CN118005237A - Treatment method and device for polycyclic aromatic hydrocarbon in urban drainage overflow pollution - Google Patents
Treatment method and device for polycyclic aromatic hydrocarbon in urban drainage overflow pollution Download PDFInfo
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- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The application relates to the technical field of urban drainage pipe network overflow sewage treatment, in particular to a method and a device for treating polycyclic aromatic hydrocarbon in urban drainage overflow pollution. The application provides a treatment method of polycyclic aromatic hydrocarbon in urban drainage overflow pollution, which comprises the following steps: s1: screening urban drainage overflow sewage to remove solid matters to obtain first treated water; s2: pre-panning the first treated water to obtain second treated water; s3: placing the second treated water in an anoxic environment and an aerobic environment for reaction to obtain third treated water; s4: reacting the third treated water with a coagulant and a flocculant, and removing the precipitate to obtain fourth treated water; s5: and (3) treating the fourth treated water by micro-nano bubbles, ozone and a catalyst to obtain water from which the polycyclic aromatic hydrocarbon is removed. The application adopts the coagulation and multistage AO pool and micro-nano bubble ozone to achieve the purpose of controlling the polycyclic aromatic hydrocarbon in the overflow pollution of the urban drainage pipe network, and the combined process has high removal efficiency and cost saving, and can be widely used.
Description
Technical Field
The application relates to the technical field of urban drainage pipe network overflow sewage treatment, in particular to a method and a device for treating polycyclic aromatic hydrocarbon in urban drainage overflow pollution.
Background
The overflow water of the urban drainage pipe network refers to that when a rainy season comes, the water quantity exceeds the transportation capacity of the drainage pipe network, and sewage is directly discharged through overflow of a drainage system. At this time, the water body contains a large amount of pollutants, mainly including organic matters, TP (total phosphorus), TN (total nitrogen), SS (solid suspended solids), pathogenic microorganisms, heavy metals, polycyclic Aromatic Hydrocarbons (PAHs) and the like.
PAHs are an environmental pollutant with strong carcinogenicity, have multiple homologs, and toxicity is often the result of the synergistic effect of the multiple homologs, 7 of the 16 PAHs listed by USEPA as the pollutant for preferential control are recognized as being strong in carcinogenicity, including benzo [ a ] anthracene, benzo [ a ] pyrene, benzo [ b ] fluoranthene, benzo [ k ] fluoranthene, dro, dibenzo [ a, h ] anthracene, indeno [1,2,3-cd ] pyrene.
For the urban drainage pipe network overflow water end treatment process, a rapid coagulating sedimentation and high-efficiency fiber filter combined process is generally adopted, the removal rate of SS, COD (chemical oxygen demand) and TP can reach more than 80%, 50% and 80%, and most of insoluble pollutants can be removed.
In addition, the method can also be used for reducing the pollution of the overflow sewage to the water body by adopting an activated sludge process, for example, a sewage treatment plant in a great Yangtze river protection project adopts an equipped pure membrane MBBR system to treat the overflow sewage. The system adopts two operation modes of rainy season and dry season, and the average concentration of effluent COD, ammonia nitrogen, TP and SS is 30mg/L, 3mg/L, 0.5mg/L and 10mg/L respectively. The pollution is greatly reduced, the pollutant enters the natural water body through the overflow effect, and the occurrence of black and odorous water body is controlled at the source end.
The conventional process has limited removal capability of polycyclic aromatic hydrocarbon, and the removal efficiency is generally less than 30%. Therefore, there is a need to develop a treatment process that is more efficient in the removal of polycyclic aromatic hydrocarbons.
Disclosure of Invention
In view of the above-mentioned shortcomings of the prior art, the present inventors have found that adding an ozone micro-nano bubble treatment unit can effectively remove polycyclic aromatic hydrocarbons in overflow pollution. Ozone is a strong oxidant, has higher oxidation-reduction potential, can directly or indirectly perform oxidation reaction with polycyclic aromatic hydrocarbon, has special physical and chemical properties, and can effectively improve the ozone utilization rate due to the fact that common bubbles quickly rise to the water surface to collapse and disappear and the micro-nano bubbles rise slowly in a time factory.
To achieve the above and other related objects, a first aspect of the present application provides a method for treating polycyclic aromatic hydrocarbons in urban drainage overflow pollution, comprising the steps of:
s1: screening urban drainage overflow sewage to remove solid matters to obtain first treated water;
S2: pre-panning the first treated water to obtain second treated water;
S3: placing the second treated water in an anoxic environment and an aerobic environment for reaction to obtain third treated water;
S4: reacting the third treated water with a coagulant and a flocculant, and removing the precipitate to obtain fourth treated water;
s5: and (3) treating the fourth treated water by micro-nano bubbles, ozone and a catalyst to obtain water from which the polycyclic aromatic hydrocarbon is removed.
In any embodiment of the present application, in step S1, the solid matter includes one or more of crushed stone, branches, towels, paper.
In any embodiment of the present application, in step S1, the screening is performed in a grid; preferably, the overflow speed of the urban drainage overflow sewage in the grid is 0.7-0.9 m/s; the water flow speed in front of the grille is 0.6-0.7 m/s; the depth of water in front of the grille is 0.15-0.25 m.
In any embodiment of the present application, in step S2, the pre-panning separates the sludge and the sewage by stirring the first treated water, and dissolves the polycyclic aromatic hydrocarbon in the organic particles into the sewage to obtain the second treated water.
In any embodiment of the present application, in step S2, the pre-panning time is 20 to 30 minutes.
In any embodiment of the present application, in step S3, the volume ratio of the anoxic environment to the aerobic environment is 1:1.5 to 2.5.
In any embodiment of the present application, in step S3, the second treated water is fed into an anoxic environment and an aerobic environment in batches; preferably, the batch of the second treated water is 3 to 5 batches.
In any embodiment of the present application, in step S3, the reaction time of the second treated water in the anoxic environment is 3 to 5 hours, and the reaction time in the aerobic environment is 7 to 9 hours.
In any embodiment of the present application, in step S3, the second process is performed on a moisture 3 lot, lot 1: batch 2: the water inflow of batch 3 was 40%:40%:30%; batch 1: batch 2: the volume ratio of the anoxic environment to the aerobic environment in the 3 rd batch is 1:1:2.
In any embodiment of the present application, in step S4, the coagulant is selected from polyaluminum chloride and/or polyferric chloride; the flocculant is polyacrylamide and magnetic Fe 3O4 powder; preferably, the addition amount of the magnetic Fe 3O4 powder is 0.5-1 mg/L.
In any embodiment of the present application, in step S4, when the third treated water reacts with the coagulant and the flocculant, mechanical stirring is used to make the average surface water load 8 to 12m 3/m2 ·h.
In any embodiment of the present application, in step S4, the reaction time of the third treated water and the coagulant is 5 to 10 minutes.
In any embodiment of the present application, in step S4, the reaction time of the third treated water and the flocculant is 5 to 10 minutes.
In any embodiment of the present application, in step S4, the reaction time for removing the precipitate of the third treated water is 20 to 30 minutes.
In any embodiment of the present application, in step S5, the catalyst is selected from manganese ferrite, and the addition amount of the catalyst is 0.1-0.5 mg/L.
In any embodiment of the present application, in step S5, the ozone is added in an amount of 3-8 mg/L.
In any embodiment of the present application, in step S5, the ozone and the clean water are pressurized and vacuumized to obtain a gas-liquid mixture containing micro-nano bubbles; preferably, the vacuum degree of the vacuumizing is 0.025-0.03 Mpa; the pressurizing pressure is 0.25-0.40 MPa; the total volume of the gas-liquid mixture is taken as a reference, and the gas content is 5-10%. The flow rate of the gas in the gas-liquid mixture is 7-8L/min; the flow rate of the liquid in the gas-liquid mixture is 5-6L/min; more preferably, the micro-nano bubbles occupy 60 to 80% by volume based on the total volume of the gas.
The application provides a treatment device for polycyclic aromatic hydrocarbon in urban drainage overflow pollution, which comprises a grid, a pre-elutriation tank, a multistage AO tank, a coagulation tank, a sedimentation tank and an ozone reaction tank which are connected in sequence; the ozone reaction tank is connected with an ozone generator through a micro-bubble generation system.
In any embodiment of the application, the microbubble generation system comprises a gas-liquid circulating pump and a gas-liquid releaser which are connected, wherein the gas-liquid releaser is connected with the ozone reaction tank; the gas-liquid circulating pump is connected with the ozone generator; preferably, the gas-liquid circulating pump is used for pressurizing and vacuumizing the introduced gas and liquid to obtain a gas-liquid mixture containing micro-nano bubbles; more preferably, the vacuum degree of the vacuuming is 0.025-0.03 Mpa; the pressurizing pressure is 0.25-0.40 MPa; taking the total volume of the gas-liquid mixture as a reference, wherein the gas content is 5-10%; the flow rate of the gas in the gas-liquid mixture is 7-8L/min; the flow rate of the liquid in the gas-liquid mixture is 5-6L/min; the volume ratio of micro-nano bubbles is 60-80% based on the total volume of gas, so that manganese ferrite MnFe 2O4 serving as a nano catalyst material can be added in an amount of 0.1-0.5 mg/L for better degrading polycyclic aromatic hydrocarbon, the manganese ferrite MnFe 2O4 serving as a nano catalyst material has a spinel structure, and Fe 3+ can better excite ozone to generate free radicals and degrade refractory organic matters, and meanwhile, mn 2+ plays a certain catalytic role on ozone.
In any embodiment of the application, the multistage AO-cell comprises a number of connected anoxic and aerobic zones; the anoxic zone is connected with the pre-elutriation tank, and the aerobic zone is connected with the coagulation tank; preferably, the volume ratio of the anoxic zone to the aerobic zone is 1:1.5 to 2.5.
In any embodiment of the application, the coagulation tank comprises a T1 rapid reaction coagulation tank and a T2 magnetic medium mixing reaction tank which are connected; the T1 rapid reaction coagulation tank is connected with the multistage AO tank, and the T2 magnetic medium mixing reaction tank is connected with the sedimentation tank; preferably, a coagulant is arranged in the T1 rapid reaction coagulation tank; a flocculating agent is arranged in the T2 magnetic medium mixing reaction tank; more preferably, the coagulant is selected from polyaluminum chloride and/or polyferric chloride; the flocculant is selected from polyacrylamide, and for better agglomeration and precipitation of polycyclic aromatic hydrocarbon, magnetic Fe 3O4 powder can be added into a T2 magnetic medium, and the adding amount is 0.5-1 mg/L.
In any embodiment of the application, the ozone reaction tank comprises a reaction tank and a clean water tank which are connected, wherein the reaction tank is connected with the sedimentation tank, and the clean water tank is connected with the microbubble generating system.
In any embodiment of the application, the ozone reaction tank further comprises an aeration disc which is connected with an ozone generator.
In any embodiment of the application, the ozone generator is used for adding ozone, and the adding amount of the ozone is 3-8 mg/L.
A third aspect of the application provides the use of the aforementioned treatment method or the aforementioned treatment device for purifying urban drainage overflow pollution.
Compared with the prior art, the application has the beneficial effects that:
The application adopts coagulant, flocculant, multistage anoxic and aerobic environment, micro-nano bubble ozone and catalyst to achieve the purpose of controlling polycyclic aromatic hydrocarbon in overflow pollution of urban drainage pipe network, and the combined process has high removal efficiency and cost saving, and can be widely used.
Drawings
FIG. 1 is a schematic view of a processing apparatus according to the present application.
FIG. 2 is a schematic diagram of a processing apparatus according to the present application.
Figure 3 is a multi-stage AO-cell diagram of a processing device according to the application.
FIG. 4 is a schematic diagram of a coagulation basin and a sedimentation basin of the treatment device of the present application.
Description of element numbers:
1 grille
2 Pre-panning pool
3 Multistage AO-pool
30 Inlet pipe
31 Anoxic zone
311 Anoxic stirrer
32 Aerobic zone
321 Aeration pipe
33 Outlet pipe
4 Coagulation pool
41T1 rapid reaction coagulation tank
42T2 magnetic medium mixing reaction tank
5 Sedimentation tank
6 Ozone reaction tank
61 Discharge port
62 Stirring device
63 Clean water basin
64 Aeration disc
65 Reaction tank
7 Microbubble generation system
71 Gas-liquid circulating pump
72 Gas-liquid releaser
73 Vacuum gauge
74 Gas flowmeter
75Y-type filter
8 Ozone generator
Detailed Description
In order to make the objects, technical solutions and advantageous effects of the present application clearer, the present application will be further described with reference to examples. It is to be understood that the examples are provided for the purpose of illustrating the application and are not intended to limit the scope of the application. The test methods used in the following examples are conventional, and other advantages and effects of the present application will be readily apparent to those skilled in the art from the disclosure herein.
The inventor of the present application has found a treatment method and a treatment device for polycyclic aromatic hydrocarbon in urban drainage overflow pollution through a great deal of research and study, and the present application is completed on the basis.
The application provides a treatment method of polycyclic aromatic hydrocarbon in urban drainage overflow pollution, which comprises the following steps:
s1: screening urban drainage overflow sewage to remove solid matters to obtain first treated water;
S2: pre-panning the first treated water to obtain second treated water;
S3: placing the second treated water in an anoxic environment and an aerobic environment for reaction to obtain third treated water;
S4: reacting the third treated water with a coagulant and a flocculant, and removing the precipitate to obtain fourth treated water;
s5: and (3) treating the fourth treated water by micro-nano bubbles, ozone and a catalyst to obtain water from which the polycyclic aromatic hydrocarbon is removed.
In the treatment method provided by the application, step S1 is to screen urban drainage overflow sewage to remove solid matters so as to obtain first treated water. Wherein the solid matter comprises one or more of crushed stone, branches, towels and paper. In step S1, the screening is performed in a grid; preferably, the overflow speed of the urban drainage overflow sewage in the grid is 0.7-0.9 m/s; the water flow speed in front of the grille is 0.6-0.7 m/s; the depth of water in front of the grille is 0.15-0.25 m. The purpose of step S1 is to remove solid matter, such as larger suspended matter, floats, fibrous matter in the sewage, ensuring the normal operation of the subsequent treatment unit and the water pump, thereby reducing the treatment load of the subsequent treatment unit and avoiding the blockage of the sludge discharge pipeline.
In the treatment method provided by the application, step S2 refers to pre-panning the first treated water to obtain the second treated water. Wherein, pre-elutriation separates sludge and sewage by stirring the first treated water, and dissolves polycyclic aromatic hydrocarbon in organic particles into the sewage to obtain second treated water. The pre-panning time is 20-30 min. The pre-elutriation is used for better separation of the particles from the soluble organic matter. In some embodiments, pre-panning may be performed in pre-panning tank 2.
In the treatment method provided by the application, the step S3 is to place the second treated water in an anoxic environment and an aerobic environment for reaction to obtain third treated water. Wherein, the volume ratio of the anoxic environment to the aerobic environment is 1:1.5 to 2.5; specifically, it may be 1:1.5 to 1.7, 1:1.7 to 2, or 1:2 to 2.5, etc. In step S3, the second treated water is fed into the anoxic environment and the aerobic environment in batches according to a certain proportion, so that the second treated water can be sufficiently purified. Preferably, the batch of the second treated water is 3 to 5 batches. In step S3, the second process is performed on a water 3 lot, a1 st lot: batch 2: the water inflow of batch 3 was 40%:40%:30%. Batch 1: batch 2: the volume ratio of the anoxic environment to the aerobic environment in the 3 rd batch is 1:1:2. in the step S3, the reaction time of the second treated water in the anoxic environment is 3-5 hours, and the reaction time in the aerobic environment is 7-9 hours. In some embodiments, step S3 may be performed in a multi-stage AO-cell 3. The purpose of step S3 is to further remove organic matters, TN, TP, polycyclic aromatic hydrocarbons and the like.
In the treatment method provided by the application, the step S4 is to react the third treated water with the coagulant and the flocculant to remove the precipitate and obtain fourth treated water. Wherein the coagulant is selected from polyaluminum chloride (PAC) and/or polyferric chloride; the flocculant is selected from Polyacrylamide (PAM) and magnetic Fe 3O4 powder. The adding amount of the magnetic Fe 3O4 powder is 0.5-1 mg/L; specifically, the concentration may be 0.5 to 0.7mg/L, 0.7 to 0.8mg/L, or 0.8 to 1 mg/L. The magnetic Fe 3O4 powder has the function of better absorbing and agglomerating polycyclic aromatic hydrocarbon. In the step S4, when the third treated water reacts with the coagulant and the flocculant, mechanical stirring and variable frequency control are adopted, so that the average surface water load is 8-12 m 3/m2 & h. The reaction time of the third treated water and the coagulant is 5-10 min. The reaction time of the third treated water and the flocculant is 5-10 min. The reaction time for removing the sediment of the third treated water is 20-30 min. In some embodiments, step S4 may be performed in coagulation tank 4 and sedimentation tank 5. In one embodiment of the application, the third treated water is reacted with the coagulant PAC, and then the coagulant and the sewage mixture are rapidly and uniformly mixed by rapid stirring, then reacted with the flocculant, and then stirred at a high speed, and finally the sediment is removed to obtain fourth treated water. The purpose of step S4 is to further remove SS, TP, etc., and prevent clogging of subsequent reaction pipes.
In the treatment method provided by the application, step S5 refers to treating the fourth treated water by micro-nano bubbles, ozone and a catalyst to obtain water from which the polycyclic aromatic hydrocarbon is removed. Wherein, the adding amount of ozone is 3-8 mg/L; specifically, the concentration may be 3 to 5mg/L, 5 to 7mg/L, 7 to 8mg/L, or the like. Pressurizing and vacuumizing the ozone and the clean water to obtain a gas-liquid mixture containing micro-nano bubbles; preferably, the vacuum degree of the vacuumizing is 0.025-0.03 Mpa; specifically, the pressure may be 0.025 to 0.027MPa, 0.027 to 0.0028MPa, or 0.028 to 0.03 MPa. The pressurizing pressure is 0.25-0.40 MPa; specifically, the pressure may be 0.25 to 0.30MPa, 0.30 to 0.35MPa, or 0.35 to 0.40 MPa. Taking the total volume of the gas-liquid mixture as a reference, wherein the gas content is 5-10%; specifically, it may be 5 to 8%, 8 to 9%, or 9 to 10%, etc. The flow rate of the gas in the gas-liquid mixture is 7-8L/min; specifically, the concentration may be 7 to 7.2L/min, 7.2 to 7.5L/min, or 7.5 to 8L/min. The flow rate of the liquid in the gas-liquid mixture is 5-6L/min; specifically, the concentration may be 5 to 5.2L/min, 5.2 to 5.5L/min, or 5.5 to 6L/min. Taking the total volume of the gas as a reference, the volume ratio of micro-nano bubbles is 60-80%; specifically, the content may be 60 to 65%, 65 to 70%, or 70 to 80%. Ozone is a strong oxidant, has higher oxidation-reduction potential, can directly or indirectly perform oxidation reaction with polycyclic aromatic hydrocarbon, has special physical and chemical properties, and can effectively improve the ozone utilization rate due to the fact that common bubbles quickly rise to the water surface to collapse and disappear and the micro-nano bubbles rise slowly. Thus the micro-bubble ozone can further reduce the polycyclic aromatic hydrocarbon. In some embodiments, the catalyst is selected from manganese ferrite, and the catalyst is added in an amount of 0.1-0.5 mg/L; specifically, the concentration may be 0.1 to 0.3mg/L, 0.3 to 0.4mg/L, or 0.4 to 0.5 mg/L. The catalyst manganese ferrite MnFe 2O4, preferably nano manganese ferrite MnFe 2O4, has a spinel structure, fe 3+ can better excite ozone to generate free radicals, degrade refractory organic matters, and meanwhile, mn 2+ has a certain catalytic effect on ozone. Therefore, the micro-nano bubbles, ozone and the catalyst in the step S5 can act synergistically to remove the polycyclic aromatic hydrocarbon more comprehensively and effectively. In some embodiments, step S5 may be performed using ozone reaction cell 6, microbubble generation system 7, and ozone generator 8.
The second aspect of the application provides a treatment device for polycyclic aromatic hydrocarbon in urban drainage overflow pollution, which is shown in figure 1 and comprises a grid 1, a pre-elutriation tank 2, a multistage AO tank 3, a coagulation tank 4, a sedimentation tank 5 and an ozone reaction tank 6 which are connected in sequence; the ozone reaction tank 6 is connected with an ozone generator 8 through a micro-bubble generation system 7. The device has simple structure and small occupied area, and is beneficial to industrial application.
In the treatment device provided by the application, the grid 1 is used for removing solid substances such as larger suspended matters, floaters and fibrous substances in sewage, so that the normal operation of a subsequent treatment unit and a water pump is ensured, the treatment load of the subsequent treatment unit is reduced, and the blockage of a sludge discharge pipeline is avoided.
In the treatment device provided by the application, the pre-elutriation tank 2 is used for dissolving polycyclic aromatic hydrocarbon in organic matter particles into sewage, so that the separation of the particles and soluble organic matters is better realized.
In the treatment device provided by the application, as shown in figure 3, the multi-stage AO pool 3 comprises a plurality of connected anoxic zones 31 and aerobic zones 32; the anoxic zone 31 is connected with the pre-elutriation tank 2, and the aerobic zone 32 is connected with the coagulation tank 4; preferably, the volume ratio of the anoxic zone 31 to the aerobic zone 32 is 1:1.5 to 2.5. The multistage AO pool 3 adopts a multi-stage AO pool sewage treatment process of split-point water inlet, and the number of reactor sections of the anoxic zone 31 and the aerobic zone 32 is generally 3-5. The sewage quantity to be treated respectively enters each level of anoxic sections according to a certain proportion, so that the sewage is purified. Preferably, the number of reactor sections of the anoxic zone 31 and the aerobic zone 32 is 3, and the water inflow of each stage is 40 percent respectively: 40%:30%.
In some embodiments, as shown in fig. 3, an anoxic stirrer 311 is provided in the anoxic zone 31 for stirring the mixture and maintaining an anoxic environment. An aeration pipe 321 is arranged at the bottom of the aerobic zone 32 and is used for providing air.
In some embodiments, as shown in fig. 3, the multi-stage AO-cell 3 further comprises a water inlet pipe 30 and a water outlet pipe 33. A water inlet pipe 30 is arranged at the bottom of the first-stage anoxic zone and is connected with the pre-panning tank 2. The water outlet pipe 33 is arranged at the top of the last-stage aerobic zone 32 and is connected with the coagulation tank 4. The multistage AO pool 3 is used for further removing organic matters, TN, TP, polycyclic aromatic hydrocarbon and the like.
In the treatment device provided by the application, as shown in fig. 4, the coagulation tank 4 comprises a T1 rapid reaction coagulation tank 41 and a T2 magnetic medium mixing reaction tank 42 which are connected; the T1 rapid reaction coagulation tank 41 is connected with the multi-stage AO tank 3, specifically, the T1 rapid reaction coagulation tank 41 is connected with the water outlet pipe 33. The T2 magnetic medium mixing reaction tank 42 is connected with the sedimentation tank 5; preferably, a coagulant is arranged in the T1 rapid reaction coagulation tank 41; a flocculating agent is arranged in the T2 magnetic medium mixing reaction tank 42; more preferably, the coagulant is selected from polyaluminum chloride and/or polyferric chloride; the flocculant is selected from polyacrylamide and magnetic Fe 3O4 powder. The adding amount of the magnetic Fe 3O4 powder is 0.5-1 mg/L; specifically, the concentration may be 0.5 to 0.7mg/L, 0.7 to 0.8mg/L, or 0.8 to 1 mg/L. The magnetic Fe 3O4 powder has the function of better absorbing and agglomerating polycyclic aromatic hydrocarbon. The coagulant and flocculant can cause particles in the water that are difficult to precipitate to polymerize with each other to form a colloid, which then combines with impurities in the water to form larger flocks. The floccule has strong adsorption force, and can adsorb suspended matters, partial bacteria and soluble matters. The floccule is absorbed, and the volume is increased to sink.
In the treatment apparatus provided by the present application, as shown in fig. 4, the sedimentation tank 5 adopts an upward flow inclined plate (pipe) for sedimentation. The coagulation tank 4 and the sedimentation tank 5 are used for further removing substances such as SS, TP and the like and preventing the subsequent reaction pipelines from being blocked.
In the treatment device provided by the application, as shown in fig. 2, the ozone reaction tank 6 comprises a reaction tank 65 and a clean water tank 63 which are connected, the reaction tank 65 is connected with the sedimentation tank 5, and a stirring device 62 is arranged in the reaction tank 65 and is used for stirring and accelerating the reaction of sewage and micro-bubble ozone. The clean water tank 63 is connected with a gas-liquid circulating pump 71 in the micro-bubble generating system 7, and the clean water tank 63 contains clean water. An aeration disc 64 is arranged in the reaction tank 65 and is connected with the ozone generator 8 for discharging ozone in the ozone generator 8.
In the treatment device provided by the application, as shown in fig. 2, a micro-bubble generation system 7 comprises a gas-liquid circulating pump 71 and a gas-liquid releaser 72 which are connected, wherein the gas-liquid releaser 72 is connected with a reaction tank 65; the gas-liquid circulating pump 71 is connected with the ozone generator 8; preferably, the gas-liquid circulation pump 71 is used for pressurizing and vacuumizing the gas introduced by the ozone generator 8 and the liquid introduced by the clean water tank 63 to obtain a gas-liquid mixture containing micro-nano bubbles, and discharging the gas-liquid mixture into the reaction tank 65 through the gas-liquid releaser 72, and reacting with sewage in the reaction tank 65; more preferably, the vacuum degree of the vacuuming is 0.025-0.03 Mpa; specifically, the pressure may be 0.025 to 0.027MPa, 0.027 to 0.0028MPa, or 0.028 to 0.03 MPa. The pressurizing pressure is 0.25-0.40 MPa; specifically, the pressure may be 0.25 to 0.30MPa, 0.30 to 0.35MPa, or 0.35 to 0.40 MPa.
The stable operation mode of the gas-liquid circulating pump 71 is to adjust the flow rate of the liquid introduced into the clean water tank 63, control the vacuum degree to be 0.025-0.03 Mpa, and then gradually adjust the flow rate of the gas introduced into the ozone generator 8, under which condition the gas-liquid circulating pump 71 can operate stably. If not adjusted in this way, the operation of the gas-liquid circulation pump 71 is not smooth, so that the contents of ozone and micro-nano bubbles in the discharged gas-liquid mixture cannot meet the processing requirements. Unless otherwise indicated, the flow rates and flows of the present application are synonymous. Taking the total volume of the gas-liquid mixture as a reference, wherein the gas content is 5-10%; specifically, it may be 5 to 8%, 8 to 9%, or 9 to 10%, etc. The flow rate of the gas in the gas-liquid mixture is 7-8L/min; specifically, the concentration may be 7 to 7.2L/min, 7.2 to 7.5L/min, or 7.5 to 8L/min. The flow rate of the liquid in the gas-liquid mixture is 5-6L/min; specifically, the concentration may be 5 to 5.2L/min, 5.2 to 5.5L/min, or 5.5 to 6L/min. Taking the total volume of the gas as a reference, the volume ratio of micro-nano bubbles is 60-80%; specifically, the content may be 60 to 65%, 65 to 70%, or 70 to 80%.
In the treatment device provided by the application, the ozone generator 8 is used for adding ozone, and the adding amount of the ozone is 3-8 mg/L; specifically, the concentration may be 3 to 5mg/L, 5 to 7mg/L, 7 to 8mg/L, or the like. Ozone can be subjected to oxidation reaction with polycyclic aromatic hydrocarbon, micro-nano bubbles rise slowly, the existence time is long, and the ozone utilization rate can be effectively improved. When the micro-bubble generating system 7 works stably, micro-nano bubbles in the reaction tank 65 shrink by themselves, the volume becomes small, and the rising speed becomes slow, so that the ozone solubility can be improved, the ozone loss rate is reduced, and the ozone adding amount can be gradually reduced to 3-4 mg/L. Therefore, the application adopts a specific treatment means, not only can utilize micro-nano bubble ozone to further reduce the polycyclic aromatic hydrocarbon, but also can utilize the volume change of the micro-nano bubble to reduce the ozone consumption, thereby meeting the requirement of removing the polycyclic aromatic hydrocarbon.
In some embodiments, the reaction tank 65 also comprises catalyst manganese ferrite, and the adding amount of the catalyst is 0.1-0.5 mg/L; specifically, the concentration may be 0.1 to 0.3mg/L, 0.3 to 0.4mg/L, or 0.4 to 0.5 mg/L. The manganese ferrite MnFe 2O4 is preferably nano manganese ferrite MnFe 2O4, has a spinel structure, and Fe 3+ can better excite ozone to generate free radicals to degrade refractory organic matters, and meanwhile, mn 2+ has a certain catalytic effect on ozone. Therefore, the micro-nano bubbles, ozone and the catalyst can act synergistically to remove the polycyclic aromatic hydrocarbon more comprehensively and effectively.
In the treatment device provided by the application, the gas-liquid circulating pump 71 utilizes clear water in the clear water tank 63 to be fully mixed with ozone in the ozone generator 8, pressurization and vacuum pumping are carried out, so that micro-bubble ozone water is generated, the micro-bubble ozone water flows back to the ozone reaction tank 6, the micro-bubble ozone water is continuously provided for the ozone reaction tank 6, and the micro-bubble ozone water fully reacts with polycyclic aromatic hydrocarbon.
In the treatment apparatus provided by the present application, as shown in fig. 2, a Y-type filter 75, a vacuum gauge 73 and a gas flowmeter 74 are further provided between the gas-liquid circulation pump 71 and the clean water tank 63, which are sequentially connected. Among other things, the Y-filter 75 is used to remove impurities to protect the valve and equipment for normal use. The vacuum gauge 73 is used for detecting the vacuum degree in the gas-liquid circulation pump 71, and the gas flow meter is used for detecting the flow rate of ozone supplied from the ozone generator 8. Ozone and polycyclic aromatic hydrocarbon in the ozone reaction tank 6 are subjected to oxidation reaction, so that the micro-nano bubbles effectively improve the ozone utilization rate, and the micro-bubble ozone can further reduce the polycyclic aromatic hydrocarbon.
In the treatment device provided by the application, as shown in fig. 2, the bottom of the ozone reaction tank 6 is also provided with a discharge port 61 for discharging treated sewage, and the sewage treated by the treatment device can effectively control polycyclic aromatic hydrocarbon.
A third aspect of the application provides the use of the aforementioned treatment method or the aforementioned treatment apparatus for cleaning urban drainage overflow pollution. The application can realize the efficient removal of the polycyclic aromatic hydrocarbon in urban overflow pollution.
The application is further illustrated by the following examples, which are not intended to limit the scope of the application.
Example 1
Taking urban overflow sewage with a treatment scale of 100m 3/d as an example, the following method is adopted and the treatment is carried out in a treatment device as shown in figures 1 to 4:
S1: screening urban drainage overflow sewage in a grid 1 to obtain first treated water;
s2: pre-panning the first treated water in a pre-panning tank 2 to obtain second treated water;
S3: placing the second treated water into a multistage AO pool 3 for reaction to obtain third treated water;
s4: treating the third treated water coagulation tank 4 and the sedimentation tank 5 to obtain fourth treated water;
s5: and (3) treating the fourth treated water in an ozone reaction tank 6 by micro-nano bubbles, ozone and catalyst manganese ferrite to obtain water from which the polycyclic aromatic hydrocarbon is removed.
Wherein, the parameters of the grid 1 are as follows: wide b=0.8 m, channel depth 2m, gate pitch b=20 mm, power n=1.1 kW of water pump in grid.
The multistage AO-cell 3 has 6 partitions in total, and the costs of the partitions are l×b×h=1.1 m×2.5m×2m (anoxic zone 31), l×b×h=1.4 m×2.5m×2m (aerobic zone 32), l×b×h=1.1 m×2.5m×2m (anoxic zone 31), l×b×h=1.4 m×2.5m×2m (anoxic zone 32), l×b×h=1.1 m×2.5m×2m (anoxic zone 31), l×b×h=3.9 m×2.5m×2m (aerobic zone 32), respectively.
The cell size of the pre-panning cell 2 was l×b×h=1m×1m×2m.
In the coagulation tank 4: the cell size of the T1 rapid reaction coagulation tank 41 is l×b×h=0.5 m×0.5m×2m, and the cell size of the T2 magnetic medium mixing reaction tank 42 is l×b×h=0.5 m×0.5m×2m. The T1 rapid reaction coagulation tank 41 contains a coagulant which is polyaluminium chloride and polyferric chloride, the T2 magnetic medium mixing reaction tank 42 contains a flocculant which is polyacrylamide and magnetic Fe 3O4 powder, and the adding amount of the magnetic Fe 3O4 powder is 0.5mg/L.
The cell size of the sedimentation tank 5 is l×b×h=1m×1m×2m.
The vacuum degree of the inlet of the gas-liquid circulating pump 71 is 0.025MPa, the outlet pressure is 0.25-0.40 MPa, the gas flow is 7-8L/min, the water flow is 5.0L/min, the total volume of the microbubble ozone water is the standard, the gas content is 10%, in the adjusting process, the stable operation mode is to firstly adjust the water flow rate of the clean water tank 63, the vacuum degree is controlled, then the flow rate of the gas of the ozone generator 8 is gradually adjusted, under the condition, the device can stably operate, a large amount of micro-nano bubbles are generated in the reactor, the ozone adding amount is 5mg/L, after the microbubble generating system 7 works stably, the bubbles shrink by themselves, the volume of the bubbles becomes small, the rising speed becomes slow, so the ozone solubility can be improved, the ozone losing rate can be reduced, and the ozone adding amount can be gradually reduced to 3-4 mg/L. In order to better degrade polycyclic aromatic hydrocarbon, a nano catalyst material manganese ferrite MnFe 2O4 is added into the ozone reaction tank 6, the addition amount is 0.2mg/L, the nano catalyst material manganese ferrite MnFe 2O4 has a spinel structure, and Fe 3+ can better excite ozone to generate free radicals to degrade refractory organic matters, and meanwhile, mn 2+ plays a certain catalytic role on ozone. When the initial polycyclic aromatic hydrocarbon concentration in the urban overflow sewage is 10ug/L, the effluent concentration after the treatment by the device is 2-3 ug/L, and the treatment efficiency is (water inlet concentration-water outlet concentration)/water inlet concentration=70-80%.
Comparative example 1
Taking urban overflow sewage with a treatment scale of 100m 3/d as an example, the following method is adopted for treatment:
S1: screening urban drainage overflow sewage in a grid 1 to obtain first treated water;
s2: pre-panning the first treated water in a pre-panning tank 2 to obtain second treated water;
S3: treating the second treated water coagulation tank 4 and the sedimentation tank 5 to obtain third treated water;
s4: and (3) treating the third treated water in an ozone reaction tank 6 by micro-nano bubbles and ozone to obtain water from which the polycyclic aromatic hydrocarbon is removed.
Wherein, the parameters of the grid 1 are as follows: wide b=0.8 m, channel depth 2m, gate pitch b=20 mm, power n=1.1 kW of water pump in grid.
The cell size of the pre-panning cell 2 was l×b×h=1m×1m×2m.
In the coagulation tank 4: the cell size of the T1 rapid reaction coagulation tank 41 is l×b×h=0.5 m×0.5m×2m, and the cell size of the T2 magnetic medium mixing reaction tank 42 is l×b×h=0.5 m×0.5m×2m. The T1 rapid reaction coagulation tank 41 contains a coagulant which is polyaluminium chloride and polyferric chloride, the T2 magnetic medium mixing reaction tank 42 contains a flocculant which is polyacrylamide and magnetic Fe 3O4 powder, and the adding amount of the magnetic Fe 3O4 powder is 0.5mg/L.
The cell size of the sedimentation tank 5 is l×b×h=1m×1m×2m.
The vacuum degree of the inlet of the gas-liquid circulating pump 71 is 0.025MPa, the outlet pressure is 0.25-0.40 MPa, the gas flow is 7-8L/min, the water flow is 5.0L/min, the total volume of the microbubble ozone water is the standard, and the gas content is 10%. Under the condition, the device runs stably, a large amount of micro-nano bubbles are generated in the reactor, the ozone adding amount is 5mg/L, when the initial polycyclic aromatic hydrocarbon concentration in urban overflow sewage is 10ug/L, the effluent concentration after being treated by the device is 4-5 ug/L, and the treatment efficiency is (water inlet concentration-water outlet concentration)/water inlet concentration=50-60%
The absence of multistage AO treatment and manganese ferrite catalyst in comparative example 1, resulted in lower polycyclic aromatic hydrocarbon treatment efficiency than in example 1.
In conclusion, the application adopts coagulant, flocculant, multistage anoxic and aerobic environment, micro-nano bubble ozone and catalyst to achieve the purpose of controlling polycyclic aromatic hydrocarbon in overflow pollution of urban drainage pipe network, meets the requirement of removing polycyclic aromatic hydrocarbon, and has the advantages of high removal efficiency, low cost and wide application.
The above embodiments are merely illustrative of the principles of the present application and its effectiveness, and are not intended to limit the application. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the application. Accordingly, it is intended that all equivalent modifications and variations of the application be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.
Claims (10)
1. A treatment method of polycyclic aromatic hydrocarbon in urban drainage overflow pollution comprises the following steps:
s1: screening urban drainage overflow sewage to remove solid matters to obtain first treated water;
S2: pre-panning the first treated water to obtain second treated water;
S3: placing the second treated water in an anoxic environment and an aerobic environment for reaction to obtain third treated water;
S4: reacting the third treated water with a coagulant and a flocculant, and removing the precipitate to obtain fourth treated water;
s5: and (3) treating the fourth treated water by micro-nano bubbles, ozone and a catalyst to obtain water from which the polycyclic aromatic hydrocarbon is removed.
2. The process according to claim 1, wherein in step S1, the solid matter comprises one or more of crushed stone, branches, towels, paper;
And/or, in step S1, the screening is performed in a grid; the flow rate of the urban drainage overflow sewage passing through the grid is 0.7-0.9 m/s; the water flow speed in front of the grille is 0.6-0.7 m/s; the depth of water in front of the grille is 0.15-0.25 m.
3. The treatment method according to claim 1, wherein in step S2, the pre-panning separates sludge and sewage by stirring the first treated water, and dissolves polycyclic aromatic hydrocarbon in the organic matter particles into the sewage to obtain second treated water;
And/or, in the step S2, the pre-panning time is 20-30 min.
4. The method according to claim 1, wherein in step S3, the volume ratio of the anoxic environment to the aerobic environment is 1:1.5 to 2.5;
and/or, in step S3, the second treated water is fed into an anoxic environment and an aerobic environment in batches; the batches of the second treatment water are 3-5 batches;
And/or in the step S3, the reaction time of the second treated water in the anoxic environment is 3-5 h, and the reaction time in the aerobic environment is 7-9 h.
5. The method according to claim 4, wherein in step S3, the second water 3 lot is processed, and the 1 st lot: batch 2: the water inflow of batch 3 was 40%:40%:30%; batch 1: batch 2: the volume ratio of the anoxic environment to the aerobic environment in the 3 rd batch is 1:1:2.
6. The process according to claim 1, wherein in step S4, the coagulant is selected from polyaluminium chloride and/or polyaluminium chloride; the flocculant is polyacrylamide and magnetic Fe 3O4 powder; preferably, the adding amount of the magnetic Fe 3O4 powder is 0.5-1 mg/L;
And/or, in the step S4, when the third treated water reacts with the coagulant and the flocculant, mechanical stirring is adopted, so that the average surface water load is 8-12 m 3/m2 & h;
And/or in the step S4, the reaction time of the third treated water and the coagulant is 5-10 min;
And/or in the step S4, the reaction time of the third treated water and the flocculating agent is 5-10 min;
And/or in the step S4, the reaction time for removing the sediment of the third treatment water is 20-30 min.
7. The method according to claim 1, wherein in step S5, the catalyst is selected from manganese ferrite, and the catalyst is added in an amount of 0.1 to 0.5mg/L;
And/or the ozone adding amount is 3-8 mg/L;
and/or, in the step S5, pressurizing and vacuumizing the ozone and the clean water to obtain a gas-liquid mixture containing micro-nano bubbles; preferably, the vacuum degree of the vacuumizing is 0.025-0.03 Mpa; the pressurizing pressure is 0.25-0.40 MPa; taking the total volume of the gas-liquid mixture as a reference, wherein the gas content is 5-10%; the flow rate of the gas in the gas-liquid mixture is 7-8L/min; the flow rate of the liquid in the gas-liquid mixture is 5-6L/min; more preferably, the micro-nano bubbles occupy 60 to 80% by volume based on the total volume of the gas.
8. A treatment device for polycyclic aromatic hydrocarbon in urban drainage overflow pollution comprises a grid (1), a pre-elutriation tank (2), a multistage AO tank (3), a coagulation tank (4), a sedimentation tank (5) and an ozone reaction tank (6) which are connected in sequence; the ozone reaction tank (6) is connected with an ozone generator (8) through a micro-bubble generation system (7).
9. The treatment device according to claim 8, wherein the microbubble generation system (7) comprises a gas-liquid circulation pump (71) and a gas-liquid releaser (72) connected, the gas-liquid releaser (72) being connected to the ozone reaction tank (6); the gas-liquid circulating pump (71) is connected with the ozone generator (8); preferably, the gas-liquid circulating pump (71) is used for pressurizing and vacuumizing the introduced gas and liquid to obtain a gas-liquid mixture containing micro-nano bubbles; more preferably, the vacuum degree of the vacuuming is 0.025-0.03 Mpa; the pressurizing pressure is 0.25-0.40 MPa; taking the total volume of the gas-liquid mixture as a reference, wherein the gas content is 5-10%; the flow rate of the gas in the gas-liquid mixture is 7-8L/min; the flow rate of the liquid in the gas-liquid mixture is 5-6L/min; taking the total volume of the gas as a reference, the volume ratio of micro-nano bubbles is 60-80%;
And/or, the multistage AO pool (3) comprises a plurality of connected anoxic zones (31) and aerobic zones (32); the anoxic zone (31) is connected with the pre-elutriation tank (2), and the aerobic zone (32) is connected with the coagulation tank (4); preferably, the volume ratio of the anoxic zone (31) to the aerobic zone (32) is 1:1.5 to 2.5;
And/or the coagulation tank (4) comprises a T1 rapid reaction coagulation tank (41) and a T2 magnetic medium mixing reaction tank (42) which are connected; the T1 rapid reaction coagulation tank (41) is connected with the multistage AO tank (3), and the T2 magnetic medium mixing reaction tank (42) is connected with the sedimentation tank (5); preferably, a coagulant is arranged in the T1 rapid reaction coagulation tank (41); a flocculating agent is arranged in the T2 magnetic medium mixing reaction tank (42); more preferably, the coagulant is selected from polyaluminium chloride; the flocculant is selected from polyacrylamide;
and/or the ozone reaction tank (6) comprises a reaction tank (65) and a clean water tank (63) which are connected, and the reaction tank (65) is connected with the sedimentation tank (5); the clean water tank (63) is connected with the micro-bubble generation system (7);
and/or the ozone reaction tank (6) also comprises an aeration disc (64) which is connected with an ozone generator (8);
and/or the ozone generator (8) is used for adding ozone, and the adding amount of the ozone is 3-8 mg/L.
10. Use of a treatment process according to any one of claims 1 to 7 or a treatment apparatus according to any one of claims 8 to 9 for purifying urban drainage overflow pollution.
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