CN114380468A - Full-amount treatment system and method for leachate of garbage transfer station - Google Patents
Full-amount treatment system and method for leachate of garbage transfer station Download PDFInfo
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Images
Classifications
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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
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
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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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/465—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electroflotation
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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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
- C02F2209/05—Conductivity or salinity
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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
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
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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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
Abstract
The invention provides a garbage transfer station leachate full-scale treatment system and a method, wherein the system comprises an electric flocculation reaction tank, an MBR biochemical reactor, an STRO membrane module, an AOP reaction tower, a BAC reaction tower, an ozone generator, a pure oxygen preparation device and a sludge dewatering device which are sequentially connected; the anode of the electrocoagulation reaction tank can generate oxygen bubbles or chlorine bubbles, and the cathode can generate hydrogen bubbles; the MBR biochemical reactor comprises an anaerobic tank, an aerobic tank and an MBR ultrafiltration membrane component which are connected in sequence, wherein the aerobic tank adopts a jet aeration adding mode to carry out pure oxygen aeration, and can generate oxygen bubbles with the diameter less than 50 microns; the STRO membrane module is connected with the MBR ultrafiltration membrane module, and the AOP reaction tower is connected with a concentrated solution outlet of the STRO membrane module; the ozone generator is connected with the AOP reaction tower, the pure oxygen preparation device is respectively connected with the aerobic tank and the ozone generator, and the sludge dewatering device is respectively connected with the electric flocculation reaction tank and the anaerobic tank. The invention can effectively discharge the percolate of the garbage transfer station up to the standard.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a full-scale treatment system and method for high-difficulty organic wastewater such as leachate of a garbage transfer station and the like.
Background
After the household garbage is thrown into the garbage can by residents, the household garbage enters a middle-end transferring link. The garbage truck is compressed by small garbage transfer stations collected to a community concentration point by each community, then transported to large and medium transfer stations of each community by a garbage truck to be compressed again, and finally transported to a garbage incineration plant or a landfill site by a large vehicle to be finally treated.
When the garbage transfer station compresses garbage, garbage percolate accounting for about 5-15% of the total amount of the garbage can be generated. The leachate belongs to fresh garbage leachate, has short stacking and fermentation time, high content of suspended matters (SS), animal and vegetable oil, high concentration of Chemical Oxygen Demand (COD) and Biochemical Oxygen Demand (BOD), high concentration of total nitrogen, organic matters with difficult degradability and high salt content. Due to seasonal influences, different living habits of different regions and differences of flushing water quantities of vehicles, containers and the ground of various transfer stations, the fluctuation of water quality and water quantity of generated percolate is large.
At present, leachate of a plurality of garbage transfer stations is directly discharged, but the concentration and complexity of the pollutants of the leachate are far higher than those of municipal sewage, so that great impact is brought to municipal sewage treatment plants, the leachate needs to be treated on the transfer station site, and most of the pollutants are removed and then discharged into a municipal pipe network.
The traditional process generally adopts a process route of coagulation, biochemical treatment and membrane treatment or a simple biochemical method, and although the process has a certain pollutant removal effect, the process still has a plurality of defects: large occupied area, unstable biochemical operation, unqualified COD and total nitrogen treatment, membrane concentrated solution to be treated and the like. Therefore, a small and efficient full-scale treatment system is urgently needed to be developed to solve the problem of the percolate of the transfer station.
Disclosure of Invention
The invention provides a full-scale treatment system for percolate of a garbage transfer station, which comprises an electric flocculation reaction tank, an MBR biochemical reactor, an STRO membrane module, an AOP reaction tower, a BAC reaction tower, an ozone generator, a pure oxygen preparation device and a sludge dewatering device;
wherein the electrocoagulation reaction tank, the MBR biochemical reactor, the STRO membrane module, the AOP reaction tower and the BAC reaction tower are connected in sequence;
the anode of the electrocoagulation reaction tank can generate oxygen bubbles or chlorine bubbles, and the cathode can generate hydrogen bubbles;
the MBR biochemical reactor comprises an anaerobic tank, an aerobic tank and an MBR ultrafiltration membrane component which are connected in sequence, wherein the aerobic tank adopts a jet aeration adding mode to carry out pure oxygen aeration and can generate oxygen bubbles with the diameter less than 50 microns;
the STRO membrane module is connected with the MBR ultrafiltration membrane module, and the AOP reaction tower is connected with a concentrated solution outlet of the STRO membrane module;
the ozone generator is connected with the AOP reaction tower, the pure oxygen preparation device is respectively connected with the aerobic tank and the ozone generator, and the sludge dewatering device is respectively connected with the electric flocculation reaction tank and the anaerobic tank.
In some embodiments of the present invention, the system further includes an ozone tail gas decomposition and utilization device, the ozone tail gas decomposition and utilization device includes an ozone thermal catalytic decomposition tower and an oxygen compressor which are connected, the ozone thermal catalytic decomposition tower is connected with the ozone tail gas outlet of the AOP reaction tower, and the oxygen compressor is connected with the gas storage tank of the pure oxygen preparation device.
In some embodiments of the invention, the system further comprises a dosing device connected to the electrocoagulation reaction tank and the STRO membrane module, respectively.
In some embodiments of the invention, the system further comprises a mobile cleaning device for cleaning the STRO membrane module and the MBR ultrafiltration membrane module.
In some embodiments of the invention, the system further comprises a control cabinet, wherein the control cabinet is provided with a remote control mode for controlling the system through a terminal.
In some embodiments of the invention, the pure oxygen preparation device is further connected to the electrocoagulation reaction tank.
In some embodiments of the present invention, the electrocoagulation reaction tank is an electrolysis, flocculation and air flotation integrated machine, the anode of the electrocoagulation reaction tank is metallic iron, and the cathode of the electrocoagulation reaction tank is an inert electrode;
the sludge dewatering device is a stacked screw type dewatering machine;
the AOP reaction tower and the BAC reaction tower are respectively a two-stage AOP reaction tower and a two-stage BAC reaction tower; wherein, in the second stage AOP reaction tower, ozone can be coupled with hydrogen peroxide and/or ultraviolet light to generate hydroxyl radicals.
The second objective of the present invention is to provide a method for fully processing leachate in a garbage transfer station by the aforementioned system for fully processing leachate in a garbage transfer station, comprising:
sending the leachate of the garbage transfer station into the electric flocculation reaction tank, and removing suspended matters and/or oil substances in the leachate of the garbage transfer station to obtain first wastewater and first sludge;
sending the first wastewater into the anaerobic tank for treatment to obtain second wastewater and second sludge; wherein the DO solubility in the anaerobic pool is less than 0.5 mg/L;
feeding the second wastewater into the aerobic tank for treatment to obtain third wastewater, third sludge and mixed liquor; wherein the DO solubility in the aerobic pool is 2-4mg/L, and the COD load is higher than 12kg/m3D, MLVSS is higher than 12000mg/L, the diameter of the oxygen bubbles in the aerobic tank is less than 50 microns;
sending the third wastewater into the MBR ultrafiltration membrane module for treatment to obtain fourth wastewater;
sending the fourth wastewater into the STRO membrane module for treatment to obtain first produced water and concentrated solution;
sending the concentrated solution into the AOP reaction tower and the BAC reaction tower in sequence for treatment to obtain second water production;
feeding the first sludge and the second sludge into the sludge dewatering device for treatment;
returning the third sludge and the mixed liquor to the anaerobic tank for treatment;
wherein, the ozone required by the AOP reaction tower is provided by the ozone generator, and the oxygen required by the aerobic pool and the ozone generator is provided by the pure oxygen preparation device.
In some embodiments of the invention, the fourth wastewater is treated by feeding the fourth wastewater to the STRO membrane module after adjusting the pH of the fourth wastewater to 6.3 to 6.8.
In some embodiments of the invention, the concentrate is subjected to a two-stage AOP reaction in the AOP reaction column, followed by a two-stage BAC reaction in the BAC reaction column;
wherein, the time of the first-stage AOP reaction is 2-3h, the time of the second-stage AOP reaction is 2.5-3.5h, the time of the first-stage BAC reaction is 2-3h, and the time of the second-stage BAC reaction is 2.5-3.5 h;
wherein, when the second stage AOP reaction is carried out, the concentrated solution reacts with hydroxyl radicals in a second stage AOP reaction tower.
The invention combines the technologies of materialization, biochemistry, membrane filtration and advanced oxidation, integrates the advantages of various materialization pretreatments and advanced treatment, integrates the advantages of stable and efficient biochemical treatment, uses a set of pure oxygen gas generation system, is used for oxygen for biochemical aeration and ozone at the same time, fully utilizes limited land occupation and resources, and can effectively meet the standard emission treatment requirements of high-salinity, high-SS, high-grease, high-COD and high-total-nitrogen high-difficulty organic wastewater of the percolate of a refuse transfer station.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
Fig. 1 is a schematic structural diagram of a full leachate treatment system of a refuse transfer station according to an embodiment of the present invention.
Fig. 2 is a schematic structural diagram of a diamond-shaped separation net of an STRO membrane module according to an embodiment of the present invention.
Fig. 3 is a schematic perspective view of a diaphragm of an stroo membrane module according to an embodiment of the present invention.
Fig. 4 is a schematic front view of a diaphragm of an STRO membrane module according to an embodiment of the present invention.
Fig. 5 is a schematic structural diagram of a stress-resistant disc of an STRO membrane module according to an embodiment of the present invention.
Fig. 6 is a flow chart of a process for treating leachate in a refuse transfer station according to an embodiment of the present invention.
Detailed Description
The following detailed description of the present invention, taken in conjunction with the accompanying drawings and examples, is provided to enable the invention and its various aspects and advantages to be better understood. However, the specific embodiments and examples described below are for illustrative purposes only and are not limiting of the invention.
It is expressly intended that all such similar substitutes and modifications which would be obvious to one skilled in the art are deemed to be included in the invention. While the methods and applications of this invention have been described in terms of preferred embodiments, it will be apparent to those of ordinary skill in the art that variations and modifications in the methods and applications described herein, as well as other suitable variations and combinations, may be made to implement and use the techniques of this invention without departing from the spirit and scope of the invention.
Fig. 1 shows a full-scale treatment system 1000 for percolate from a refuse transfer station, which comprises an electrocoagulation reaction tank 110, a Membrane Bioreactor (MBR)120, a pipe-network type reverse osmosis membrane module (STRO membrane module) 130, an ozone advanced oxidation reaction tower (AOP reaction tower) 140, a biological activated carbon reaction tower (BAC reaction tower) 150, an ozone generator 160, a pure oxygen preparation device 170 and a sludge dewatering device 180. Wherein, the electrocoagulation reaction tank 110, the MBR biochemical reactor 120, the STRO membrane module 130, the AOP reaction tower 140 and the BAC reaction tower 150 are connected in sequence.
Alternatively, the electric flocculation reaction tank 110 is an electrolysis, flocculation and floatation integrated machine, and direct current is provided by a rectification power supply. In one embodiment of the present invention, the voltage is about 5.0V and the current density is about 20mA/cm2。
The anode of the electrocoagulation reaction tank 110 can generate oxygen bubbles or chlorine bubbles, and the cathode can generate hydrogen bubbles. The fine micro-bubbles generate air flotation to bring the floccules to the water surface to form a scum layer and are scraped to a slag collecting barrel by a slag scraper.
In one embodiment of the present invention, the anode of the electrocoagulation reaction tank 110 is metallic iron, and the cathode is an inert electrode. The inert electrode can be metallic titanium or graphite. In one embodiment of the present invention, the inter-plate distance is about 2.5 cm. Ferrous ions dissolved at the anode and transferred into the solution during electrolysis are hydrolyzed into polynuclear hydroxyl complexes, which are good flocculants, thereby forming the SS and/or oil substances (animal oil and/or vegetable oil) into flocs.
The invention refers to the effluent obtained after the leachate of the garbage transfer station is treated by the electrocoagulation reaction tank 110 as first wastewater, and the obtained solid garbage as first sludge.
The first wastewater is then sent to MBR biochemical reactor 120. The MBR biochemical reactor 120 comprises an anaerobic tank 121, an aerobic tank 122 and an MBR ultrafiltration membrane component 123 which are connected in sequence. The first wastewater sequentially passes through the anaerobic tank 121, the aerobic tank 122 and the MBR ultrafiltration membrane module 123 to be respectively subjected to anaerobic treatment, aerobic treatment and MBR ultrafiltration.
After the first wastewater is treated in the anaerobic tank 121, a second wastewater and a second sludge are obtained. In one embodiment of the present invention, the dissolved oxygen concentration (DO solubility) in the anaerobic tank 121 is less than 0.5 mg/L.
The aerobic tank 122 of the invention adopts pure oxygen aeration and adopts a high-precision jet aeration feeding mode, which is different from a common biochemical aerobic tank adopting air aeration. In the present invention, the oxygen in the aerobic tank 122 is provided by the pure oxygen preparing device 170 (i.e. the pure oxygen preparing device 170 is connected to the aerobic tank 122).
In an embodiment of the present invention, the oxygen bubbles are micro-nano bubbles, and the diameter of the bubbles is less than 50 μm, so that the utilization efficiency of oxygen is very high, which can reach 50-70%, and the conventional method is only 10-25%, and the microorganisms can also make full use of the micro-bubble oxygen, so that the air quantity required by the aerobic tank 122 is only 1/12-1/15 of air aeration, so that the sludge concentration of the MBR biochemical reactor can be increased to 18000 and 28000mg/L, and the floor area of the MBR biochemical reactor is reduced to 50-70% of that of the conventional method. In addition, because pure oxygen aeration is adopted, the air flow is small, so that when the temperature is high in summer or low in winter, a high-temperature heat source or a low-temperature cold source brought by the aeration is greatly reduced, and a more appropriate environmental condition is provided for microorganisms.
In the invention, the DO solubility in the aerobic tank 122 is 2-4mg/L, and the COD load is higher than 12kg/m3D, the mixed liquor volatile suspended solids concentration (MLVSS) is higher than 12000 mg/L.
In an embodiment of the present invention, the biochemical system employs two-stage A/O-A/O for enhanced denitrification, and the mixed liquid and sludge (referred to as third sludge in the present invention) in the aerobic tank 122 flow back to the anaerobic tank 121. The second wastewater is sent to the aerobic tank 122 for treatment, and then third wastewater, third sludge and mixed liquor are obtained.
And the third wastewater is sent to the MBR ultrafiltration membrane module 133 for treatment, so as to obtain fourth wastewater. Removing SS, BOD, organic nitrogen and NH in wastewater by an MBR biochemical reactor3-N、NO3N, heavy metals and the like, and can effectively improve the hardness, the chromaticity and the turbidity of the organic wastewater.
Removing SS, BOD, organic nitrogen and NH in wastewater by an MBR biochemical reactor3-N、NO3N, heavy metals and the like, and can effectively improve the hardness, the chromaticity and the turbidity of the organic wastewater.
The STRO membrane module 130 is connected to the MBR ultrafiltration membrane module 123. The fourth wastewater is sent to the STRO membrane module 130 for treatment to obtain a first product water and a concentrated solution.
Fig. 2 to 5 show a partial structure of the STRO membrane module 130 according to an embodiment of the present application.
Referring to fig. 2 to 5, MBR effluent is directly intercepted by a highly effective open type mesh tube flow channel reverse osmosis STRO membrane system to intercept refractory COD and total nitrogen. The membrane component of the STRO membrane system comprises a membrane shell, a flange end cover, a flow guide disc 131, an anti-stress disc 132, a central flow guide pipe 133 and a separation layer coated on the periphery of the central flow guide pipe, wherein the separation layer is a membrane bag layer formed by rolling a plurality of membrane bags and an open type separation net in the same direction.
As shown in fig. 2, the open type partition net is arranged in the water inlet flow channel between the surfaces of the adjacent membrane bag layers, the open type partition net and the membrane bag surfaces are in a convex point type contact mode, the rhombic thin partition net is connected with the convex points, and a rhombic wide open type flow channel is formed between two rows of convex point type partition nets on the surfaces in contact with the membrane bag along the water inlet and outlet direction. When the water flow enters the flow channel at an angle of 45 degrees with the rhombic fine separation net during working, the water flow with extremely small resistance is formed in the channel, and the surface flow velocity of the membrane is high, so that the pollution blockage of the membrane caused by the fact that intercepted pollutants are attached to the surfaces of the water inlet channel and the membrane is effectively avoided.
As shown in fig. 3 and 4, the diversion disk 131 is a spiral-flow diversion disk, a water inlet hole 131a is formed on the disk surface of the diversion disk, the water inlet hole 131a is close to the edge of the disk of the diversion disk and is a tangential water inlet, and the water inlet hole is an arc-shaped hole, so that spiral-flow water distribution is formed, and the water distribution is uniform.
As shown in fig. 3, the center nozzle connecting hole 131b of the swirl flow deflector 131 is relatively large and deep, and the center pouring tube 133 is tightly sealed with the center nozzle of the swirl flow deflector 131 by a packing ring thereon.
As shown in fig. 5, the anti-stress disc 132 is designed hydraulically, and the support pieces connected with the center and the circumference are arc-shaped and radially supported, so that the design can effectively and uniformly distribute the inlet water to the disc surface. The disk surface is provided with a circular hole from the center to the periphery, and the hole diameter is gradually increased from inside to outside. Because the membrane element is of a roll type structure, the membrane area of each circle of the membrane element from the center to the outside is gradually enlarged (namely the membrane area of the circumference of the center is the smallest, and the membrane area of the circumference of the outermost circle is the largest), so the design can lead the water inflow born by the membrane surfaces of different parts to be close to the same, lead the membrane element to be in the best service performance, and transfer and disperse the water inflow stress.
In addition, two open mesh tube flow channel reverse osmosis membrane elements can be placed in one pressure membrane shell. The central flow guide pipes of the two membrane elements connected in series are connected through a flow guide pipe connector. The investment cost of the membrane components in combined application can be greatly reduced, about one half of the occupied area is saved, the pressure loss among the membrane components can be reduced, and the energy consumption of operation is saved.
The special design ensures that the requirements of the high-efficiency open type net pipe runner reverse osmosis STRO membrane system on water inlet SS and COD are much lower than those of a common RO membrane, the common pollution blockage and scaling in the reverse osmosis membrane component can be greatly reduced, the water yield can reach more than 70 percent, and the retention rate can reach more than 95.8 percent. The produced water after being treated by the STRO membrane can meet the strict water quality discharge requirement.
In an embodiment of the present invention, the AOP reaction tower 140 and the BAC reaction tower 150 are a two-stage AOP reaction tower and a two-stage BAC reaction tower, respectively. That is, the concentrated solution is subjected to two-stage AOP reaction in the AOP reaction column 140, and then two-stage BAC reaction is carried out in the BAC reaction column 150.
Wherein, in the second stage AOP reaction tower, ozone can be coupled with hydrogen peroxide and/or ultraviolet light to generate hydroxyl free radical (OH), that is, when the second stage AOP reaction is carried out, the concentrated solution reacts with the hydroxyl free radical in the second stage AOP reaction tower, thereby breaking chains of organic macromolecules to form medium and small molecules, improving the BOD 5-COD ratio (B/C ratio) of the wastewater, and degrading and mineralizing a part of organic matters which are difficult to degrade into CO2And H2O, and has the function of sterilization.
In one embodiment of the present invention, the time for the first stage AOP reaction is 2-3h, the time for the second stage AOP reaction is 2.5-3.5h, the time for the first stage BAC reaction is 2-3h, and the time for the second stage BAC reaction is 2.5-3.5 h.
In the invention, the STRO membrane concentrated solution adopts an ozone advanced oxidation combined system, the ozone system adopts an oxygen source ozone generator, and the ozone concentration is 150-3And the oxidation capability is stronger. In addition, in the ozone reaction tower, ozone is coupled with hydrogen peroxide and/or ultraviolet to generate hydroxyl radical (OH) with high oxidation capacity, so that most of organic matters difficult to degrade can be degraded and mineralized into CO2And H2And O. In addition, based on the principle that organic matter in the wastewater is acted by ozone to break chains of organic macromolecules to form small and medium molecules so as to improve the B/C ratio of the wastewater, the BAC reaction is placed in an AOP reaction tower, and the biological decomposition effect of microorganisms in the biological activated carbon is utilized to further improve the B/C ratio of the wastewaterOrganic matters in the wastewater are removed, and meanwhile, the operation cost is effectively saved. According to the COD and the total nitrogen of the inlet water, the combination of the AOP reaction tower and the BAC reaction tower in one stage or multiple stages can be designed, so that the COD and the total nitrogen in the concentrated solution can be removed more economically and effectively.
The second produced water produced by the treatment is discharged out of the system together with the first produced water.
In the present invention, an ozone generator 160 is connected to the AOP reaction tower 140. That is, the ozone generator 160 supplies ozone to the AOP reaction tower 140.
Optionally, the ozone generator 160 employs an oxygen source manner to synthesize ozone by high-voltage discharge of oxygen, wherein the ozone concentration is 150-3And the oxidation capability is strong. Alternatively, the generated ozone gas is piped to the AOP reactor 140, where it is coupled with hydrogen peroxide and/or uv light to generate hydroxyl radicals (OH) with high oxidation capacity, which oxidatively degrades the wastewater. Optionally, the ozone generator 160 is further provided with a water chiller for cooling the ozone generator 160.
In the present invention, the pure oxygen preparing device 170 is connected to the aerobic tank 122 and the ozone generator 160, respectively, to provide oxygen thereto.
Optionally, the pure oxygen preparation device 170 includes an air compressor, a freeze dryer, an oxygen generator, and a gas storage tank, which are sequentially connected, the air compressor compresses air, conveys the air to the freeze dryer for drying, and then passes through the molecular sieve oxygen generator to prepare oxygen with a purity of about 92% and stores the oxygen in the gas storage tank.
In one embodiment of the present invention, the pure oxygen preparation device 170 is further connected to the electrocoagulation reaction tank 110. At this time, a part of oxygen of the pure oxygen preparation device 170 generates micro-nano oxygen bubbles through the micro-nano bubble generator and sends the micro-nano oxygen bubbles into the electric flocculation reaction tank 110, so that on one hand, the air flotation effect can be increased, and on the other hand, ferrous ions can be oxidized into ferric ions to improve the flocculation effect.
In the present invention, the sludge dewatering device 180 is connected to the electrocoagulation reaction tank 110 and the anaerobic tank 121, respectively, and is configured to treat the first sludge and the second sludge generated in the electrocoagulation reaction tank 110 and the anaerobic tank 121.
In an embodiment of the invention, the sludge dewatering device 180 is a stacked screw type dewatering machine, which occupies a small area and is convenient to maintain. Optionally, cationic Polyacrylamide (PAM) accounting for about 0.25% of the dry weight of the sludge is added into the sludge before dehydration, and stirring and mixing are carried out to promote the formation of compact alum flocs, so that the effect is better. The dewatered filtrate can be returned to the electric flocculation reaction tank 110, and the dewatered mud cake is dewatered by a dewatering machine until the water content is below 80 percent, so that the mud cake and the garbage of the garbage transfer station are sent to a garbage landfill for final treatment.
In the embodiment shown in fig. 1, an ozone tail gas decomposition and utilization device 190 is further included. The device 190 for decomposing and utilizing the ozone tail gas can comprise an ozone thermal catalytic decomposition tower and an oxygen compressor which are connected, wherein the ozone thermal catalytic decomposition tower is connected with an ozone tail gas outlet of the AOP reaction tower 140, and the oxygen compressor is connected with a gas storage tank of the pure oxygen preparation device 170 in a compression mode.
The ozone tail gas of the AOP reaction tower is sucked into the ozone tail gas decomposition and utilization device by negative pressure, is firstly decomposed by the ozone thermal catalytic decomposition tower, is pumped out by the exhaust fan, enters the oxygen compressor for compression, enters the pure oxygen preparation device after the air pressure is increased, and is used as pure oxygen to supply oxygen for the aerobic pool and the ozone generator, so that the oxygen amount can be saved by 20-45%, and the reutilization of the ozone tail gas is fully realized. The ozone tail gas recycling mode fully excavates and utilizes the internal resources of the system, and realizes the minimization of equipment and the maximization of resources as far as possible, thereby achieving the aim of saving investment and operating cost.
In an embodiment of the present invention, the system may further comprise a medicating device. The dosing device is respectively connected with the electrocoagulation reaction tank and the STRO membrane component, provides medicine (such as PAM) for the electrocoagulation reaction tank, adjusts the proper pH value and adjusts the water inlet of the STRO membrane component. In one embodiment of the present invention, the fourth wastewater is treated by feeding into the STRO membrane module after the pH of the fourth wastewater is adjusted to 6.3 to 6.8.
In an embodiment of the present invention, the system may further include a mobile cleaning apparatus for cleaning the STRO membrane module and the MBR ultrafiltration membrane module. The movable cleaning device can be vehicle-mounted and convenient to move, so that the movable cleaning device can be shared by a plurality of garbage transfer stations, and the garbage transfer stations do not need to be specially provided with cleaning equipment placing spaces, so that the occupied area is effectively saved.
In an embodiment of the present invention, the system may further include a control cabinet. Wherein, the switch board is provided with the remote control mode through terminal control system. The system can be used for controlling the running state of the whole garbage transfer station leachate full-scale treatment system, can realize one-key starting and remote control, saves labor cost as much as possible, and hands the whole system to skilled technicians for remote regulation and control, so that the system runs more stably.
In summary, the above technical solution of the present invention has the following beneficial effects:
(1) the invention fully considers the limitation of narrow and small ground of the garbage transfer station, and can save the occupied area by 23.3-42.5 percent compared with the traditional MBR full treatment process by using compact equipment for system combination, such as an electric flocculation pretreatment all-in-one machine integrating electrolysis, flocculation and air flotation, an STRO concentration, biochemical MBR system and ozone advanced oxidation sharing a pure oxygen gas production system, pure oxygen aeration, ozone tail gas conversion into oxygen for recycling, a sludge dehydrator, mobile cleaning equipment and the like.
(2) The pure oxygen gas production system is simultaneously used for oxygen supply of the MBR biochemical aerobic tank and oxygen supply of the ozone generator. The air inflow of the biochemical aerobic tank is only 1/10 of air aeration; micro-nano bubbles are formed by adopting high-precision jet aeration, and the oxygen utilization efficiency is up to more than 50%; ozone tail gas of the ozone reaction tower is subjected to ozone thermal catalytic decomposition and compressed by an oxygen compressor and is used as pure oxygen for oxygen supply of the MBR biochemical aerobic tank, so that the ozone tail gas is recycled, and the oxygen resource utilization maximization is realized by the three measures.
(3) The invention adopts the high-efficiency open type net pipe runner reverse osmosis STRO membrane system, the membrane component of the system passes through a unique rhombic open type separation net, a rotational flow type diversion disc, an anti-stress disc with radial arc shape and gradually increased disc surface holes from inside to outside, two open type net pipe runner reverse osmosis membrane components are arranged in a pressure membrane shell, and the like, so that the system is optimally designed, has lower requirements on inlet water SS and COD (SDI (less than or equal to 20) than that of a common RO membrane, has the advantages of small pressure loss, uniform water flow distribution, small occupied area and the like, can greatly reduce common pollution blockage and scaling in the reverse osmosis membrane component, and can produce water which can meet the strict water quality discharge requirement.
The STRO membrane concentrated solution of the invention adopts an ozone advanced oxidation combined system, couples ozone with hydrogen peroxide and/or ultraviolet light to generate hydroxyl free radicals (OH) with high oxidation capacity, and simultaneously carries out combined treatment on one-stage or multi-stage ozone AOP reaction tower and BAC reaction tower, thereby realizing more economic and effective removal of COD and total nitrogen in the concentrated solution.
Fig. 6 shows a method for processing leachate in a garbage transfer station according to an embodiment of the present invention, which may include the following steps.
And (3) conveying the percolate of the garbage transfer station into an electric flocculation reaction tank, and removing suspended matters and/or oil substances in the percolate of the garbage transfer station to obtain first wastewater and first sludge.
And sending the first wastewater into an anaerobic tank for treatment to obtain second wastewater and second sludge. Wherein the DO solubility in the anaerobic pool is lower than 0.5 mg/L.
And sending the second wastewater into an aerobic tank for treatment to obtain third wastewater, third sludge and mixed liquor. Wherein the DO solubility in the aerobic tank is 2-4mg/L, and the COD load is higher than 12kg/m3D, MLVSS higher than 12000mg/L, and the diameter of the oxygen bubbles in the aerobic tank is less than 50 microns.
And sending the third wastewater into an MBR ultrafiltration membrane component for treatment to obtain fourth wastewater.
And sending the fourth wastewater into an STRO membrane module for treatment to obtain first produced water and concentrated solution.
And (4) sequentially sending the concentrated solution into an AOP reaction tower and a BAC reaction tower for treatment to obtain second water production.
And sending the first sludge and the second sludge into a sludge dewatering device for treatment.
And returning the third sludge and the mixed liquor to the anaerobic tank for treatment.
It should be specifically noted that the order of the above steps may be adjusted accordingly, unless necessary.
The specific steps are the same as the system description, and are not repeated.
The present invention will be described below with reference to specific examples. The values of the process conditions taken in the following examples are exemplary and ranges of values are provided as indicated in the foregoing summary, and reference may be made to conventional techniques for process parameters not specifically noted. The detection methods used in the following examples are all conventional in the industry. Unless otherwise indicated, the reagents and instruments used in the technical scheme provided by the invention can be purchased from conventional channels or markets.
Example 1
In this embodiment, the amount of leachate in the garbage transfer station is 5m3/d、、COD 22630mg/L，TN 1254mg/L、NH3-N 757mg/L、SS 5228mg/L。
The landfill leachate firstly enters an electric flocculation reaction tank, the voltage is 5.0V, and the current density is 20mA/cm2The metal iron is used as an anode, the metal titanium is used as a cathode, the distance between polar plates is 2.5cm, the COD of effluent is 15932mg/L, the removal rate is 29.6 percent, SS 1770mg/L and the removal rate is 66.1 percent. Then the wastewater is conveyed to an MBR biochemical reactor and firstly enters an anaerobic tank, and the DO concentration of the anaerobic tank is controlled to be about 0.4 mg/L. Then flows into an aerobic tank, the DO solubility is controlled to be about 3mg/L, and the COD load is about 15kg/m3D, MLVSS of 12000mg/L or more. The biochemical system adopts A two-stage A/O-A/O mode to strengthen denitrification, and the mixed liquid and the sludge in the aerobic tank flow back to the anaerobic tank. The produced water of the aerobic tank flows into an MBR ultrafiltration membrane component, and after being treated by the MBR ultrafiltration membrane component, the COD563mg/L and the TN65.2mg/L, NH of the produced water3And (4) N8.2mg/L and SS18.9mg/L, and the produced water enters the STRO membrane component for concentration, the water production rate of the membrane reaches 81.2 percent, and the produced water reaches the standard and is discharged. The STRO concentrated solution sequentially passes through the two-stage AOP reaction tower and the two-stage BAC reaction tower, ozone and hydrogen peroxide are coupled in the second-stage ozone AOP reaction tower to generate hydroxyl free radicals (OH) with high oxidation capacity, organic macromolecules are broken to form middle and small molecules, the B/C ratio of the wastewater is improved, and in addition, a part of organic matters which are difficult to degrade is degraded and mineralized into CO2And H2O, and has the function of sterilization. The reaction time of the first stage ozone AOP is controlled to be 2.5hr, and the reaction time of the second stage ozone AOP is controlled to be 3.0 hr. Then utilizing the biological decomposition action of the microorganisms in the BAC reaction tower to further remove organic matters and total nitrogen in the wastewaterSo as to decompose and remove most BOD, COD, TN, chroma, turbidity, humic acid and the like in the concentrated solution, the reaction time of the first-stage BAC is controlled to be 2.5hr, and the reaction time of the second-stage BAC is controlled to be 3.0 hr. Finally, the effluent is combined with the water produced by the STRO membrane, and the mixture of the effluent COD23.5mg/L and TN30.5mg/L, NH3-N1.2mg/L and SS15.9mg/L, and meets the standard discharge of the landfill leachate. The sludge generated by the electric flocculation reaction tank and the anaerobic tank is discharged after being treated by the sludge dewatering device, and the wastewater flows back to the electric flocculation reaction tank for treatment.
In this embodiment, the above-mentioned full-scale treatment system for leachate in the garbage transfer station is designed to be as compact as possible, and the required floor space is only 9.2m2And the occupied area required by the traditional MBR full-scale treatment process is 12-16m2And the occupied area can be saved by about 23.3 to 42.5 percent.
It should be understood that the above examples are only for clearly illustrating the present invention and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications of the invention may be made without departing from the scope of the invention.
Claims (10)
1. A full-scale treatment system for percolate of a garbage transfer station is characterized by comprising an electric flocculation reaction tank, an MBR biochemical reactor, an STRO membrane component, an AOP reaction tower, a BAC reaction tower, an ozone generator, a pure oxygen preparation device and a sludge dewatering device;
wherein the electrocoagulation reaction tank, the MBR biochemical reactor, the STRO membrane module, the AOP reaction tower and the BAC reaction tower are connected in sequence;
the anode of the electrocoagulation reaction tank can generate oxygen bubbles or chlorine bubbles, and the cathode can generate hydrogen bubbles;
the MBR biochemical reactor comprises an anaerobic tank, an aerobic tank and an MBR ultrafiltration membrane component which are connected in sequence, wherein the aerobic tank adopts a jet aeration adding mode to carry out pure oxygen aeration and can generate oxygen bubbles with the diameter less than 50 microns;
the STRO membrane module is connected with the MBR ultrafiltration membrane module, and the AOP reaction tower is connected with a concentrated solution outlet of the STRO membrane module;
the ozone generator is connected with the AOP reaction tower, the pure oxygen preparation device is respectively connected with the aerobic tank and the ozone generator, and the sludge dewatering device is respectively connected with the electric flocculation reaction tank and the anaerobic tank.
2. The system according to claim 1, further comprising an ozone tail gas decomposition and utilization device, wherein the ozone tail gas decomposition and utilization device comprises an ozone thermal catalytic decomposition tower and an oxygen compressor which are connected, the ozone thermal catalytic decomposition tower is connected with an ozone tail gas outlet of the AOP reaction tower, and the oxygen compressor is connected with a gas storage tank of the pure oxygen preparation device.
3. The system of claim 1, further comprising a dosing device connected to the electrocoagulation reaction tank and the STRO membrane module, respectively.
4. The system of claim 1, further comprising a mobile cleaning device for cleaning the STRO membrane module and the MBR ultrafiltration membrane module.
5. The system of claim 1, further comprising a control cabinet, wherein the control cabinet is provided with a remote control mode for controlling the system through a terminal.
6. The system of claim 1, wherein the pure oxygen preparation device is further connected to the electrocoagulation reaction tank.
7. The system of claim 1, wherein the electrocoagulation reaction tank is an electrolysis, flocculation and floatation integrated machine, the anode of the electrocoagulation reaction tank is metallic iron, and the cathode of the electrocoagulation reaction tank is an inert electrode;
the sludge dewatering device is a stacked screw type dewatering machine;
the AOP reaction tower and the BAC reaction tower are respectively a two-stage AOP reaction tower and a two-stage BAC reaction tower; wherein, in the second stage AOP reaction tower, ozone can be coupled with hydrogen peroxide and/or ultraviolet light to generate hydroxyl radicals.
8. The method for fully treating the percolate from the refuse transfer station by using the full percolate treatment system of the refuse transfer station according to any one of claims 1 to 7, which is characterized by comprising the following steps:
sending the leachate of the garbage transfer station into the electric flocculation reaction tank, and removing suspended matters and/or oil substances in the leachate of the garbage transfer station to obtain first wastewater and first sludge;
sending the first wastewater into the anaerobic tank for treatment to obtain second wastewater and second sludge; wherein the DO solubility in the anaerobic pool is less than 0.5 mg/L;
feeding the second wastewater into the aerobic tank for treatment to obtain third wastewater, third sludge and mixed liquor; wherein the DO solubility in the aerobic pool is 2-4mg/L, and the COD load is higher than 12kg/m3D, MLVSS is higher than 12000mg/L, the diameter of the oxygen bubbles in the aerobic tank is less than 50 microns;
sending the third wastewater into the MBR ultrafiltration membrane module for treatment to obtain fourth wastewater;
sending the fourth wastewater into the STRO membrane module for treatment to obtain first produced water and concentrated solution;
sending the concentrated solution into the AOP reaction tower and the BAC reaction tower in sequence for treatment to obtain second water production;
feeding the first sludge and the second sludge into the sludge dewatering device for treatment;
returning the third sludge and the mixed liquor to the anaerobic tank for treatment;
wherein, the ozone required by the AOP reaction tower is provided by the ozone generator, and the oxygen required by the aerobic pool and the ozone generator is provided by the pure oxygen preparation device.
9. The method according to claim 8, wherein the fourth wastewater is treated by feeding the fourth wastewater to the STRO membrane module after the pH value of the fourth wastewater is adjusted to 6.3 to 6.8.
10. The method according to claim 8, wherein the concentrate is subjected to a two-stage AOP reaction in the AOP reaction column and then to a two-stage BAC reaction in the BAC reaction column;
wherein, the time of the first-stage AOP reaction is 2-3h, the time of the second-stage AOP reaction is 2.5-3.5h, the time of the first-stage BAC reaction is 2-3h, and the time of the second-stage BAC reaction is 2.5-3.5 h;
wherein, when the second stage AOP reaction is carried out, the concentrated solution reacts with hydroxyl radicals in a second stage AOP reaction tower.
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