CN110498563A - Membraneless integrated treatment system and method for leachate of garbage transfer station - Google Patents

Abstract

The invention relates to a filmless integrated treatment system for leachate in a garbage transfer station, including a raw water tank, a grid tank, a regulating tank, a biochemical treatment device, a flocculation sedimentation tank, a zeolite adsorption tank and an ecological wetland, the outlet of the raw water tank and the grid tank. The inlet is connected, the outlet of the grid tank is connected to the inlet of the regulating tank, the regulating tank is connected to the inlet of the biochemical treatment device through a lift pump, the liquid outlet of the biochemical treatment device is connected to the liquid inlet of the flocculation sedimentation tank, and the dosing device is connected to the flocculation sedimentation tank The dosing port of the method is connected, the liquid outlet of the flocculation sedimentation tank is connected with the inlet of the zeolite adsorption tank, and the outlet of the zeolite adsorption tank is connected with the inlet of the ecological wetland; the treatment method is also disclosed. The invention combines simple physical and chemical technology + biochemical technology + wetland technology, low investment cost, low difficulty in operation and maintenance, no secondary pollution of concentrated liquid, and can reach GB/T31962-2015 "Water Quality Standards for Sewage into Urban Sewers" A-level discharge after treatment Standard, greatly saving the power and energy consumption of operation.

Description

Membraneless integrated treatment system and method for leachate of garbage transfer station

technical field

The invention relates to the technical field of sewage treatment, in particular to a membraneless integrated treatment system and method for leachate in a garbage transfer station.

Background technique

In order to reduce the volume and volume of bulk garbage, the garbage needs to be compressed after being transported to the transfer station. In the process of high compression, the water contained in the garbage is squeezed out. This part of the waste water is called compressed seepage. filtrate. The compressed leachate in the waste water of the garbage transfer station is the main source of pollutants. If it is not treated properly, it will seep into the surrounding soil and groundwater, causing irreversible environmental pollution. It is very difficult to deal with the pollution after it is polluted. It is not only harmful to the environment, but also a potential threat to human health. If pollutants enter the human body through the food chain, it will seriously affect human health. Therefore, landfill leachate must be treated effectively to minimize its impact on the environment.

At present, the treatment of leachate in transfer stations often uses membrane treatment technology, including membrane bioreactor (MBR) technology for sewage treatment. MBR uses microfiltration and ultrafiltration membranes to replace traditional secondary sedimentation tanks. A complete separation between solid retention time (SRT, ie sludge sludge age) and hydraulic retention time (HRT) is achieved. Under higher effluent requirements, nanofiltration membranes and reverse osmosis membranes will also be equipped, which have a significant effect on reducing the concentration of pollutants and meet the emission requirements.

However, for the treatment of waste water in the waste transfer station, although the effect of membrane treatment is acceptable, the investment cost of this process is relatively high, and for the leachate of the transfer station with a high concentration of pollutants, it is easy to pollute the membrane and cause serious pollution to the membrane. The operation and management bring inconvenience, and the cleaning and replacement of the membrane will also increase the operating cost. At the same time, the treatment of the concentrate after membrane filtration is also a major problem that needs to be solved.

Contents of the invention

The purpose of the present invention is to overcome the shortcomings of the prior art, and provide a membraneless integrated treatment system and method for leachate in a garbage transfer station, which has low cost, simple operation and maintenance, no secondary pollution of concentrated liquid, and can reach GB/T after treatment. T31962-2015 "Water Quality Standards for Discharge of Sewage into Urban Sewers" Class A discharge standard.

The purpose of the present invention is achieved through the following technical solutions:

The membraneless integrated leachate treatment system of the garbage transfer station includes a raw water tank, a grid tank, a regulating tank, a biochemical treatment device, a flocculation sedimentation tank, a zeolite adsorption tank and an ecological wetland. The outlet of the raw water tank and the inlet of the grid tank connected, the outlet of the grid tank is connected to the inlet of the adjustment tank, the adjustment tank is connected to the inlet of the biochemical treatment device through a lift pump, the liquid outlet of the biochemical treatment device is connected to the liquid inlet of the flocculation sedimentation tank, The dosing device is connected to the dosing port of the flocculation-settling tank, the liquid outlet of the flocculation-settling tank is connected to the inlet of the zeolite adsorption tank, and the outlet of the zeolite adsorption tank is connected to the inlet of the ecological wetland.

Further, the biochemical treatment device includes an anaerobic tank, a primary aerobic tank, a primary sedimentation tank, a facultative oxygen tank, a secondary aerobic tank, a secondary sedimentation tank and an aeration assembly, and the outlet of the lift pump is connected to the The anaerobic tank is connected, the outlet of the anaerobic tank is connected with the inlet of the first-level aerobic tank, the outlet of the first-level aerobic tank is connected with the inlet of the first-level sedimentation tank, and the liquid outlet of the first-level sedimentation tank is connected with the The inlet of the aerobic tank is connected, the outlet of the aerobic tank is connected with the inlet of the secondary aerobic tank, the upper outlet of the secondary aerobic tank is connected with the inlet of the secondary sedimentation tank, and the liquid outlet of the secondary sedimentation tank Connected to the liquid inlet of the flocculation sedimentation tank, the aeration component provides oxygen for the primary aerobic tank, facultative tank and secondary aerobic tank respectively,

The sludge outlet of the first-stage sedimentation tank is connected with a first sludge discharge pipe, and the middle part of the first sludge discharge pipe is connected with one end of the first sludge return pipe, and the first sludge return pipe The other end is connected to the anaerobic tank, and the first sludge return pump is installed on the pipeline of the first sludge return pipe,

The sludge outlet of the secondary sedimentation tank is connected with a second sludge discharge pipe, the middle part of the second sludge discharge pipe is connected with one end of the second sludge return pipe, and the second sludge return pipe The other end of the tank is connected to the inlet of the aerobic tank, and a second sludge return pump is installed on the pipeline of the second sludge return pipe,

The lower outlet of the secondary aerobic tank is connected to one end of the mixed liquid return pipe, the other end of the mixed liquid return pipe is connected to the inlet of the aerobic tank, and a mixed liquid return pipe is installed on the pipeline of the mixed liquid return pipe. Pump.

Further, the aeration assembly includes an air pump, a main pipe, a branch pipe and a microporous aeration head, the outlet of the air pump is connected to the main pipe, and a plurality of branch pipes are sequentially connected to the pipe of the main pipe, and the outlets of each branch pipe are respectively installed There is a microporous aeration head, and the microporous aeration head respectively sinks into the bottom of the primary aerobic tank, the bottom of the facultative oxygen tank and the bottom of the secondary aerobic tank.

Further, the dosing device includes a dosing tank, a dosing tube and a dosing pump, one end of the dosing tube is connected to the outlet of the dosing tank, and the other end of the dosing tube is connected to the dosing tank of the flocculation sedimentation tank. The medicine port is connected, and a medicine dosing pump is installed on the pipeline of the medicine dosing pipe.

Further, the first-level aerobic pool, the facultative oxygen pool and the second-level aerobic pool are respectively filled with combined fillers, the combined fillers are composed of elastic three-dimensional fillers and ecological bases, and the filling rate of the combined fillers is 60-80 %, the microporous aeration head is located at the bottom of the corresponding combined packing.

Further, the volume ratio of the anaerobic tank, the primary aerobic tank, the facultative oxygen tank and the secondary aerobic tank is 4:5-6:4:5-6.

The membraneless integrated treatment method for leachate in a garbage transfer station uses the membraneless integrated treatment system for leachate in a garbage transfer station, including the following steps:

S1. Store the leachate produced by the garbage transfer station in the raw water tank, and the leachate in the raw water tank enters the grid pool, and the grid pool removes high-concentration suspended solids, large-size pollutants, and some organic matter in the leachate. filter out;

S2. The leachate overflows from the grid pool into the adjustment tank, and the leachate is adjusted to make it evenly mixed;

S3. The leachate treated in the regulating tank enters the biochemical treatment device through the lifting pump, and the leachate is denitrified and dephosphorized, and organic pollutants are removed at the same time;

S4. The effluent from the biochemical treatment device enters the flocculation-sedimentation tank, and the flocculant is added to the flocculation-settling tank through the dosing device. The effluent from the liquid outlet of the flocculation-settling tank passes through the zeolite adsorption tank for adsorption, and the effluent from the outlet of the zeolite adsorption tank passes through the ecological wetland. Then discharge directly, the discharged water quality: COD content ≤ 200mg/L, ammonia nitrogen content ≤ 15mg/L, total phosphorus content ≤ 5mg/L.

Further, in step S3, when the biochemical treatment device treats the leachate, it is divided into two-stage AO treatment, wherein: the first-stage AO treatment is completed by the anaerobic pond, the first-stage aerobic pond and the first-stage sedimentation pond, and the anaerobic pond The phosphorus-accumulating microorganisms in the process release phosphorus, and the first-level aerobic tank performs excessive phosphorus absorption, and the sludge return ratio of the first-level AO treatment is 60-85%; the second-level AO treatment consists of facultative The aerobic tank and the secondary sedimentation tank are completed, and biological denitrification is carried out. The sludge reflux ratio of the second-stage AO treatment is 60-80%, and the mixed liquor reflux ratio is 150-250%.

Further, the treatment time of the anaerobic pool is 2-3 days, the treatment time of the primary aerobic pool is 2.5-4.5 days, the treatment time of the facultative oxygen pool is 2-3 days, and the treatment time of the secondary aerobic pool is 2.5-4.5 days. 4.5 days.

Further, in step S4, the flocculant is PAFC coagulant.

The present invention has the following advantages:

1. Combining physical and chemical technology + biochemical technology + wetland technology, it can reach the A-level discharge standard of GB/T31962-2015 "Water Quality Standards for Discharge of Sewage into Urban Sewers", which greatly saves the power and energy consumption of operation.

2. The composite filler in the form of elastic three-dimensional filler and ecological base phase is applied to wastewater treatment. Experiments have proved that the composite filler has fast film formation, rich microbial phases, and high pollutant degradation efficiency when treating the leachate of the transfer station. Advantages, significantly improving the efficiency of biochemical pools to remove pollutants.

3. Under the appropriate sludge reflux ratio and mixed liquor reflux ratio, the two-stage AO can bear high sludge load, can handle high-concentration transfer station leachate, and operates stably.

4. Provides a detailed domestication method of biochemical pool sludge, which can shorten the period of sludge domestication and make the system reach a stable operating state in advance.

5. The ecological wetland can re-purify the physical and biochemical effluent, the sand and gravel can absorb suspended solids, and the plants can absorb nutrients.

6. Compared with membrane treatment, the investment cost and operating cost are lower, which is more in line with the current development trend of social technology.

7. The core part of the combined process is the use of activated sludge technology. The technology is mature, the difficulty of operation and maintenance is low, and there is no membrane pollution, which solves the problem of using the membrane process to produce concentrated liquid.

Description of drawings

Fig. 1 is a structural representation of the present invention;

Fig. 2 is the frame connection schematic diagram of the present invention;

Fig. 3 is the structural representation of the biochemical treatment device of the present invention;

Fig. 4 is a schematic structural view of the aeration assembly of the present invention;

Fig. 5 is the structural representation of the dosing device of the present invention;

Fig. 6 is the COD concentration curve figure of the present invention in different stages in two-stage AO treatment;

Fig. 7 is the ammonia nitrogen concentration curve figure of different stages in the two-stage AO treatment of the present invention;

Fig. 8 is the total phosphorus concentration curve figure of the present invention in different stages in two-stage AO treatment;

Fig. 9 is the COD concentration graph of different stages in the embodiment of the present invention 1;

Fig. 10 is the COD removal rate curve diagram of different stages in the embodiment of the present invention 1;

Fig. 11 is the ammonia nitrogen concentration curve diagram in different stages in embodiment 1 of the present invention;

Fig. 12 is the curve chart of ammonia nitrogen removal rate in different stages in Example 1 of the present invention;

Fig. 13 is the total phosphorus concentration curve figure of different stages in the embodiment of the present invention 1;

Fig. 14 is the graph of total phosphorus removal rate in different stages in the embodiment of the present invention 1;

Fig. 15 is the COD concentration graph of different stages in the embodiment of the present invention 2;

Fig. 16 is the COD removal rate curve diagram of different stages in the embodiment of the present invention 2;

Fig. 17 is a curve diagram of ammonia nitrogen concentration at different stages in Example 2 of the present invention;

Fig. 18 is the curve chart of ammonia nitrogen removal rate at different stages in Example 2 of the present invention;

Fig. 19 is a curve diagram of total phosphorus concentration at different stages in Example 2 of the present invention;

Fig. 20 is the graph of total phosphorus removal rate in different stages in Example 2 of the present invention;

In the figure: 1-raw water tank, 2-grid tank, 3-regulating tank, 4-lift pump, 5-biochemical treatment device, 5a-anaerobic tank, 5b-first-level aerobic tank, 5c-first-level sedimentation tank , 5d-aerobic tank, 5e-secondary aerobic tank, 5f-secondary sedimentation tank, 5g-aeration component, 5g1-air pump, 5g2-director, 5g3-branch, 5g4-microporous aeration head, 5h- The first sludge discharge pipe, 5i-the first sludge return pipe, 5j-the first sludge return pump, 5k-the second sludge discharge pipe, 5m-the second sludge return pipe, 5n-the second sewage Mud return pump, 5p-mixed liquid return pipe, 5q-mixed liquid return pump, 6-flocculation sedimentation tank, 7-dosing device, 7a-dosing tank, 7b-dosing pipe, 7c-dosing pump, 8- Zeolite adsorption pool, 9-ecological wetland.

Detailed ways

The present invention will be further described below in conjunction with the accompanying drawings, but the protection scope of the present invention is not limited to the following description.

As shown in Figure 1 and Figure 2, the membraneless integrated leachate treatment system of the garbage transfer station includes a raw water tank 1, a grid tank 2, a regulating tank 3, a biochemical treatment device 5, a flocculation sedimentation tank 6, a zeolite adsorption tank 8 and Ecological wetland 9, the outlet of the raw water tank 1 is connected to the inlet of the grid pool 2, the outlet of the grid pool 2 is connected to the inlet of the regulating pond 3, and the regulating pond 3 is connected to the inlet of the biochemical treatment device 5 Connected by the lifting pump 4, the liquid outlet of the biochemical treatment device 5 is connected with the liquid inlet of the flocculation sedimentation tank 6, the dosing device 7 is connected with the dosing port of the flocculation sedimentation tank 6, and the liquid outlet of the flocculation sedimentation tank 6 is connected with the liquid inlet of the flocculation sedimentation tank 6. The inlet of the zeolite adsorption pool 8 is connected, and the outlet of the zeolite adsorption pool 8 is connected with the inlet of the ecological wetland 9 . Two screens are set in screen pool 2, one coarse screen and one fine screen, to separate high-concentration suspended solids and pollutants with larger particle sizes in the leachate, so as to avoid the blockage of the subsequent sewage pump; it can also be removed through the screen For a part of organic matter, the function of the regulating tank 3 is to pre-adjust the leachate to form a uniform mixed solution. At the same time, the regulating tank 3 is equipped with an oil separation structure, which can remove most oily substances and prevent grease from entering the biochemical treatment device. 5. The biochemical treatment device 5 denitrifies and dephosphorizes the leachate and removes organic pollutants at the same time. The design of the lift pump 4 can form a stable supply of leachate and increase the flow of leachate. Zeolite is selected as the adsorption material , the particle size is 5-10mm, and the filling rate in the zeolite adsorption pool 8 is 50-70%. Using zeolite can further reduce the chromaticity, COD and ammonia nitrogen of the system effluent. The ecological wetland 9 adopts a multi-stage ditch structure. UPVC pipes are used to connect the ditches, and the lower edge of the elbow is used at the connection to avoid blockage. The bottom of the ditch is paved with gravel, ceramic particles, and planting soil, which can filter the suspended solids in the water, and the planted plants can absorb the nutrients in the water again, reducing the concentration of various pollutants.

Further, as shown in Figure 3, the biochemical treatment device 5 includes an anaerobic pond 5a, a primary aerobic pond 5b, a primary sedimentation pond 5c, a facultative oxygen pond 5d, a secondary aerobic pond 5e, and a secondary sedimentation pond 5f and aeration assembly 5g, the outlet of the lift pump 4 is connected with the anaerobic tank 5a, the outlet of the anaerobic tank 5a is connected with the inlet of the primary aerobic tank 5b, and the outlet of the primary aerobic tank 5b Connected with the inlet of the primary sedimentation tank 5c, the liquid outlet of the primary sedimentation tank 5c is connected with the inlet of the aerobic tank 5d, and the outlet of the aerobic tank 5d is connected with the inlet of the secondary aerobic tank 5e, the The upper outlet of the secondary aerobic tank 5e is connected to the inlet of the secondary sedimentation tank 5f, the liquid outlet of the secondary sedimentation tank 5f is connected to the liquid inlet of the flocculation sedimentation tank 6, and the aeration components 5g are respectively the primary aerobic tanks 5b, facultative oxygen pool 5d and secondary aerobic pool 5e provide oxygen,

The sludge outlet of the primary sedimentation tank 5c is connected with a first sludge discharge pipe 5h, and the middle part of the first sludge discharge pipe 5h is connected with one end of a first sludge return pipe 5i. The other end of the sludge return pipe 5i is connected to the anaerobic tank 5a, and a first sludge return pump 5j is installed on the pipeline of the first sludge return pipe 5i,

The sludge outlet of the secondary sedimentation tank 5f is connected with a second sludge discharge pipe 5k, and the middle part of the second sludge discharge pipe 5k is connected with one end of the second sludge return pipe 5m. The other end of the sludge return pipe 5m is connected to the inlet of the aerobic tank 5d, and a second sludge return pump 5n is installed on the pipeline of the second sludge return pipe 5m,

The lower outlet of the secondary aerobic tank 5e is connected to one end of the mixed liquid return pipe 5p, and the other end of the mixed liquid return pipe 5p is connected to the inlet of the aerobic tank 5d. On the pipeline of the mixed liquid return pipe 5p A mixed liquid return pump 5q is installed.

Further, as shown in Figure 4, the aeration assembly 5g includes an air pump 5g1, a main pipe 5g2, a branch pipe 5g3 and a microporous aeration head 5g4, the outlet of the air pump 5g1 is connected to the main pipe 5g2, and the pipeline of the main pipe 5g2 is sequentially A plurality of branch pipes 5g3 are connected, and a microporous aeration head 5g4 is respectively installed at the outlet of each branch pipe 5g3, and the microporous aeration head 5g4 sinks into the bottom of the primary aerobic pool 5b, the bottom of the facultative pool 5d and The bottom of the secondary aerobic tank 5e.

Further, as shown in Figure 5, the dosing device 7 includes a dosing pool 7a, a dosing tube 7b and a dosing pump 7c, one end of the dosing tube 7b is connected to the outlet of the dosing pool 7a, the The other end of the dosing pipe 7b is connected to the dosing port of the flocculation sedimentation tank 6, and a dosing pump 7c is installed on the pipeline of the dosing pipe 7b.

Further, the first aerobic pool 5b, the aerobic pool 5d and the second aerobic pool 5e are respectively filled with combined fillers, the combined fillers are composed of elastic three-dimensional fillers and ecological bases, and the filling rate of the combined fillers is 60-80%, the microporous aeration head 5g4 is located at the bottom of the corresponding combined packing, the combined packing shears the air bubbles generated by the aeration component 5g, and the biofilm attached to the combined packing is stirred by the updraft This speeds up the renewal of the biofilm. The combined packing in the form of elastic three-dimensional packing and ecological base is applied to wastewater treatment. After laboratory experiments, it is found that the combined packing has fast film formation, rich microbial phase, and degradable pollutants when treating the leachate of the transfer station. The advantages of high efficiency have significantly improved the efficiency of the biochemical pool to remove pollutants.

Further, the volume ratio of the anaerobic pool 5a, the primary aerobic pool 5b, the facultative oxygen pool 5d and the secondary aerobic pool 5e is 4:5～6:4:5～6, the designed volume ratio, It ensures optimum processing quality and processing efficiency.

The membraneless integrated treatment method for leachate in a garbage transfer station uses the membraneless integrated treatment system for leachate in a garbage transfer station, including the following steps:

S1. Store the leachate produced by the garbage transfer station in the raw water tank 1, and the leachate in the raw water tank 1 enters the grid pool 2, and the grid pool 2 removes high-concentration suspended solids and large-size pollutants in the leachate And part of the organic matter is filtered out;

S2. The leachate overflows from the grid tank 2 into the regulating tank 3, and the leachate is adjusted to make it evenly mixed;

S3. The leachate treated in the regulating tank 3 enters the biochemical treatment device 5 through the lifting pump 4, and the leachate is denitrified and dephosphorized, and organic pollutants are removed at the same time;

S4. The effluent from the biochemical treatment device 5 enters the flocculation-settling tank 6, and the flocculant is added to the flocculation-settling tank 6 through the dosing device 7, and the effluent from the liquid outlet of the flocculation-settling tank 6 passes through the zeolite adsorption tank 8 for adsorption, and is adsorbed from the zeolite The effluent from the outlet of the pond 8 is discharged directly after passing through the ecological wetland 9. The discharged water quality: COD content ≤ 200mg/L, ammonia nitrogen content ≤ 15mg/L, total phosphorus content ≤ 5mg/L.

In the above-mentioned membraneless integrated treatment method for the leachate of the garbage transfer station, the biochemical treatment device 5 adopts the sludge inoculation method to domesticate and cultivate microorganisms, and the specific steps for the sludge inoculation method to domesticate and cultivate are as follows: take a water content of 80% to 90% % of dewatered sludge containing aerobic nitrifying bacteria, and then configured into activated sludge with a sludge mass concentration of 3-5g/L, anaerobic pool 5a, primary aerobic pool 5b, facultative pool 5d and secondary 60% of the total volume of activated sludge is respectively injected into the aerobic pool 5e, and the leachate is pumped into the anaerobic pool 5a through the lift pump 4, and the dissolved oxygen in the anaerobic pool is controlled at 0.1-0.5 mg/L. Simultaneously start the aeration component 5g to supply oxygen to the facultative oxygen tank 5d, the primary aerobic pond 5b, and the secondary aerobic pond 5e, and control the dissolved oxygen in the facultative oxygen pond 5d to be 0.5-1mg/L, and the primary aerobic pond 5b and the dissolved oxygen in the secondary aerobic pool 5e is 3-5mg/L. In the first 10 days, inject 5% of the total volume of leachate from the transfer station every 2 days, and inject 5% of the total volume of leachate from the transfer station every day for the next 5 days. After each pool of the biochemical treatment device 5 is full of water, it can be gradually increased. Adjust the leachate inflow of the tank to increase the load until the design inflow is reached, and gradually increase the sludge mass concentration of the nitrification tank to 4-8g/L, and the sludge load reaches 0.8-1.6kgCOD/kgMLSS·d.

Further, in step S3, when the biochemical treatment device 5 processes the leachate, it is divided into two stages of AO (abbreviation of Anoxic Oxic, AO process method is also called anaerobic aerobic process method), wherein: the first stage AO treatment is performed by The anaerobic tank 5a, the first-level aerobic tank 5b and the first-level sedimentation tank 5c are completed, the phosphorus-accumulating microorganisms in the anaerobic tank 5a perform the process of releasing phosphorus, the first-level aerobic tank 5b performs excess phosphorus absorption, and the first-level AO The reflux ratio of the treated sludge is 60-85%; the second-stage AO treatment is completed by the facultative pool 5d, the secondary aerobic pool 5e and the secondary sedimentation pool 5f for biological denitrification, and the sludge treated by the second-stage AO The reflux ratio is 60-80%, and the reflux ratio of the mixed liquid is 150-250%. By designing the reflux ratio, it can improve the treatment efficiency and quality of the whole system for ammonia nitrogen and total phosphorus, and ensure the stability and reliability of the whole system operation. , At the same time, the processing quality is also ensured. The designed two-stage AO treatment process is phosphorus removal and nitrogen removal process respectively, and the two are combined with each other to remove nitrogen and phosphorus while removing organic matter. The two-stage AO biochemical treatment device 5 can stably degrade the leachate, and can adapt to changes in water quality fluctuations. The effluent water quality is stable: the COD content is 500-2000mg/L, as shown in Figure 6, and the ammonia nitrogen content is 50-100mg /L, as shown in Figure 7, the total phosphorus content is 20-40mg/L, as shown in Figure 8.

Further, the treatment time of the anaerobic pool 5a is 2-3 days, the treatment time of the primary aerobic pool 5b is 2.5-4.5 days, the treatment time of the facultative oxygen pool 5d is 2-3 days, and the treatment time of the secondary aerobic pool 5e The time is 2.5-4.5 days.

Further, in step S4, the flocculant is a PAFC coagulant, and the PAFC coagulant is first configured into a solution, pumped into it, the dosage is 500-1000ppm, the coagulation time is 3-5min, and the settling time is 10 ~15min, it can efficiently remove phosphorus and part of COD.

Now, the membraneless integrated treatment method of the leachate of the garbage transfer station is further explained by an embodiment:

Example 1:

The leachate of the garbage transfer station has a daily treatment capacity of 3 tons, with an average COD content of 11,500 mg/L, an average ammonia nitrogen content of 350 mg/L, and a total phosphorus content of 200 mg/L.

According to the leachate characteristics of the above garbage transfer station, the treatment method includes the following steps:

S1. The leachate generated by the garbage transfer station passes through the grid tank 2, and part of the organic matter is removed through the grid;

S2. The leachate enters the regulating tank 3 from the grid pool 2, and the leachate is evenly mixed;

S3. The leachate treated in the regulating tank 3 enters the biochemical treatment device 5 through the lifting pump 4, and the leachate is denitrified and dephosphorized, and organic pollutants are removed at the same time;

S4, the effluent of the biochemical treatment device 5 flows into the flocculation and sedimentation tank 6, and the leachate undergoes flocculation and sedimentation;

S5. The effluent of the supernatant of the coagulation sedimentation tank 6 enters the zeolite adsorption tank 8, and the leachate is discharged into the ecological wetland 9 after being adsorbed and filtered by the zeolite adsorption tank 8, and the leachate is directly discharged after passing through the ecological wetland 9;

The ecological wetland 9 is in the form of a ditch, with gravel laid at the bottom, planting soil, etc., and emergent and floating plants planted. A coarse grid (30 mesh) and a fine grid (60 mesh) are set in the grid pool 2. The regulating pool 3 adopts a liquid storage tank.

The biochemical treatment device 5 is two-stage AO, the first-stage AO is anaerobic + aerobic, the volume ratio is 4:5, and the sludge return ratio is set to 80%; the second-stage AO is facultative + aerobic, the volume ratio is 4:5, Set the sludge backflow to 70%, and the mixed liquor backflow to 150%. The biochemical treatment device 5 adopts the biological contact oxidation method, and is provided with 5 g of combined packing and aeration components. The composite filler is a composite filler in the form of a combination of elastic three-dimensional filler and ecological base, and the filling rate of the composite filler is 70%. The aeration component 5g adopts microporous aeration to perform blast aeration at the bottom of the combined packing.

The biochemical treatment device 5 adopts the sludge inoculation method to domesticate and cultivate microorganisms, and the dewatered sludge containing aerobic nitrifying bacteria has a moisture content of 80% to 90% from a nearby sewage treatment plant, and is configured to have a sludge mass concentration of 3 to 5g/L. sludge water. Inject the activated sludge of 60% of the total volume into the anaerobic pool 5a and the aerobic pool, and drive the transfer station leachate into the anaerobic pool 5a, the facultative pool 5d and the aerobic pool through the lift pump 4, and the anaerobic pool 5a Dissolved oxygen is controlled at 0.1-0.5mg/L. Simultaneously start the air pump 5g1 to supply oxygen to the facultative pool 5d and the aerobic pool, and control the dissolved oxygen in the facultative pool 5d to be 0.5-1 mg/L, and the dissolved oxygen in the aerobic pool to be 3-5 mg/L. In the first 10 days, inject 5% of the total volume of leachate from the transfer station every 2 days, and inject 5% of the total volume of leachate from the transfer station every day for the next 5 days. After each pool of the biochemical treatment device 5 is full of water, it can be gradually increased. Adjust the leachate inflow of the tank to increase the load until the design inflow is reached, and gradually increase the sludge mass concentration of the nitrification tank to 4-8g/L, and the sludge load reaches 0.8-1.6kgCOD/kgMLSS·d.

The dosing pool 7a adopts PLC control system to automatically add medicine, and the coagulant is PAFC coagulant, which is first configured into a concentrated solution and pumped into it. The dosage is 650ppm, and the coagulation time is 3 minutes; the sedimentation time is 12 minutes.

The adsorption pool uses zeolite as the adsorption material, the particle size is 5-10mm, and the filling rate is 50%.

The use of zeolite can further reduce the chroma, COD and ammonia nitrogen of the system effluent.

The ecological wetland 9 adopts the form of multi-level ditches, and the ditches of each level are connected by UPVC pipes, and the lower edge of the elbow is used at the joints to avoid blockage. The bottom of the ditch is paved with gravel, ceramic particles, and planting soil, which can filter suspended solids in the water, and the planted plants can absorb the nutrients in the water again, reducing the concentration of various indicators.

When the two-stage AO-coagulation-adsorption process continuously treats the waste water of the garbage transfer station, the COD removal effect of each stage is shown in Figure 9 and Figure 10. The COD value of the influent is between 6750 and 15675mg/L, and the two-stage AO The COD value of the effluent is between 232 and 604mg/L, and most of the organic matter can be removed by two-stage AO stages. The COD value of the effluent from the coagulation unit is between 186 and 320mg/L. The COD value of the effluent from the zeolite unit fluctuates around 70.5-132.5 mg/L. The effluent meets the effluent requirements.

The two-stage AO-coagulation-adsorption combined process for the removal of NH ₃ -N in the waste water of the waste transfer station is shown in Figure 11 and Figure ₁₂ . Between L, the NH ₃ -N value of the two-stage AO effluent is between 18.9 and 70.2mg/L, the NH ₃ -N value of the effluent of the coagulation unit is between 11.3 and 23.1, and the NH ₃ -N value of the effluent of the zeolite unit is 3.2～ Fluctuating up and down between 7.6mg/L.

The two-stage AO-coagulation-zeolite combined process for the removal of TP (total phosphorus) in the waste water of the waste transfer station is shown in Figure 13 and Figure 14, and the TP value (total phosphorus value) of the influent is between 119 and 244 mg/L , The TP value of the two-stage AO effluent is between 7.5 and 17.5mg/L, the TP value of the effluent of the coagulation unit is between 4.8 and 12.5mg/L, and the TP value of the effluent of the zeolite unit is between 3.2 and 4.3mg/L. The effluent meets the requirements.

Example 2:

The leachate of the garbage transfer station has a daily treatment capacity of 5t, with an average COD content of 12,500mg/L, an average ammonia nitrogen content of 380mg/L, and a total phosphorus content of 255mg/L.

According to the leachate characteristics of the above garbage transfer station, the treatment method includes the following steps:

S1. The leachate generated by the garbage transfer station passes through the grid tank 2, and part of the organic matter is removed through the grid;

S2. The leachate enters the regulating tank 3 from the grid pool 2, and the leachate is evenly mixed;

S3. The leachate treated in the regulating tank 3 enters the biochemical treatment device 5 through the lifting pump 4, and the leachate is denitrified and dephosphorized, and organic pollutants are removed at the same time;

S4, the effluent of the biochemical treatment device 5 flows into the flocculation and sedimentation tank 6, and the leachate undergoes flocculation and sedimentation;

S5. The effluent of the supernatant of the coagulation sedimentation tank 6 enters the zeolite adsorption tank 8, and the leachate is discharged into the ecological wetland 9 after being adsorbed and filtered by the zeolite adsorption tank 8, and the leachate is directly discharged after passing through the ecological wetland 9;

The ecological wetland 9 is in the form of a ditch, with gravel laid at the bottom, planting soil, etc., and emergent and floating plants planted. A coarse grid (40 mesh) and a fine grid (70 mesh) are set in the grid pool.

The regulating pool 3 adopts a liquid storage tank.

The biochemical treatment device 5 is two-stage AO, the first-stage AO is anaerobic + aerobic, the volume ratio is 2:3, and the sludge return ratio is set to 70%; the second-stage AO is facultative + aerobic, the volume ratio is 2:3, and the set Sludge backflow 80%, mixed liquid backflow 200%. The biochemical treatment device 5 adopts the biological contact oxidation method, and is provided with 5 g of combined packing and aeration components. The filler is a composite filler in the form of a combination of elastic three-dimensional filler and ecological base, and the filling rate of the composite filler is 70%. The aeration component 5g adopts microporous aeration to perform blast aeration at the bottom of the filler.

The biochemical treatment device 5 adopts the sludge inoculation method to domesticate and cultivate microorganisms, and the dewatered sludge containing aerobic nitrifying bacteria has a moisture content of 80% to 90% from a nearby sewage treatment plant, and is configured to have a sludge mass concentration of 3 to 5g/L. sludge water. Inject the activated sludge of 60% of the total volume into the anaerobic pool 5a and the aerobic pool, and drive the transfer station leachate into the anaerobic pool 5a, the facultative pool 5d and the aerobic pool through the lift pump 4, and the anaerobic pool 5a Dissolved oxygen is controlled at 0.1-0.5mg/L. Simultaneously start the air pump 5g1 to supply oxygen to the facultative pool 5d and the aerobic pool, and control the dissolved oxygen in the facultative pool 5d to be 0.5-1 mg/L, and the dissolved oxygen in the aerobic pool to be 3-5 mg/L. In the first 10 days, inject 5% of the total volume of leachate from the transfer station every 2 days, and inject 5% of the total volume of leachate from the transfer station every day for the next 5 days. After each pool of the biochemical treatment device 5 is full of water, it can be gradually increased. Adjust the leachate inflow of the tank to increase the load until the design inflow is reached, and gradually increase the sludge mass concentration of the nitrification tank to 4-8g/L, and the sludge load reaches 0.8-1.6kgCOD/kgMLSS·d.

The dosing pool 7a adopts PLC control system to automatically add medicine, and the coagulant is PAFC coagulant, which is first configured into a concentrated solution and injected with a pump. The dosage is 750ppm, and the coagulation time is 5 minutes; the precipitation time is 15 minutes.

The adsorption pool uses zeolite as the adsorption material, with a particle size of 5-10 mm and a filling rate of 60%.

The use of zeolite can further reduce the chroma, COD and ammonia nitrogen of the system effluent.

The ecological wetland 9 adopts the form of multi-level ditches, and the ditches of each level are connected by UPVC pipes, and the lower edge of the elbow is used at the joints to avoid blockage. The bottom of the ditch is paved with gravel, ceramic particles, and planting soil, which can filter suspended solids in the water, and the planted plants can absorb the nutrients in the water again, reducing the concentration of various indicators.

When the two-stage AO-coagulation-adsorption process continuously treats the waste water of the garbage transfer station, the COD removal effect of each stage is shown in Figure 15 and Figure 16. The COD value of the influent is between 9325 and 13675mg/L The COD value of AO effluent is between 172 and 742mg/L, and most of the organic matter can be removed by two-stage AO stages. The COD value of the effluent from the coagulation unit is between 82.5 and 252.5 mg/L, and the COD value of the effluent from the zeolite unit fluctuates around 126 to 192.5 mg/L. The effluent meets the effluent requirements.

The two-stage AO-coagulation-adsorption combined process for the removal of _NH3 -N in the waste water of the waste transfer station is shown in Figure 17 and Figure 18. During the period, the NH ₃ -N value of the two-stage AO effluent is between 18.9-50.9mg/L, the NH ₃ -N value of the effluent of the coagulation unit is between 10.1-19.9, and the NH ₃ -N value of the effluent of the zeolite unit is 3.8-9.2mg Float up and down between /L. The effluent meets the requirements.

The two-stage AO-coagulation-zeolite combined process for the removal of TP in the waste water of the waste transfer station is shown in Figure 19 and Figure 20. The TP value of the influent water is between 196.4 and 407 mg/L, and the TP value of the two-stage AO effluent is 10 ～34.9mg/L, the TP value of the effluent of the coagulation unit is between 6.8～14mg/L, and the TP value of the effluent of the zeolite unit fluctuates between 3.9～4.8mg/L. The effluent meets the requirements.

Although the embodiments of the present invention have been shown and described, those skilled in the art can understand that various changes, modifications and substitutions can be made to these embodiments without departing from the principle and spirit of the present invention. and modifications, the scope of the invention is defined by the appended claims and their equivalents.

Claims (10)

1. leachate in garbage transfer station is without film integrated processing system, it is characterised in that: including raw water water tank (1), grid pond (2), conditioning tank (3), biochemical treatment apparatus (5), flocculation sedimentation tank (6), zeolite adsorption tank (8) and ecological wetland (9), the original The outlet of water tank (1) is connect with the entrance of grid pond (2), and the outlet of the grid pond (2) and the entrance of conditioning tank (3) connect It connects, the conditioning tank (3) is connect with the entrance of the biochemical treatment apparatus (5) by elevator pump (4), the biochemical treatment apparatus (5) liquid outlet is connect with the liquid inlet of flocculation sedimentation tank (6), the dosing mouth of chemicals dosing plant (7) and flocculation sedimentation tank (6) Connection, the liquid outlet of the flocculation sedimentation tank (6) are connect with the entrance of zeolite adsorption tank (8), the zeolite adsorption tank (8) Outlet is connect with the entrance of ecological wetland (9).

2. leachate in garbage transfer station according to claim 1 is without film integrated processing system, it is characterised in that: the life Changing processing unit (5) includes that anaerobic pond (5a), level-one aerobic tank (5b), first stage precipitation tank (5c), oxygen compatibility pool (5d), second level are aerobic Pond (5e), second-level settling pond (5f) and aeration component (5g), the outlet of the elevator pump (4) is connect with anaerobic pond (5a), described The outlet of anaerobic pond (5a) is connect with the entrance of level-one aerobic tank (5b), and the outlet of the level-one aerobic tank (5b) and level-one precipitate The entrance in pond (5c) connects, and the liquid outlet of the first stage precipitation tank (5c) is connect with the entrance of oxygen compatibility pool (5d), described and oxygen The outlet in pond (5d) is connect with the entrance of second level aerobic tank (5e), the upper outlet and two-stage precipitation of the second level aerobic tank (5e) The entrance in pond (5f) connects, and the liquid outlet of second-level settling pond (5f) is connect with the liquid inlet of flocculation sedimentation tank (6), the exposure Pneumatic module (5g) is respectively that level-one aerobic tank (5b), oxygen compatibility pool (5d) and second level aerobic tank (5e) provide oxygen,

The sludge outlet of the first stage precipitation tank (5c) is connected with the outer comb (5h) of the first sludge, the outer comb of first sludge The middle part of (5h) is connect with the one end of the first mud return line (5i), the other end and anaerobism of first mud return line (5i) Pond (5a) connects, and is equipped with the first sludge reflux pump (5j) on the pipeline of first mud return line (5i),

The sludge outlet of the second-level settling pond (5f) is connected with the outer comb (5k) of the second sludge, the outer comb of second sludge The middle part of (5k) is connect with the one end of the second mud return line (5m), the other end of second mud return line (5m) and and oxygen The entrance in pond (5d) connects, and is equipped with the second sludge reflux pump (5n) on the pipeline of second mud return line (5m),

The lower part outlet of the second level aerobic tank (5e) is connect with one end of mixed liquor return pipe (5p), the mixed liquor return pipe The other end of (5p) is connect with the entrance of oxygen compatibility pool (5d), and mixed liquor is equipped on the pipeline of the mixed liquor return pipe (5p) and is returned Stream pump (5q).

3. leachate in garbage transfer station according to claim 2 is without film integrated processing system, it is characterised in that: the exposure Pneumatic module (5g) includes air pump (5g1), is responsible for (5g2), branch pipe (5g3) and micro porous aeration head (5g4), the air pump (5g1) Outlet is connect with supervisor (5g2), is connected with more branch pipes (5g3), every branch pipe (5g3) in turn on the pipeline of supervisor (5g2) Exit be separately installed with a micro porous aeration head (5g4), micro porous aeration head (5g4) sinks to level-one aerobic tank (5b) respectively The bottom of bottom, the bottom of oxygen compatibility pool (5d) and second level aerobic tank (5e).

4. leachate in garbage transfer station according to claim 1 is without film integrated processing system, it is characterised in that: described to add Medicine device (7) includes dosing pond (7a), chemical feed pipe (7b) and dosing pump (7c), one end and dosing pond of the chemical feed pipe (7b) The outlet of (7a) connects, and the other end of the chemical feed pipe (7b) is connect with the dosing mouth of flocculation sedimentation tank (6), the chemical feed pipe Dosing pump (7c) is installed on the pipeline of (7b).

5. leachate in garbage transfer station according to claim 3 is without film integrated processing system, it is characterised in that: described one It is separately filled with composite filling in grade aerobic tank (5b), oxygen compatibility pool (5d) and second level aerobic tank (5e), the composite filling is by bullet Property 3-D filler and ecological matrix composition, the filling rate of the composite filling be 60~80%, the micro porous aeration head (5g4) is located at The bottom of corresponding composite filling.

6. leachate in garbage transfer station according to claim 5 is without film integrated processing system, it is characterised in that: described Anaerobic pond (5a), level-one aerobic tank (5b), oxygen compatibility pool (5d) and second level aerobic tank (5e) volume ratio be 4:5~6:4:5~6.

7. leachate in garbage transfer station uses the rubbish as described in claim 1~6 any one without film integral treatment method Terminal percolate is handled without film integrated processing system, it is characterised in that: the following steps are included:

In S1, percolate deposit raw water water tank (1) for generating garbage transfer station, the percolate in raw water water tank (1) enters lattice In grid pond (2), grid pond (2) carries out high concentration suspended matter, big partial size pollutant and a part of organic matter in percolate It filters out；

S2, percolate enter in conditioning tank (3) from grid pond (2) overflow, and percolate is adjusted, and are uniformly mixed it, adjust Save water quality and quantity；

S3, conditioning tank (3) treated percolate enter biochemical treatment apparatus (5) by elevator pump (4), take off to percolate Nitrogen dephosphorization processing, while removing removal organic polluter；

S4, enter flocculation sedimentation tank (6) from the water outlet of biochemical treatment apparatus (5), by chemicals dosing plant (7) to flocculation sedimentation tank (6) flocculant is added in, is adsorbed from the water outlet of flocculation sedimentation tank (6) liquid outlet by zeolite adsorption tank (8), from zeolite The water outlet of adsorption tank (8) outlet is expelled directly out after ecological wetland (9), the water quality of discharge: COD content≤200mg/L, ammonia nitrogen Content≤15mg/L, total phosphorus content≤5mg/L.

8. leachate in garbage transfer station according to claim 7 is without film integral treatment method, it is characterised in that: step S3 In, biochemical treatment apparatus (5) is divided into two-stage AO processing when handling percolate, in which: first order AO processing is by anaerobic pond (5a), level-one aerobic tank (5b) and first stage precipitation tank (5c) are completed, and the poly- phosphorus microorganism in anaerobic pond (5a) release the mistake of phosphorus Journey, level-one aerobic tank (5b) carry out excess and inhale phosphorus, and the return sludge ratio of first order AO processing is 60~85%；Second level AO processing It is completed by oxygen compatibility pool (5d), second level aerobic tank (5e) and second-level settling pond (5f), carries out biological denitrificaion, the dirt of second level AO processing Mud reflux ratio is 60~80%, and return current ratio of the mixed liquid is 150~250%.

9. leachate in garbage transfer station according to claim 8 is without film integral treatment method, it is characterised in that: described to detest Oxygen pond (5a) the processing time is 2~3 days, and level-one aerobic tank (5b) the processing time is 2.5~4.5 days, when oxygen compatibility pool (5d) is handled Between be 2~3 days, second level aerobic tank (5e) handle the time be 2.5~4.5 days.

10. leachate in garbage transfer station according to claim 7 is without film integral treatment method, it is characterised in that: step In S4, the flocculant is PAFC coagulant.