 is also connected to the outlet of the jet pump 7. The inlet of the jet pump 7 and the outlet of the jet injector 8 are both connected to the granular sludge tank 11.

[0039] The jet injector 8 mixes ozone and hydrogen peroxide under negative pressure and then sends the mixture into the granular sludge tank 11, enhancing ozone utilization and oxidation effect. The gas-liquid mixing function of the jet injector 8 promotes ozone diffusion, strengthens the oxidation reaction in the granular sludge tank 11, improves pollutant removal efficiency, and simultaneously uses ozone exhaust gas to aerate the buffer tank 4, optimizing system operation.

[0040] The jet injector 8 adopts the device described in patent CN220579038U. The jet injector 8 is a self-pulse cavitation jet injector 8, with an ozone dosage of 2.0 to 6.0 mg / L, a gas-liquid contact time of 3 to 20 min, and an ozone / hydrogen peroxide dosage ratio of 10:1 to 2:1.

[0041] An aeration disc 3 is installed at the bottom of the buffer tank 4, and the aeration disc 3 is connected to an air compressor 14, which is connected to the ozone collection device 13. The ozone collection device 13 at the top of the reaction tank 12 collects unreacted ozone exhaust gas and transports it through pipelines to the aeration disc 3 at the bottom of the buffer tank 4, realizing ozone recycling. This not only reduces ozone emission waste but also provides dissolved oxygen (>10mg / L) to the buffer tank 4, maintaining an aerobic environment, promoting the adsorption of powdered carbon and the subsequent formation of granular sludge, ensuring treatment effect, and enhancing the environmental friendliness and economy of the system.

[0042] The granular sludge tank 11 is provided with a first support layer 18, on which granular sludge is filled. The first support layer 18 prevents the granular sludge from being lost and evenly distributes the water flow, ensuring a stable upward flow velocity (15-25 m / h). The granular sludge has a particle size of 1.5-3.0 mm, preferably 2.0-2.5 mm, a sludge volume index (SVI) of ≤40 mL / g, approximately 32-36 mL / g, and a biomass MLSS of approximately 60-70 kg / m³. 3 The preferred granular sludge (60-67) has a filling height of approximately 20-40 cm and a fluidization height of approximately 1.0-1.5 m. The high biomass and rich microbial community of the granular sludge enable efficient ammonia nitrogen oxidation and organic matter degradation. However, if the support layer particle size is too small, it may lead to clogging.

[0043] The bottom of the biological fluidized bed 16 is provided with a second support layer 15. The upper part of the second support layer 15 is filled with a compound filler of coconut shell charcoal and coal charcoal (mass ratio 1:1, iodine value ≥900mg / g, particle size 0.6-1.0mm), with a filling thickness of 1.5-3.0m. The bottom is provided with a pebble support layer (thickness 300mm). The contact time between the biological fluidized bed 16 and water is 5-20min, the expansion rate is 30%-50%, and a circulation pump is provided to maintain the fluidized state.

[0044] The first support layer 18 and the second support layer 15 are pebble support layers (particle size 20-40mm, thickness 100mm). The pebble support layer has good permeability and mechanical strength, which can effectively support the upper packing material and prevent it from being lost. At the same time, it can ensure uniform water flow distribution, reduce the impact of water flow on the bottom of the pool, ensure stable operation of the treatment unit, extend the service life of the system, and ensure the water purification effect.

[0045] This system, through deep coupling of functional units and precise parameter control, can effectively reduce energy consumption and save costs (30% reduction in operating cost per ton of water) while maintaining a high pollutant removal rate, and the effluent quality meets the limit requirements of GB5749-2022.

[0046] Work process:

[0047] Raw water enters from the top of buffer tank 4 and connects to the bottom inlet 1 of granular sludge tank 11. A powdered activated carbon dosing device 2 is installed at the bottom, with a powdered activated carbon dosage of 1.0-5.0 mg / L. An aeration disc 3 extends into the bottom of buffer tank 4 to maintain dissolved oxygen levels greater than 10 mg / L. The bottom of granular sludge tank 11 is filled with a first support layer 18. Above the first support layer 18 are granular sludge and suspended sludge zones. The static filling height of the sludge layer is approximately 20-40 cm, and the fluidization height is approximately 1.0-1.5 m. During the start-up phase, raw water with added powdered activated carbon and ozone-enriched tail gas is continuously introduced into the aerobic granular sludge tank 11. Under appropriate hydraulic shear force, microorganisms use the powdered activated carbon as nuclei to form aerobic granular sludge. Over time, the granular sludge gradually matures and becomes fluidized under hydraulic conditions. The hydraulic retention time in granular sludge tank 11 is 4-12 minutes. Water enters from the top of reaction tank 12, where ozone catalytic oxidation takes place. The water depth in reaction tank 12 is no less than 9m. Ozone / hydrogen peroxide is added from the bottom via cavitation jet injector 8, creating gas-water convection to improve ozone utilization. The ozone dosage is 2.0–5.0 mg / L, the contact time between ozone and water is 5–20 min, and the ozone / hydrogen peroxide dosage ratio is 10:1–2:1. Next, water is pumped from the lower outlet 17 of reaction tank 12 into biological fluidized bed 16. Biological fluidized bed 16 uses a bottom inlet and top outlet design, with a bottom support layer. The packing material is a mixture of coconut shell charcoal and coal-based charcoal granules in a 1:1 ratio, with a particle size of 0.6–1.0 mm and a packing thickness of 1.5–3.0 m. The contact time between biological fluidized bed 16 and water is 3–20 min, and the expansion rate is 30%–50%.

[0048] Example 1

[0049] An integrated water pretreatment system includes a buffer tank 4, a granular sludge tank 11, a reaction tank 12, and a biological fluidized bed 16 connected in sequence. The inlet 1 of the integrated system is located at the top of the buffer tank 4, and the outlet 17 of the integrated system is located at the top of the biological fluidized bed 16.

[0050] The buffer tank 4 adopts a top inlet and bottom outlet, with a powdered carbon dosage of 3 mg / L and dissolved oxygen greater than 10 mg / L. The effluent enters the granular sludge tank 11.

[0051] The granular sludge tank 11 adopts a bottom inlet and top outlet design, with a static sludge layer height of approximately 25 cm and a hydraulic retention time of 5 minutes. The effluent enters the reaction tank 12. The aerobic granular sludge has a particle size of 2.0 mm and a MLSS of 60 kg / m³. 3 The SVI30 concentration is 32 mL / g. The reaction tank 12 has a top inlet and a bottom outlet. Ozone is added through a self-excited pulse cavitation jet 8. The ozone dosage in the reaction tank 12 is 3 mg / L, the hydrogen peroxide dosage is 0.6 mg / L, the contact time between ozone / hydrogen peroxide and water is 5 min, and the effluent enters the biological fluidized tank 16.

[0052] The biological fluidized bed 16 adopts a bottom inlet and top outlet, including a support layer and an activated carbon packing layer. The packing is a mixture of coconut shell carbon and coal-based carbon granules with a mixing ratio of 1:1 and a particle size of 0.6 mm. The biological fluidized bed 16 has a contact time with water of 5 minutes and an expansion rate of 35%.

[0053] The process described in Example 1 was used to treat a slightly polluted water source (permanganate index: 4.35 mg / L, ammonia nitrogen: 0.96 mg / L, particle count: 8342 CNT / ml, turbidity: 11.03 NTU). The effluent entered a mixing + flocculation sedimentation + filtration process. Testing showed that the average permanganate index of the aerobic granular sludge effluent was 3.2 mg / L, and the average ammonia nitrogen was 0.4 mg / L; the average permanganate index of the filtered effluent was 0.52 mg / L, the average ammonia nitrogen was 0.02 mg / L, the average particle count was 56 CNT / ml, the average turbidity was 0.032 NTU, and the average total bacterial count was 83 CFU / ml. The effluent quality met and exceeded the "Standards for Drinking Water Quality" (GB5749-2022).

[0054] Comparative Example 1

[0055] The difference from Example 1 is that a slightly polluted source water (permanganate index: 5.42 mg / L, ammonia nitrogen: 0.98 mg / L, particle count: 8002 CNT / ml, turbidity: 10.18 NTU) was treated using the existing ozone-hydrogen peroxide advanced oxidation biological fluidized bed 16 process. The ozone dosage was 3.0 mg / L and the hydrogen peroxide dosage was 0.6 mg / L. The effluent entered a mixing + flocculation sedimentation + filtration process. After testing, the average permanganate index of the effluent was 1.58 mg / L, the ammonia nitrogen was less than 0.1 mg / L, the average particle count was 112 CNT / ml, the average turbidity was 0.092 NTU, and the average total bacterial count was 99 CFU / ml.

[0056] The effluent sampling and testing results of Example 1 show that the granular sludge tank 11 in this invention can effectively remove ammonia nitrogen and initially remove biodegradable organic pollutants such as TOC. Furthermore, it can reduce the treatment load of the subsequent ozone biological fluidized bed 16 process, reduce the ozone dosage, and extend the service life of the biological activated carbon.

[0057] By comparing the effluent sampling and testing results of Example 1 and Comparative Example 1, it can be found that the present invention can effectively improve the removal effect of organic matter and ammonia nitrogen in water, and also improve the removal rate of turbidity, particle number, etc. to varying degrees. The aerobic granular sludge process and the ozone biological fluidized bed 16 process work synergistically to enhance the effect, which is highly practical and energy-saving.

[0058] Although the specific embodiments of the present utility model have been described above in conjunction with the accompanying drawings, this is not intended to limit the scope of protection of the present utility model. Those skilled in the art should understand that various modifications or variations that can be made by those skilled in the art without creative effort based on the technical solution of the present utility model are still within the scope of protection of the present utility model.

Claims

1. An integrated system for water pretreatment processes, characterized in that, It includes a buffer tank, a granular sludge tank, a reaction tank and a biological fluidized bed connected in sequence. The buffer tank is provided with an inlet and the biological fluidized bed is provided with an outlet. The buffer tank is connected to an external powdered carbon dosing device, and the reaction tank is connected to an external ozone generator and a hydrogen peroxide dosing device. An ozone collection device is installed at the top of the reaction tank, which collects the ozone exhaust gas at the top of the reaction tank and circulates it into the bottom of the buffer tank.

2. The integrated water pretreatment system as described in claim 1, characterized in that, The inlet is located at the upper part of the buffer tank. The buffer tank and the granular sludge tank are completely separated. The lower part of the buffer tank is connected to the lower part of the granular sludge tank through a first pipeline, and a first inlet pump is installed on the first pipeline.

3. The integrated water pretreatment system as described in claim 1, characterized in that, A partition is provided between the granular sludge tank and the reaction tank. The upper side of the partition has a gap, through which water from the granular sludge tank flows into the reaction tank.

4. The integrated water pretreatment system as described in claim 1, characterized in that, The bottom of the reaction tank and the bottom of the biological fluidized tank are connected by a second pipeline, on which a second inlet pump is installed, and the outlet is located at the top of the biological fluidized tank.

5. The integrated water pretreatment process system as described in claim 1, characterized in that, The ozone generator and the hydrogen peroxide dosing device are both connected to the inlet of the jet injector. The inlet of the jet injector is also connected to the outlet of the jet pump. The inlet of the jet pump and the outlet of the jet injector are both connected to the granular sludge tank.

6. The integrated water pretreatment process system as described in claim 1, characterized in that, An aeration disc is installed at the bottom of the buffer pool, and the aeration disc is connected to an air compressor, which is connected to the ozone collection device.

7. The integrated water pretreatment process system as described in claim 1, characterized in that, The granular sludge tank is provided with a first support layer, and the upper part of the first support layer is filled with granular sludge.

8. The integrated water pretreatment system as described in claim 7, characterized in that, The bottom of the biological fluidized bed is provided with a second support layer, and the upper part of the second support layer is filled with a compound filler of coconut shell charcoal and coal charcoal.

9. The integrated water pretreatment process system as described in claim 8, characterized in that, The first and second support layers are cobblestone support layers.

10. The integrated water pretreatment process system as described in claim 8, characterized in that, The granular sludge has a particle size of 1.5-3.0 mm, a static filling height of 20-40 cm, a fluidization height of 1.0-1.5 m, and the compound filler has a particle size of 0.6-1.0 mm and a filling thickness of 1.5-3.0 m.

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