CN112794578A - Urban domestic sewage treatment system and treatment process - Google Patents
Urban domestic sewage treatment system and treatment process Download PDFInfo
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/18—PO4-P
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to a town domestic sewage treatment system and a treatment process, which comprises a grid sewage interception mechanism, a rotational flow sedimentation tank, an oxidation ditch, a secondary sedimentation tank, a deep bed denitrification filter tank, a flocculation tank, an immersed super filter tank and a disinfection tank which are sequentially communicated, wherein the oxidation ditch comprises an anaerobic zone, an anoxic zone and an aerobic zone which are sequentially communicated, the anaerobic zone is communicated with the rotational flow sedimentation tank, the aerobic zone is communicated with the secondary sedimentation tank, and a sludge reflux mechanism is arranged between the secondary sedimentation tank and the anaerobic zone. The invention can achieve good effects of removing organic matters, removing nitrogen and phosphorus, and can realize that the final effluent reaches the quasi IV-class water standard.
Description
Technical Field
The invention relates to a town domestic sewage treatment system and a treatment process, and belongs to the field of sewage treatment.
Background
The message that municipal wastewater treatment plant effluent standards may raise a portion to surface class iv water has caused tremendous repercussions in the industry. In recent years, the industry has been disputed around the bidding of sewage treatment plants. On one hand, with the improvement of the technical process, the pollutant discharge standard of a local sewage treatment plant is improved from first grade A to surface IV type water in cities of Beijing, Kunming and the like, and the practice is already carried out. On the other hand, there are also companies that claim that the effluent can reach surface class iv water at a cost of 0.1 dollar per ton. Standard lifts have been trending.
With the development of society, the land development density is increased year by year, the environmental bearing capacity is gradually weakened, or the environmental capacity is reduced, and the protection of the ecological environment is more and more important. The work of improving the process technology of municipal sewage treatment plants to improve the pollutant emission standard of local sewage treatment plants from first class A to quasi-surface IV class water is urgent.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a town domestic sewage treatment system and a treatment process so as to improve the sewage treatment effect.
The technical scheme adopted by the invention is as follows:
the utility model provides a town domestic sewage treatment system, includes grid cut dirty mechanism, whirl sedimentation tank, oxidation ditch, two sedimentation tanks, deep bed denitrification filtering pond, flocculation basin, submergence formula super filtering ponds and the disinfection pond that communicate in proper order, the oxidation ditch is including the anaerobic zone, anoxic zone and the aerobic zone that communicate in proper order, anaerobic zone and whirl sedimentation tank intercommunication, aerobic zone and two sedimentation tanks intercommunication, be equipped with mud backward flow mechanism between two sedimentation tanks and the anaerobic zone.
Further, the grating sewage intercepting mechanism comprises a first grating groove and a second grating groove which are sequentially communicated, and the grating size of the first grating groove is larger than that of the second grating groove.
Furthermore, an oil separation tank is arranged between the rotational flow sedimentation tank and the anaerobic zone, a truss type foam scraping machine is arranged in the oil separation tank, a self-suction type submersible aerator is arranged at the front end of the oil separation tank, and an oil collecting pipe is arranged at the tail end of the oil separation tank.
The town domestic sewage treatment process is carried out by adopting the town domestic sewage treatment system, and comprises the following steps:
s1, sequentially carrying out grating pollutant interception treatment and cyclone sedimentation treatment on the urban domestic sewage to be treated to obtain first effluent;
s2, introducing the first effluent into an oxidation ditch, sequentially carrying out anaerobic treatment, anoxic treatment and aerobic treatment, and then carrying out mud-water separation to obtain second effluent and sludge;
wherein part of the sludge is returned to the front end of the anaerobic zone, and the BOD of the second effluent5/TN≤3；
S3, mixing sodium acetate into the second effluent, and introducing the second effluent into a deep bed denitrification filter to obtain third effluent;
and S4, sequentially carrying out dephosphorization treatment, immersed ultrafiltration treatment and disinfection treatment on the third effluent to obtain purified water.
Further, between S1 and S2, a step of performing oil removal treatment on the first effluent is further included.
Further, in S2, the return flow of the sludge is 75-150wt% of the inflow flow of the urban domestic sewage to be treated.
Further, in S4, PAC is added to the third effluent to perform phosphorus removal treatment.
Further, in S4, chlorine dioxide is used for the sterilization treatment.
The anaerobic zone is arranged in the oxidation ditch, so that the dephosphorization and denitrification effects can be greatly improved; oxidation ditch for removing degraded carbon pollutants (BOD)5) Besides, the composite material also has certain nitrification and denitrification effects, has certain denitrification effect, and can excessively absorb phosphorus in an aerobic state, thereby having certain phosphorus removal effect. The oxidation ditch of the invention not only keeps the general characteristics of the conventional oxidation ditch process, but also has A2The advantages of the O process.
In the invention, the effluent BOD of the secondary sedimentation tank5the/TN is less than or equal to 3, an organic carbon source needs to be added for denitrification, and the deep bed denitrification filter tank is arranged behind the secondary sedimentation tank and can utilize the secondary sedimentation tank to dischargePart of COD in the water is used as carbon source supplement, and the adding amount of the external carbon source is reduced. The flocculation tank is arranged behind the deep bed denitrification filter tank, so that the added carbon source is fully utilized in the denitrification process, and the removal rate of nitrogen is improved. The removal of nitrogen and phosphorus provides a good reaction environment for subsequent immersed ultrafiltration, reduces the energy consumption of the ultrafiltration membrane, and makes the membrane technology become one of the main technologies of large-scale water treatment facilities possible.
As most of the inflow water of the urban domestic sewage is inorganic fine sand, the removal rate of the fine sand in the cyclone sedimentation tank is high, and the removal rate of the fine sand with 140 meshes (0.104 mm) can also reach 73 percent, thereby greatly reducing the load of subsequent treatment.
The oxidation ditch with the anaerobic zone at the front end is adopted, and the oil separation tank is arranged at the upstream of the anaerobic zone, so that the burden of a subsequent treatment unit can be reduced. The technological process of the oxidation ditch is simplified, and a primary sedimentation tank is not needed generally. The oxidation ditch has plug flow characteristics, so that a dissolved oxygen gradient is formed along the length direction of the pond to form an aerobic zone, an anoxic zone and an anaerobic zone respectively. N and P can be well removed through reasonable design and control. The hydraulic retention time and sludge age of the oxidation ditch are long, organic matters are removed more thoroughly, and the residual sludge is highly stable.
Deep bed denitrification filter pool, flocculation pool and immersion ultrafiltration pool are adopted for deep treatment, carbon source is added after the secondary sedimentation pool and before the deep bed denitrification filter pool, and because sufficient organic carbon source is needed in the denitrification process, the denitrification rate is also influenced by different types of carbon source. The denitrification carbon source can be divided into three categories: the first is soluble organic matter that is readily biodegradable; the second type is slowly degradable organic matter; the third category is cellular material, which bacteria use cellular components for endogenous nitrification. Among the three classes of substances, the first class of organic substances has the fastest reaction rate as carbon sources, and the third class of organic substances has the slowest reaction rate. The invention selects sodium acetate with best effect.
Optionally, the deep bed denitrification filter adopts 3-4mm quartz sand medium filter materials, the depth of the filter bed is usually 1.8m, and the filter can ensure that the SS of the effluent is lower than 5 mg/L. The surface layers of most of the filter tanks are easy to block or harden and lose water heads quickly, and the unique homogeneous quartz sand of the deep bed denitrification filter tank allows solid impurities to penetrate through the surface layer of the filter bed and go deep into the filter material of the filter tank, so that the excellent effect of intercepting the solid matters in the whole filter tank in the longitudinal and deep direction is achieved.
The method adopts a chemical phosphorus removal method, and adds PAC medicament at the rear position, so that the reduction of carbon sources in deep bed denitrification influent water can be avoided, and the removal efficiency of TN is ensured.
The immersed ultrafiltration tank has an efficient interception effect, and particulate matters, colloid, macromolecular organic matters, bacteria and the like in the sewage are intercepted on the water inlet side of the membrane. The immersed super filter also has the advantages of compact equipment, small occupied area, low energy consumption and operation cost, strong pollution resistance and the like, and is suitable for large-scale water treatment application. In order to realize the automatic operation of the system, the water quality of inlet and outlet water is monitored in real time, and a certain number of instruments can be arranged according to the requirement.
The invention only needs carbon source, PAC and other medicaments, does not need inhibitors, bactericides and other medicaments, has less required medicament amount, does not have a large amount of activated sludge in the whole treatment system, does not need to worry about algae microorganisms to block devices, and reduces the burden of ultrafiltration membranes and the like from the source.
The invention can effectively improve the water environment quality, relieve the pressure of water resource shortage, eliminate poor class V water on the earth surface, improve the effluent standard of a sewage plant to the standard of class IV water, and further improve the effluent quality, which is a decision requirement and is also an environmental requirement. The process can overcome the defects of insufficient carbon source, low organic pollutant removal rate, low nitrogen and phosphorus removal efficiency and the like in the conventional sewage treatment process, so that the town sewage treatment technology is more economic and efficient and operates stably.
Drawings
FIG. 1 is a flow chart of the town domestic sewage treatment process of the invention.
FIG. 2 is a graph showing the results of the oxidation ditch of the present invention.
Detailed Description
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict. For convenience of description, the words "upper", "lower", "left" and "right" in the following description are used only to indicate the correspondence between the upper, lower, left and right directions of the drawings themselves, and do not limit the structure.
Referring to fig. 1 and 2, the town domestic sewage treatment system comprises a grid sewage interception mechanism 1, a rotational flow sedimentation tank 2, an oxidation ditch 3, a secondary sedimentation tank 4, a deep bed denitrification filter tank 5, a flocculation tank 6, an immersed ultrafiltration tank 7 and a disinfection tank 8 which are sequentially communicated, wherein the oxidation ditch 3 comprises an anaerobic zone 301, an anoxic zone 302 and an aerobic zone 303 which are sequentially communicated, the anaerobic zone 301 is communicated with the rotational flow sedimentation tank 2, the aerobic zone 303 is communicated with the secondary sedimentation tank 4, and a sludge reflux mechanism 9 is arranged between the secondary sedimentation tank 4 and the anaerobic zone 301. A high-speed impeller is arranged in the anaerobic zone, low-speed impellers are respectively arranged in the anoxic zone and the aerobic zone, and an inverted umbrella-shaped surface aerator is arranged at the water inlet end of the aerobic zone. The oxidation ditch can remove organic pollutants such as BOD and the like, and can also reduce the quantity of TP and TN to a certain extent. The oxidation ditch process belongs to a complete mixed activated sludge method, and the circulating flow in the tank is large, so that the oxidation ditch process has the advantage of strong impact load resistance. The effluent of the oxidation ditch is arranged in a high dissolved oxygen region, which is beneficial to partially removing P and improving the dissolved oxygen of the effluent of the secondary sedimentation tank.
Optionally, a tubular aerator is arranged in the aerobic zone 303 for aeration, and not only oxidation, nitrification and biochemical reaction for aerobic phosphorus absorption are generated in the section, but also synchronous denitrification can be generated, and partial denitrification can be realized; the effluent of the oxidation ditch is arranged in a high dissolved oxygen region, which is beneficial to partial phosphorus removal and improvement of the dissolved oxygen of the effluent of the secondary sedimentation tank. Optionally, the secondary sedimentation tank is a circular-periphery water inlet and periphery water outlet radial-flow sedimentation tank, and has the advantages of strong impact resistance, high hydraulic load, short sedimentation duration, high volume utilization rate of a sedimentation area and the like. The circumferential entering type has large water passing section and much smaller water inlet flow speed due to the perimeter of the pool. The flow rate is small, the Reynolds number and the Froude number are both smaller than those of a medium-entering type, the Reynolds number is small, and the inertia effect is small; the Froude number is small, the viscous force effect is large, and the development of the flow state in the sedimentation tank to the laminar flow is effectively promoted, the cocurrent flow is generated, and the activated sludge is promoted to sink. Meanwhile, due to the adsorption clarification effect of the activated sludge layer, sludge particles in the mixed liquor continuously collide, adsorb, combine and flocculate with the activated sludge in the suspension layer, so that a good clarification effect is generated, and the sedimentation effect is improved. Therefore, the method has the advantages of strong impact resistance, high hydraulic load, short settling time, high volume utilization rate of a settling zone and the like. Optionally, the mud suction system of the secondary sedimentation tank adopts a column type central transmission mud suction machine; the driving device is arranged on the central pillar and drives the central pillar frame, the sludge suction pipe, the scum skimming and the like to rotate through the internal gear device, and the sludge suction pipe collects sludge to the central sludge discharge pipe along the bottom of the tank and then discharges the sludge to the outside of the tank through water pressure in the tank. The working bridge is fixedly installed in a half-bridge mode, serves as a channel for the central upright post and the platform around the pool, and is suitable for maintenance and management of workers.
The COD removal rate of the common activated sludge method is only 70-80%, and the COD removal rate of the oxidation ditch of the invention can reach 85-90%. The front end of the oxidation ditch is an anaerobic zone and an anoxic zone, so that A is formed2O pattern, and does not need to specially arrange an external reflux device of mixed liquid, which is beneficial to the phosphorus-accumulating bacteria and the nitrobacillus to obtain sufficient carbon source under anaerobic and anoxic conditions, thereby completing the release of phosphorus and NO3Denitrification of N to achieve nitrogen removal. As the effluent is in the aerobic zone, the phosphorus-accumulating bacteria can excessively absorb phosphorus, thereby realizing phosphorus removal. The above complicated process can be realized in an oxidation ditch with a very simple structure.
Optionally, 2 online dissolved oxygen measuring instruments (1 each for an aerobic zone and an anoxic zone) and 1 MLSS measuring instrument are installed in the oxidation ditch. The dissolved oxygen signal measured by the dissolved oxygen meter is transmitted to a central control room PLC system, processed by the PLC and fed back to a blower room control room, the aeration quantity is automatically adjusted, and the purposes of saving energy and operating according to the set dissolved oxygen are achieved.
The rotational flow sedimentation tank mainly utilizes the rotation of a mechanical impeller to control the flow velocity and flow state of entering water flow, so that sand is in spiral line acceleration sedimentation along the tank wall under the action of centrifugal force and gravity, meanwhile, organic matters float away along with the water flow under the action of the water force, the sand at the bottom of the sedimentation tank is lifted by air or a pump, enters a sand-water separator with a small amount of sewage, is separated and then is discharged, and cleaning water flows back to a grid well, thereby achieving the purpose of sand removal. The cyclone sedimentation tank has small occupied area; the sand setting effect is little changed by the water quantity; the sand-water separation effect is good, the water content of the separated sand is low, the organic matters are few, and the transportation is convenient; the sand washing and discharging period can be automatically controlled by adopting a PLC, and the operation is safe and reliable; the operation is convenient, the maintenance is simple, and the service life is long; little influence on the surrounding environment, good sanitary condition and the like.
The deep bed denitrification filter tank is a treatment unit integrating biological denitrification and filtration functions, has multiple functions of denitrification, dephosphorization, suspended matter removal and the like, and is formed by adopting quartz sand as a biofilm culturing medium of denitrification organisms. Can simultaneously remove TN (NO) under the condition of adding a carbon source3N), SS and TP, the wastewater can be completely contacted with the biofilm on the surface of the medium, and the system is not influenced even by short-time short flow or super water flow impact. The filter material layer of the deep bed filter tank runs in an anoxic environment, a large amount of denitrifying biological flora is attached to and grows on the surface of the filter material, the effluent of the secondary biochemical treatment flows through the filter material layer by gravity, and Nitrate (NO) in the sewage3 -) Or Nitrite (NO)2 -) Adsorbed by the biological membrane of the filter material carrier and reduced into nitrogen (N)2) Is released from the sewage, thereby realizing the denitrification process of the sewage, ensuring the TN of the effluent to reach the standard stably at low temperature and ensuring the TN of the effluent<3.0 mg/L. The granular filter material has the function of intercepting suspended matters. Optionally, the deep-bed denitrification filter tank adopts 'high-resistance' filter bricks, and abandons the traditional filter cake filter cap water and gas distribution form which is easy to block, so that the uniformity of water and gas distribution is ensured, the filter tank is prevented from being blocked, and the stability of the deep-bed denitrification filter tank is greatly improved. Optionally, the deep bed denitrification filter adopts a 'constant water level' water inlet mode, so that the increase of dissolved oxygen in the filter caused by 'water drop' can be effectively reduced, and the increase of medicament cost caused by excessive use of a carbon source is avoided. The deep bed denitrification filter is arranged behind the secondary sedimentation tank, so that part of COD in the effluent of the secondary sedimentation tank can be used as carbon source supplement, and the adding amount of an additional carbon source is reduced.
The deep bed denitrification filter tank has low operation cost: the unique nitrogen removal technology ensures that the filter has small carbon source consumption and energy consumption. The back washing water amount is small, generally less than 2 percent and far less than 4 to 10 percent of other types of filter tanks, so that the treatment cost of the back washing wastewater is reduced. Maintenance-free for life: the deep bed denitrification filter preferably adopts air-water distribution filter bricks, has no easily-damaged parts, has the characteristics of no blockage, no aging, corrosion resistance and the like due to the unique design of quick air-water distribution, adopts quartz sand as a filter material, is wear-resistant, does not run sand, and has a lifelong maintenance-free function. Unique filter brick: in order to ensure even distribution of backflushing air water, the filter chamber adopts an original air water distribution filter brick technology to form an air circulation chamber, and secondary air distribution during backflushing makes air and water be fully mixed and then be forcibly sprayed out from gaps between adjacent filter bricks. Because the gas density is less than water, the gas-water mixture gas sprayed out from the filter brick gaps overflows before the water, and the gas compensation holes are arranged in the middle of the filter brick, so that the air and the water are more uniformly distributed in the whole filter pool area; the filter brick is made of HDPE material, and the service life can reach 50 years. Submerged water inflow: usually, denitrification reaction is carried out under the anoxic condition (dissolved oxygen is 0.2-0.5 mg/L); the dissolved oxygen in the water is 4-5 mg/L after the water is fed into the deep bed filter tank and falls, and the excessive dissolved oxygen causes the consumption of a carbon source and the reduction of an effective filter layer; when the device is operated in winter, the temperature reduction of the sewage caused by water drop is obviously reduced, and the operation efficiency is greatly improved. The control system can select a front-back feedback mechanism to control: the front and back feedback control systems are adopted to increase or reduce the addition of the carbon source and the medicament according to the change of the quality of the inlet water, so that the carbon source and the medicament are accurately added, the quality of the outlet water is ensured, and the addition cost of the carbon source and the medicament is saved.
And phosphorus removal is carried out in the flocculation tank by adopting a chemical phosphorus removal method. Chemical phosphorus removal is accomplished by chemical precipitation, which is the process of adding inorganic metal salt agent into the sewage to mix with soluble salts in the sewage, such as phosphate, to form granular, insoluble substances, and this process is called phase transfer process, and the reaction equation is as follows: FeCl3+K3PO4→FePO4After the chemical agents are actually added into the ↓ +3KCl, not only precipitation reaction but also chemical flocculation reaction are carried out in the sewage. Precipitation reaction of sewageCan be simply understood as: the process of converting the dissolved matter, mostly ionic matter, into non-dissolved, granular form; flocculation is a process in which fine, undissolved solids stick to each other into a larger shape, and flocculation is not a phase transfer process.
Flocculation and sedimentation are very important in the sewage purification process, but the flocculation is used for improving the sedimentation effect of a sedimentation tank, and the sedimentation is used for removing soluble phosphorus in the sewage. If the phase inversion is effected by means of a precipitation process, then, after addition of the soluble metal salt agent to the waste water, on the one hand the soluble phosphorus is converted into the insoluble metal phosphate and, at the same time, the insoluble hydroxide (depending on the pH value) is formed. On the other hand, as the sediment increases and smaller non-soluble solids accumulate to larger non-soluble solids, the stabilized colloids destabilize and the destabilized colloids contact each other to form flocs through a velocity gradient or diffusion process. Finally, the purified sewage and the solid-liquid concentrate (chemical sludge) are obtained through solid-liquid separation, thereby achieving the purpose of chemical phosphorus removal. The chemical phosphorus removal can be generally carried out by adopting the preposed feeding, the postpositive feeding and the synchronous feeding of a biological reaction tank, and also can adopt the multipoint feeding. According to the invention, the PAC agent is added in a post-positioned manner, so that the reduction of carbon sources in deep-bed denitrification influent water can be avoided, and the removal efficiency of TN is ensured.
And (3) ultrafiltration: the method is mainly characterized in that in the process of sieve pore separation under the pushing of pressure, the diameter of components separated by an ultrafiltration method is 0.005-10 mu m, macromolecules and colloidal substances with the relative molecular weight of more than 500 can be intercepted, the adopted osmotic pressure is small and is 0.1-0.5 MPa generally, and substances removed by ultrafiltration are mainly as follows: particulates, colloids, bacteria, heat sources, and various macromolecular organic matter in the water. According to the operation procedure of the immersed ultrafiltration tank, the ultrafiltration tank generally needs to be subjected to comprehensive membrane filament back washing within a certain time, mainly prevents particulate matters from depositing inside the membrane filaments, maintains the flux of the membrane, and is beneficial to protecting the normal operation of a membrane system. When the particle impurities in the inlet water are intercepted on the surface of the membrane, the flow resistance is continuously increased along with the filtering time. After a preset value is reached, the ultrafiltration tank starts to perform automatic backwashing, so that the flux of the membrane is ensured, the set value can be membrane passing pressure (TMP), and can also be time setting or membrane flux, the membrane passing pressure and resistance are increased or the flux is reduced, and the time and the like can start a backwashing process. Backwash water is pumped from the ultrafiltration water production tank mainly by a backwash water pump. Optionally, the backwashing system firstly uses low-pressure air to scrub and loosen solid impurities accumulated on the membrane surface, and then the air-water backwashing flushes the solid impurities out of the membrane fibers. The backwashing system consists of a backwashing water pump, an air blower and related instruments. The main equipment of the ultrafiltration chemical cleaning system comprises: the whole process is automatically controlled by control systems such as a liquid medicine storage tank, a chemical dosing system, a cleaning water storage tank, a cleaning water pump, a heater, a pipeline, a valve and the like. The chemical dosing system consists of three parts of sodium hypochlorite, citric acid and sulfuric acid. The agent is mainly used for chemical cleaning and maintenance cleaning, the agent is directly added on a backflow pipeline inside a chemical cleaning system, the adding amount of the agent is controlled through the operation time of the agent adding pump, and the concentration of cleaning liquid is ensured to be average through the internal circulation of the chemical cleaning pump and the cleaning water pool. The effluent after the deep bed denitrification filter is subjected to immersed ultrafiltration, so that the turbidity is well removed, and the effluent quality is stable.
After the effluent of the flocculation tank is treated by the immersed ultrafiltration tank, the turbidity removal effect is good, and the effluent quality is stable. Generally, the immersed ultrafiltration pool is under the operating conditions of lower pressure and lower water production flux, can greatly delay the pollution speed, has much lower pollution intensity to the membrane than a pressure type ultrafiltration/microfiltration membrane, and is combined with air scrubbing and water backwashing to recover the flux of the membrane more easily; submerged ultrafiltration membranes have greater chemical resistance (pH, oxidizing agents, etc.) when the membrane must be chemically cleaned when contaminated, making cleaning easier and more complete and longer membrane life. Optionally, the effective pore size of the immersed ultrafiltration membrane is 0.04mm, the pore size distribution is uniform, the turbidity is less than 0.1NTU, and the removal rate of bacteria and viruses is greater than 99.99%, so that the effluent quality can reach the standard of a VI-like water body.
The chlorine dioxide is adopted for disinfection, the mechanism of the chlorine dioxide mainly comprises the steps of entering cell bodies through adsorption and osmosis, oxidizing enzyme systems and biological macromolecules in the cells, killing bacteria and viruses well, causing no damage to animals and plants and having long duration of sterilization. The chlorine dioxide has good disinfection and sterilization effects, small dosage, quick action, long duration of disinfection, strong oxidability, capability of maintaining residual disinfection dosage, capability of decomposing cell structures and killing spores and small influence of temperature and pH.
Considering that a small amount of industrial wastewater is contained in the inlet water of certain urban sewage plants, in order to not influence the normal operation of the subsequent treatment unit, an oil separation tank 11 is arranged between the rotational flow sedimentation tank 2 and the anaerobic zone 301, a truss type foam scraper is arranged in the oil separation tank 11, a self-suction type submersible aerator is arranged at the front end of the oil separation tank 11, and an oil collecting pipe is arranged at the tail end of the oil separation tank 11. Therefore, the oil in the sewage can be removed by utilizing the impeller air flotation principle. When the impeller of the self-suction submersible aerator rotates at a high speed, negative pressure is formed in the oil separation tank, air enters from the air inlet pipe, is crushed into fine bubbles under the stirring of the impeller, is thrown out by the guide blades after being fully mixed with water, and then vertically rises in the tank body to perform air floatation. The formed foam is continuously scraped into an oil collecting pipe at the tail end of the oil separation tank by a truss type foam scraping machine which slowly travels, and then is conveyed out of the tank through the oil collecting pipe. The arrangement of the oil separation tank can reduce the burden of the subsequent treatment unit.
After large suspended matters and floating matters in the sewage are removed by the sewage through the coarse grid grooves, the sewage enters the fine grid grooves to remove smaller suspended and floating matters in the sewage, and then the sewage enters the vortex sedimentation tank to remove inorganic particles with larger particle sizes in the raw water so as to ensure the normal operation of the subsequent process flow.
Further, a mixing tank 12 is arranged between the anaerobic zone and the oil separation tank 11, the outlet end of the sludge backflow mechanism is communicated with the mixing tank, the sludge and the effluent of the oil separation tank are fully mixed in the mixing tank and then enter the anaerobic zone, and preferably, DO of the water entering the anaerobic zone is controlled to be 0.2-0.5 mg/L so as to realize the denitrification process.
The anaerobic treatment device further comprises sludge dewatering equipment 10, wherein the sludge backflow mechanism conveys part of sludge to the front end of the anaerobic zone, and conveys the other part of sludge to the sludge dewatering equipment 10 to dewater the sludge.
Optionally, a PLC system may be used to perform interlock control on each functional unit.
The town domestic sewage treatment process is carried out by adopting the town domestic sewage treatment system, and comprises the following steps:
s1, sequentially carrying out grating pollutant interception treatment and cyclone sedimentation treatment on the urban domestic sewage to be treated to obtain first effluent;
s2, introducing the first effluent into an oxidation ditch 3, sequentially carrying out anaerobic treatment, anoxic treatment and aerobic treatment, and then carrying out mud-water separation to obtain second effluent and sludge;
wherein part of the sludge is returned to the front end of the anaerobic zone;
s3, mixing sodium acetate into the second effluent, and introducing the second effluent into the deep bed denitrification filter 5 to obtain third effluent;
wherein, each ton of the second effluent is added with 100g of 25wt% sodium acetate solution;
and S4, sequentially carrying out dephosphorization treatment, immersed ultrafiltration treatment and disinfection treatment on the third effluent to obtain purified water meeting the IV-class water standard.
And between S1 and S2, the method also comprises the step of carrying out oil separation treatment on the first effluent.
In S2, the return flow of the sludge is 75-150wt% of the inflow flow of the urban domestic sewage to be treated (a return pump can be arranged and the return flow is realized through frequency conversion control).
In S4, 10wt% PAC solution is added to the third effluent to remove phosphorus, thereby removing soluble salts (e.g., phosphate) in the wastewater. After PAC is added, the third effluent is subjected to not only chemical flocculation reaction but also precipitation reaction.
Wherein the addition amount of the PAC solution is 30g per ton of the third effluent.
In S4, chlorine dioxide is used for sterilization.
A grating is arranged between the sludge backflow mechanism and the anaerobic zone to effectively remove impurities such as entanglement and particles in the backflow sludge. Optionally, 2 submersible propellers are installed in the anoxic zone of the oxidation ditch, so that stirring and mixing effects are achieved on one hand, propelling effects are achieved on the other hand, and sludge precipitation is avoided.
The town domestic sewage treatment process of the embodiment can achieve good effects of removing organic matters, removing nitrogen and phosphorus, and can achieve the purpose that the effluent reaches the quasi IV water standard, the COD of the obtained effluent is lower than 30mg/L, the BOD5 is lower than 6mg/L, the ammonia nitrogen content is lower than 1.5mg/L, the T-P is lower than 0.3mg/L, and the T-N is lower than 12 mg/L.
The foregoing examples are set forth to illustrate the present invention more clearly and are not to be construed as limiting the scope of the invention, which is defined in the appended claims to which the invention pertains, as modified in all equivalent forms, by those skilled in the art after reading the present invention.
Claims (8)
1. The utility model provides a town domestic sewage treatment system, its characterized in that, cuts dirty mechanism (1), whirl sedimentation tank (2), oxidation ditch (3), two sedimentation tanks (4), deep bed denitrification filtering pond (5), flocculation basin (6), submergence formula super filtering pond (7) and disinfection pond (8) including the grid that communicate in proper order, oxidation ditch (3) are including anaerobic zone (301), anoxic zone (302) and aerobic zone (303) that communicate in proper order, anaerobic zone (301) and whirl sedimentation tank (2) intercommunication, aerobic zone (303) and two sedimentation tanks (4) intercommunication, be equipped with mud return mechanism (9) between two sedimentation tanks (4) and anaerobic zone (301).
2. The town domestic sewage treatment system according to claim 1, wherein the grid sewage interception mechanism (1) comprises a first grid groove and a second grid groove which are communicated in sequence, and the grid size of the first grid groove is larger than that of the second grid groove.
3. The town domestic sewage treatment system according to claim 1, wherein an oil separation tank (11) is arranged between the cyclone sedimentation tank (2) and the anaerobic zone (301), a truss type foam scraping machine is arranged in the oil separation tank (11), a self-suction type submersible aerator is arranged at the front end of the oil separation tank (11), and an oil collecting pipe is arranged at the tail end of the oil separation tank (11).
4. A town domestic sewage treatment process, which is carried out by using the town domestic sewage treatment system as claimed in any one of claims 1-3, and comprises the following steps:
s1, sequentially carrying out grating pollutant interception treatment and cyclone sedimentation treatment on the urban domestic sewage to be treated to obtain first effluent;
s2, introducing the first effluent into an oxidation ditch (3), sequentially carrying out anaerobic treatment, anoxic treatment and aerobic treatment, and then carrying out mud-water separation to obtain second effluent and sludge;
wherein part of the sludge is returned to the front end of the anaerobic zone, and the BOD of the second effluent5/TN≤3；
S3, mixing sodium acetate into the second effluent, and introducing the second effluent into a deep bed denitrification filter (5) to obtain third effluent;
and S4, sequentially carrying out dephosphorization treatment, immersed ultrafiltration treatment and disinfection treatment on the third effluent to obtain purified water.
5. The town domestic sewage treatment process of claim 4, further comprising the step of performing oil separation treatment on the first effluent between S1 and S2.
6. The town domestic sewage treatment process according to claim 4, wherein in S2, the return flow of the sludge is 75-150wt% of the inlet flow of the town domestic sewage to be treated.
7. The town domestic sewage treatment process according to claim 4, wherein PAC is added to the third effluent water in S4 for dephosphorization.
8. The town domestic sewage treatment process according to claim 4, wherein in S4, chlorine dioxide is used for disinfection.
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