CN112979090A - Method suitable for treating percolate of small and medium-sized refuse transfer stations - Google Patents

Method suitable for treating percolate of small and medium-sized refuse transfer stations Download PDF

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CN112979090A
CN112979090A CN202110296377.6A CN202110296377A CN112979090A CN 112979090 A CN112979090 A CN 112979090A CN 202110296377 A CN202110296377 A CN 202110296377A CN 112979090 A CN112979090 A CN 112979090A
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tank
sludge
ozone
aeration
percolate
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程磊
单龙
孔德军
周立南
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Xuzhou XCMG Environment Technology Co Ltd
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Xuzhou XCMG Environment Technology Co Ltd
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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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • 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
    • 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

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)

Abstract

A method suitable for treating percolate from small and medium-sized refuse transfer stations comprises filtering percolate from refuse by using a percolate grating to remove large garbage; adjusting the pH value to 6.5-7.5; electrocatalysis ozone micro-aeration air flotation modification deslagging; denitrifying to remove nitrogen, and biochemically degrading organic matters; deepening treatment, and recycling or discharging the treated wastewater; the sludge is recharged into the garbage pile body and is rolled out along with the station body after being compressed. The treatment method of the invention ensures the treatment quality of the landfill leachate of the transfer station, reduces the use of medicaments as much as possible, reduces unnecessary processes and equipment, and reduces the treatment investment, operation and maintenance cost of the landfill leachate of the transfer station to the greatest extent.

Description

Method suitable for treating percolate of small and medium-sized refuse transfer stations
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a method suitable for treating percolate of a small and medium-sized refuse transfer station.
Background
The garbage transfer station can generate certain garbage percolate in the process of compressing and transferring the household garbage, and the percolate of the garbage transfer station is displayed according to related reportsThe discharge amount is about 11 percent of the total amount of the garbage, wherein the compressed garbage liquid accounts for 6 percent of the total amount, other waste water accounts for 5 percent of the total amount, and the garbage percolate of the transfer station has high CODcrHigh ammonia nitrogen, high grease, high suspended matter, high pollutant concentration and great treatment difficulty. According to the specification of ' domestic garbage transfer station technical specification ' (CJJ 47-2016) ' rainwater and domestic sewage are considered according to the connection of municipal pipe network, and the treatment way and mode of the garbage percolate and equipment flushing wastewater are considered according to the water environment quality requirement of a transfer station service area. Meanwhile, the forty-five treatings in the explanation of the engineering project construction standard of the domestic waste transfer station (Jian Biao 117) stipulate that the waste leachate generated in the transfer operation process and the production sewage generated in the cleaning of vehicles and equipment are specially treated. The sewage treatment mode of the transfer stations is determined according to the specific conditions of each transfer station, and the sewage can be pretreated according to national and local standards and then discharged into a municipal sewage pipe network, and can also be independently treated to reach the discharge standard. Meanwhile, the determination of the emission standard needs to be determined according to the specific requirements of the environmental evaluation. At present, the garbage percolate at a transfer station is more transported or directly discharged into a municipal sewage pipe network by adopting outward transportation, the outward transportation treatment has the problem of leakage, overflow and drip leakage, the urban environment is influenced, the garbage percolate is directly discharged into the municipal sewage pipe network, the load of the municipal sewage tank is easily increased due to the high pollution concentration of the garbage percolate, the normal operation of the whole municipal sewage tank is influenced, and the percolate at the transfer station is treated on the spot along with the strict requirement of national environmental protection.
From the current treatment process of the landfill leachate of the transfer station, the process combining pretreatment, biological treatment (anaerobic treatment, aerobic treatment) and advanced treatment (membrane method, evaporative crystallization) is mostly adopted, the landfill leachate of the transfer station can be effectively treated, but the treatment process has the following defects:
the percolate of the transfer station has the characteristics of small yield, dispersion and the like, so that the marsh gas generated by anaerobic biochemistry of the percolate is difficult to effectively recover and utilize, even if the percolate is utilized, the marsh gas is difficult to generate economic benefit due to the increase of engineering and maintenance cost, meanwhile, the marsh gas generated after anaerobic treatment has flammable and explosive dangers, the place where the refuse transfer station is located is usually close to residential areas and downtown areas, a large number of sanitation transport vehicles enter and exit, the marsh gas is directly combusted or is recycled after being collected, certain potential safety hazards and the possibility of secondary pollution (hydrogen sulfide, sulfur dioxide and the like) of waste gas exist, and the application of an anaerobic treatment process in the refuse transfer station is limited;
in the conventional landfill leachate treatment process, a double-membrane treatment process of ultrafiltration and reverse osmosis is mostly used, so that the quality of effluent can be well stabilized; but the investment, operation, maintenance and other expenses of membrane treatment are high, 30-40% of concentrated solution can be generated when the percolate of the transfer station is treated by a double-membrane method, evaporation crystallization equipment and operation expenses of the concentrated solution are high, and most evaporation equipment has the phenomena of easy scaling and easy corrosion; therefore, a safe, effective and low-cost technology for treating the percolate level of the transfer station is urgently needed to replace the mainstream double-membrane treatment process.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a method which has high treatment quality and low cost and is suitable for treating percolate of small and medium-sized refuse transfer stations.
The invention is realized by the following technical scheme: a method suitable for treating percolate of small and medium-sized refuse transfer stations comprises the following steps:
s1, filtering the garbage leachate by using a grating to remove large garbage to obtain primary mixed liquor;
s2, lifting the primary mixed liquid into a pH adjusting tank through a pump, adding an alkaline agent to adjust the pH value under the automatic control of a pH online controller, and adjusting the pH value to obtain a secondary mixed liquid;
s3, electro-catalysis ozone micro-aeration air flotation modification deslagging: introducing the secondary mixed liquid into a heterogeneous catalytic oxidation ozone air floatation tank, performing electrocatalytic oxidation, ozone oxidation and ozone micro-aeration air floatation, separating scum generated by micro-aeration by using a scum scraper, and then introducing the scum into a sludge tank to obtain a third mixed liquid;
s4, denitrifying denitrification, and biochemical degradation of organic matters: introducing the third mixed liquid into a denitrification tank, and combining the third mixed liquid with the mud water refluxed in the aerobic biochemical tank in the denitrification tank to form a fourth mixed liquid; introducing the mixed liquor of the fourth time into an aerobic biochemical tank to obtain mixed liquor of the fifth time, placing an MBR membrane in the aerobic tank, and performing negative pressure suction filtration on the mixed liquor of the fifth time under the physical interception effect of the MBR membrane to obtain mixed liquor of the sixth time;
s5, introducing the mixed liquor for six times into an advanced treatment tank for advanced treatment, and recycling or discharging the treated wastewater;
and S6, recharging the sludge into the garbage heap, compressing and then transferring out along with the station body.
It further comprises the following steps: in the step S1, the grid filtration comprises coarse grid filtration and fine grid filtration, the distance between the coarse grids is 50-60mm, the distance between the fine grids is 9-12mm, and the filtered filtrate is introduced into a collection regulating reservoir to control the hydraulic retention time of the material to be 8-12 h.
And step S2, pumping the primary mixed solution into an adjusting tank by a pump, standing for 2-3 h, and adjusting the pH of the primary mixed solution to 6.5-7.5.
In the step S3, obtaining a tertiary mixed solution after the tertiary mixed solution stays for 4-6 hours, wherein the distance between the electrocatalytic oxidation electrode plates in the heterogeneous catalytic oxidation pool is 10-15 cm; the pole plate is made of iron plate or iron alloy plate; the thickness of the polar plate is 9-11 cm; the voltage of the electrocatalytic oxidation pulse direct current is 50-100V, and the current is 30-100 mA/cm2The frequency is 50-500 Hz; the ozone aeration amount is 50-100 g/h; the ozone aeration adopts a plurality of groups of microporous aeration discs, and the aeration discs are made of antioxidant materials.
The aeration disc is made of carbon fiber, organic antioxidant plastic, polyvinyl fluoride or titanium alloy.
In the step S4, the DO concentration of the denitrification pool is 0.3-0.5 mg/L, the pH value is 6.5-7.5, and the HRT is 22-28 h; introducing the mixed solution of the fourth time into an aerobic biochemical tank, wherein the DO concentration is 2-4 mg/L, the pH value is 6.5-7.5, the MLSS is 18-22 g/L, and the HRT is 5-6 d; and (4) carrying out negative pressure suction filtration under the physical action of an MBR membrane, wherein the suction-stop ratio is 8: 3.
In step S4, the MBR membrane is an MBR flat membrane with sharp lines, which is made of a PEFT material.
In the step S5, the advanced treatment time is 1-2 h, and the advanced treatment method of the advanced treatment tank is an ozone oxidation method or an ultraviolet light catalysis ozone oxidation method.
In step S6, the sludge or scum produced in steps S1, S2, S3 and S4 is pumped into a sludge tank, the sludge is periodically pumped into a stack of fresh garbage to be compressed by a sludge pump, the sludge is compressed with the garbage and then is transferred out of the station, and the filtrate enters the next stage of circulation.
The invention has the following advantages: the method for treating the percolate in the small and medium-sized refuse transfer stations directly adopts heterogeneous catalytic oxidation as a pretreatment core process, avoids adding a flocculating and precipitating agent, and greatly reduces the pretreatment cost; by adopting the high-efficiency heterogeneous catalytic air flotation, on the basis of removing part of SS and COD, macromolecule nondegradable organic matters in the leachate of the transfer station can be effectively subjected to chain scission oxidation and further decomposed into micromolecule organic matters which are easily degraded by microorganisms, so that the biodegradability of the modified water body is greatly improved, and the treatment of the leachate of the refuse transfer station by the AO process becomes possible; the advanced treatment at the rear end effectively ensures that the quality of the discharged water meets the water quality standard of GB31962-2015 for discharging sewage into urban sewers; through accounting, the investment cost for treating the refuse leachate of the transfer station is 6-8 ten thousand per ton, the operation cost is 22-28 yuan per ton, the market price is obviously lower than that of the existing transfer station leachate treatment, and the method has obvious market advantages;
the leachate treatment method is simple, the whole process is automatically operated, other links except for membrane assembly cleaning needing manual work can be operated unattended and automatically, manual operation is basically avoided, the labor amount is greatly reduced, the labor cost is reduced, and the leachate treatment method is more practical and convenient for non-professional personnel of a transfer station to operate;
the invention does not use anaerobic treatment process, reduces the generation amount of odor gas, is beneficial to the environment of a treatment area, avoids the condition of methane combustion, improves the safety of the whole process and is more practical; meanwhile, the invention utilizes the ultraviolet light to catalyze the ozone oxidation as the advanced treatment, thereby reducing the treatment cost, ensuring the treatment effect of the percolate, and being effective and practical;
the invention can not only ensure that the treated landfill leachate meets the water quality standard of GB31962-2015 sewage discharge into urban sewer, but also fundamentally remove pollutants in the landfill leachate of a transfer station, and compared with a double-membrane method, the invention has the obvious advantages of no concentrated solution treatment problem, low operation cost and no secondary pollution; compared with the traditional anaerobic biochemical treatment technology, the process has the characteristics of no methane generation, safety, reliability, small occupied area, short retention time and the like; the excess sludge is compressed along with the garbage to be compressed and then is transferred out along with the station body for incineration power generation or landfill, so that the sludge disposal cost is greatly reduced, and the method is environment-friendly and practical; the treatment method provided by the invention realizes the reduction, harmlessness and recycling of the landfill leachate to the maximum extent, does not cause load impact on subsequent treatment after the landfill leachate is managed, is suitable for the treatment of the landfill leachate of a refuse transfer station, and has the advantages of low cost, simplicity in operation, no secondary pollution and good popularization prospect.
Drawings
FIG. 1 is a schematic flow chart of the operation of the present invention.
Detailed Description
As shown in fig. 1, a method suitable for treating percolate from small and medium sized refuse transfer stations comprises the following steps:
s1, filtering the garbage leachate by using a grating to remove large garbage to obtain primary mixed liquor;
s2, lifting the primary mixed liquid into a pH adjusting tank through a pump, adding an alkaline agent to adjust the pH value under the automatic control of a pH online controller, and adjusting the pH value to obtain a secondary mixed liquid;
s3, electro-catalysis ozone micro-aeration air flotation modification deslagging: introducing the secondary mixed liquid into a heterogeneous catalytic oxidation ozone air floatation tank, performing electrocatalytic oxidation, ozone oxidation and ozone micro-aeration air floatation, separating scum generated by micro-aeration by using a scum scraper, and then introducing the scum into a sludge tank to obtain a third mixed liquid;
s4, denitrifying denitrification, and biochemical degradation of organic matters: introducing the third mixed liquid into a denitrification tank, and combining the third mixed liquid with the mud water refluxed in the aerobic biochemical tank in the denitrification tank to form a fourth mixed liquid; introducing the mixed liquor of the fourth time into an aerobic biochemical tank to obtain mixed liquor of the fifth time, placing an MBR membrane in the aerobic tank, and performing negative pressure suction filtration on the mixed liquor of the fifth time under the physical interception effect of the MBR membrane to obtain mixed liquor of the sixth time;
s5, introducing the mixed liquor for six times into an advanced treatment tank for advanced treatment, and recycling or discharging the treated wastewater;
and S6, recharging the sludge into the garbage heap, compressing and then transferring out along with the station body.
In the step S1, the landfill leachate is filtered through a coarse grid in sequence and then is introduced into a collection regulating reservoir, the hydraulic retention time of the materials is controlled to be 8-12h, water quality regulation is carried out, primary mixed liquid is obtained, grid filtration comprises coarse grid filtration and fine grid filtration, the distance between the coarse grids is 50-60mm, and the distance between the fine grids is 9-12 mm; according to the invention, the garbage leachate is filtered through a grating to intercept larger suspended garbage and particles in the leachate, and then the water quantity of uniform water quality is regulated through a collection regulating tank.
In the step, the COD content of the landfill leachate is 24000-41000mg/L, the BOD5 content is 11000-23000mg/L, the concentration of suspended matters is 11400-12600mg/L, the content of ammonia nitrogen is 690-780mg/L, the content of total nitrogen is 1450-1840mg/L, the content of total phosphorus is 130-160mg/L, and the pH value is 4.5-6.5.
In the step S2, pumping the primary mixed liquid into an adjusting tank by a pump, staying for 2-3 h, adding an alkaline medicament to adjust the pH value under the automatic control of a pH online controller, adjusting the pH value of the primary mixed liquid to 6.5-7.5, and if the pH value of the leachate is in the range, not adjusting; in the invention, the pH value of the primary mixed liquid is adjusted to 6.5-7.5 after the collection tank, so that the subsequent heterogeneous catalytic oxidation and biochemical treatment are facilitated.
In step S3, the pH of the wastewater is adjusted to obtain a secondary mixed solution, the secondary mixed solution is introduced into a multi-phase catalytic oxidation ozone air flotation tank to perform electrocatalytic ozone combined oxidation and ozone micro-aeration air flotation, and the tertiary mixed solution is obtained after the retention time is 4-6 hours.
Wherein the distance between electrocatalytic oxidation electrode plates in the heterogeneous catalytic oxidation cell is 10-15 cm; the pole plate is made of iron plate or iron alloy plate; the thickness of the polar plate is 9-11 mm; the voltage of the electrocatalytic oxidation pulse direct current is 50-100V, and the current is 30-100 mA/cm2The frequency is 50-500 Hz; the direct current power supply can be connected to the PLC for control, and the iron plate can be effectively prevented from being passivated by regularly changing the electrode, so that the labor cost is reduced; under the action of an external electric field, an intermediate product (OH, O) with strong oxidation effect is generated through an anode reaction2 、.HO2) The organic matter is oxidatively decomposed to break the long carbon chain (the aromatic compound is epoxidized to fatty acid) and decompose the long carbon chain into a short carbon chain and the short carbon chain into CO2And H2O, finally achieving the purposes of oxidizing and degrading pollutants and improving the biodegradability of the wastewater;
the ozone aeration amount is 50-100 g/h, the odor of the garbage percolate of the transfer station can be effectively reduced by adopting the ozone aeration, and the environmental benefit is good; the effect of treating the landfill leachate by combining ozone oxidation and electrocatalytic oxidation is far higher than that of any single oxidation, and the activity of OH is greatly enhanced by combining oxidation; the ozone has strong oxidizability, can form a group with strong oxidizability-hydroxyl free radical (. OH) in water, can rapidly remove organic pollutants in the wastewater, and can decompose into oxygen by itself without causing secondary pollution; in the invention, ozone micropore aeration is adopted, and modification of water is carried out while pollutants are oxidatively decomposed, so that the original stable colloid in the wastewater is destabilized, and part of heavier particles can form heavier floc sediment which is then discharged into a sludge concentration tank by a sludge discharge pump;
the ozone aeration adopts a plurality of groups of microporous aeration discs, and the aeration discs are made of antioxidant materials. The aeration disc is made of carbon fiber, organic antioxidant plastics, polyvinyl fluoride or titanium alloy and other antioxidant materials, and uniform aeration of ozone is realized as far as possible; meanwhile, an ozone dissolving device can be assembled, so that the aeration ozone dissolving rate is further improved, the ozone utilization rate is improved, and the cost is further reduced. Micro bubbles generated by ozone micropore aeration can be combined with particles in the wastewater to form a combined body with density smaller than that of water, so that the effect of air floatation deslagging is achieved, and SS of the wastewater is effectively reduced.
After the heterogeneous catalytic oxidation air floatation is completed, the removal rate of suspended matters is 60%, the removal rate of COD is 25% and the removal rate of phosphorus is 70%.
In the step S4, introducing the tertiary mixed liquid into a denitrification tank, combining the tertiary mixed liquid with the sludge water refluxed in the aerobic biochemical tank in the denitrification tank to form a quaternary mixed liquid, wherein the DO concentration of the denitrification tank is 0.3-0.5 mg/L, the pH value is 6.5-7.5, and the HRT is 22-28 h; nitrate nitrogen in the mixed liquor of the fourth time is converted into nitrogen under the action of denitrifying bacteria to carry out denitrification and denitrification; wherein the generated excess sludge is discharged into a sludge tank through a sludge discharge pump; in the invention, the mixed liquor of four times is in a denitrification pool, nitrate nitrogen in the mixed liquor of four times is converted into nitrogen under the action of denitrifying bacteria, and is removed from the wastewater; after denitrification is completed, the conversion rate of nitrate nitrogen is 96 percent, and the decomposition rate of organic pollutants is 99 percent;
introducing the mixed liquor of the fourth time into an aerobic biochemical tank, wherein the DO concentration is 2-4 mg/L, the pH value is 6.5-7.5, the MLSS is 18-22 g/L, the HRT is 5-6 d, the COD load is 25-30 kg/m3/d, the temperature is 15-40 ℃, the reflux ratio of the aerobic biochemical tank to a denitrification tank is 200-400%, and the decomposition removal of organic pollutants and the nitrification of ammonia nitrogen are realized by utilizing nitrifying bacteria and carbonized bacteria in the aerobic tank through aeration to obtain the mixed liquor of the fifth time; the generated sludge and nitrifying liquid return to the denitrification tank through a nitrifying liquid pump;
putting the MBR membrane in an aerobic tank, and performing negative pressure suction filtration on the mixed liquor for five times under the physical interception effect of the MBR membrane to obtain mixed liquor for six times; the generated residual sludge is discharged into a sludge tank through a sludge discharge pump; in the invention, the MBR membrane is subjected to negative pressure suction filtration under the physical action, and the suction-stop ratio is 8: 3; meanwhile, the MBR membrane is provided with a certain treatment allowance (taking a coefficient of 1.5 times); in the actual operation of the invention, a nutrient is not required to be added into the aerobic biochemical tank, but the MBR membrane needs to be subjected to regular back washing so as to prolong the effective service life of the membrane; the backwashing frequency is 2 times per month. The MBR membrane is a flat MBR dazzling membrane made of PEFT material, so that membrane pollution can be effectively reduced, and membrane cleaning frequency is reduced.
In the step S5, the time of the advanced treatment is 1-2 h, the advanced treatment method of the advanced treatment tank is an ozone oxidation method, the ozone aeration amount is 20-30mg/L, ultraviolet light can be used for catalyzing ozone oxidation, oxygen radicals are generated under the catalysis of 254nm ultraviolet light, the oxygen radicals are utilized to react with oxygen and water under the catalysis of 254nm ultraviolet light to generate OH, the strong oxidizing property of the OH is utilized to break carbon-oxygen bonds and carbon-hydrogen bonds of residual small-molecular organic matters, carbon dioxide and water are generated, and the residual pollutants are completely removed. The COD content of the wastewater after advanced treatment is less than 200mg/L, the BOD5 content is less than 25mg/L, the concentration of suspended matters is less than 10mg/L, the content of ammonia nitrogen is less than 25mg/L, the content of total nitrogen is less than 65mg/L, the content of total phosphorus is less than 1.5mg/L, and the pH value is 6.5-7.5. The advanced treatment method can be selected and matched according to the effluent treatment requirement, and the selection principle is set from the aspects of no secondary pollution, cost saving, sustainability, simple operation, convenient management and the like; from the perspective of saving cost, an ozone oxidation method (better ultraviolet light catalysis effect can be matched) can be continuously selected; the ultraviolet light catalytic ozone advanced oxidation advanced treatment selected by the invention can completely enable the effluent to meet the A-level standard of GB31962-2015 Water quality Standard for discharging the sewage into urban sewer.
In step S6, the sludge or scum produced in steps S1, S2, S3 and S4 is pumped into a sludge tank, the sludge is periodically pumped into a stack of fresh garbage to be compressed by a sludge pump, the sludge is compressed with the garbage and then is transferred out of the station, and the filtrate enters the next stage of circulation. The period of temporary storage of sludge in the sludge tank is determined according to the actual environment temperature, the sludge is recharged into the garbage pile body as soon as possible before the anaerobic reaction occurs, and if the sludge cannot be recharged in time, a small amount of sodium hypochlorite is added for sterilization treatment. The sludge treatment method fully utilizes the existing advantages of the transfer station, reduces the investment and use of unnecessary equipment and medicaments to the maximum extent, saves the investment cost and the operation cost, and has incomparable advantages compared with the traditional sludge treatment methods such as slow-setting sedimentation, sludge-water separation, sludge concentration and the like in economic aspects.
Example 1:
s1: filtering the landfill leachate through a coarse grating and a fine grating in sequence, introducing the filtered landfill leachate into a collecting tank, controlling the hydraulic retention time of materials to be 12 hours, and adjusting the water quality to obtain primary mixed liquid; wherein, the distance between the thick grids is 50mm, and the distance between the thin grids is 9 mm;
s2: pumping the primary mixed solution into an adjusting tank by a pump, staying for 2 hours, adding an alkaline medicament under the automatic control of a pH online controller to adjust the pH value of the primary mixed solution to 6.5; adjusting the pH of the wastewater to obtain a secondary mixed solution; wherein the pump is a small submersible screw pump, the flow rate is 1m3/h, the rated power is 0.28kw/h, the rated voltage is 220v, and the lift is 50 m;
s3: introducing the secondary mixed liquid into a heterogeneous catalytic oxidation ozone air floatation tank for electrolysisCatalyzing ozone combined oxidation and ozone micro-aeration air flotation, and standing for 4 hours to obtain a third mixed solution; wherein the ozone aeration rate is 50g/h, the thickness of the electrolytic iron carbon polar plate is 9mm, the distance between the polar plates is 10cm, and the current density is 100mA/cm2The rated voltage is 50V, the frequency of a pulse power supply is 50Hz, the ozone aeration concentration is 50g/h, and a polyvinyl fluoride microporous aeration disc is adopted as an aeration disc;
s4: introducing the tertiary mixed liquid into a denitrification tank, combining the tertiary mixed liquid with the muddy water refluxed from the aerobic biochemical tank in the denitrification tank to form a quaternary mixed liquid, controlling the DO concentration of the denitrification tank to be 0.5mg/L, the pH value to be 6.5, and the HRT to be 22h, converting nitrate nitrogen in the quaternary mixed liquid into nitrogen under the action of denitrifying bacteria, performing denitrification and denitrification, and discharging the generated residual sludge into a sludge tank through a sludge discharge pump; introducing the mixed liquor of the fourth time into an aerobic biochemical tank, controlling the DO concentration to be 2mg/L, the pH value to be 6.5, controlling the MLSS to be 22g/L and the HRT to be 5d, and carrying out aeration decomposition on organic pollutants to obtain mixed liquor of the fifth time; the generated sludge and nitrifying liquid return to the denitrification tank through a nitrifying liquid pump; pumping the residual sludge into a sludge tank through a sludge pump; performing negative pressure suction filtration on the mixed liquor obtained in the fifth time under the physical action of an MBR (membrane bioreactor) membrane to obtain mixed liquor obtained in the sixth time; in the invention, the MBR membrane is subjected to negative pressure suction filtration under the physical action, and the suction-stop ratio is 8: 3; meanwhile, the MBR membrane is provided with a certain treatment allowance (taking a coefficient of 1.5 times); wherein, the MBR membrane component is an imported dazzle line flat membrane component;
s5: introducing the mixed solution for six times into a deep treatment tank for deep treatment, wherein the deep treatment adopts ultraviolet light to catalyze ozone micropore aeration, the ultraviolet spectrum is 254nm, the deep treatment time is 1h, the ozone aeration concentration is 20mg/L, and the treated wastewater is discharged; the effluent meets the A-level standard of GB31962-2015 Water quality Standard for discharging sewage into urban sewers;
s6: sludge treatment: introducing the sludge generated in the steps 1), 2), 3) and 4) into a sludge concentration tank, pumping fresh sludge into a garbage pile to be compressed every week by a sludge pump, compressing the sludge with garbage, then transferring the compressed sludge out along with a station body, and allowing the filter pressing liquid to enter the next stage of circulation.
Example 1 concludes that the landfill leachate to be treated in example 1 has a COD content of 35600mg/L, a BOD5 content of 18300mg/L, a suspended matter concentration of 14400mg/L, an ammonia nitrogen content of 890mg/L, a total nitrogen content of 1750mg/L, a total phosphorus content of 23mg/L and a pH value of 6.2; the COD content of the finally treated wastewater is 357mg/L, the BOD5 content is 163mg/L, the concentration of suspended matters is 5mg/L, the ammonia nitrogen content is 32mg/L, the total nitrogen content is 63mg/L, the total phosphorus content is 6mg/L, and the pH value is 6.9.
Example 2:
s1: filtering the landfill leachate through a coarse grid in sequence, introducing the landfill leachate into a collecting tank, controlling the hydraulic retention time of the material to be 8 hours, and adjusting the water quality to obtain primary mixed liquid; wherein, the distance between the thick grids is 60mm, and the distance between the thin grids is 12 mm;
s2: pumping the primary mixed solution into an adjusting tank by a pump, keeping the primary mixed solution for 3 hours, adding an alkaline medicament under the automatic control of a pH online controller to adjust the pH value of the primary mixed solution to 7.5; adjusting the pH of the wastewater to obtain a secondary mixed solution;
s3: introducing the secondary mixed solution into a heterogeneous catalytic oxidation ozone air floatation tank, performing electrocatalytic ozone combined oxidation and ozone micro-aeration air floatation, and staying for 6 hours to obtain a tertiary mixed solution; wherein the thickness of the electrolytic iron-carbon polar plate is 11mm, the distance between the polar plates is 15cm, and the current density is 10mA/cm2The rated voltage is 100V, the frequency of a pulse power supply is 500Hz., the ozone aeration concentration is 100g/h, and the aeration disc adopts a polyvinyl fluoride microporous aeration disc;
s4: introducing the tertiary mixed liquid into a denitrification tank, combining the tertiary mixed liquid with the muddy water refluxed from the aerobic biochemical tank in the denitrification tank to form a quaternary mixed liquid, controlling the DO concentration of the denitrification tank to be 0.3mg/L, the pH value to be 7.5 and the HRT to be 28h, converting nitrate nitrogen in the quaternary mixed liquid into nitrogen under the action of denitrifying bacteria, performing denitrification and denitrification, and discharging the generated residual sludge into a sludge tank through a sludge discharge pump; introducing the mixed liquor of the fourth time into an aerobic biochemical tank, controlling the DO concentration to be 4mg/L, the pH value to be 7.5, the MLSS concentration to be 18g/L and the HRT concentration to be 6d, and carrying out aeration decomposition on organic pollutants to obtain mixed liquor of the fifth time; the generated sludge and nitrifying liquid return to the denitrification tank through a nitrifying liquid pump; pumping the residual sludge into a sludge tank through a sludge pump; performing negative pressure suction filtration on the mixed liquor obtained in the fifth time under the physical action of an MBR (membrane bioreactor) membrane to obtain mixed liquor obtained in the sixth time; in the invention, the MBR membrane is subjected to negative pressure suction filtration under the physical action, and the suction-stop ratio is 8: 3; meanwhile, the MBR membrane is provided with a certain treatment allowance (taking a coefficient of 1.5 times);
s5: introducing the mixed solution for six times into a deep treatment tank for deep treatment, wherein the deep treatment adopts ultraviolet light to catalyze ozone micropore aeration, the ultraviolet spectrum is 254nm, the deep treatment time is 2 hours, the ozone aeration concentration is 30mg/L, and the treated wastewater is discharged; the effluent meets the A-level standard of GB31962-2015 Water quality Standard for discharging sewage into urban sewers;
s6: sludge treatment: introducing the sludge generated in the steps 1), 2), 3) and 4) into a sludge concentration tank, pumping fresh sludge into a garbage pile to be compressed every week by a sludge pump, compressing the sludge with garbage, then transferring the compressed sludge out along with a station body, and allowing the filter pressing liquid to enter the next stage of circulation.
Example 2 conclusion that the COD content of the landfill leachate to be treated in example 2 is 31600mg/L, the BOD5 content is 16800mg/L, the suspended matter concentration is 12400mg/L, the ammonia nitrogen content is 830mg/L, the total nitrogen content is 1780mg/L, the total phosphorus content is 18mg/L, and the pH value is 4.8:; finally, the COD content of the wastewater obtained by treatment is 420mg/L, the BOD5 content is 130mg/L, the concentration of suspended matters is 8mg/L, the ammonia nitrogen content is 32mg/L, the total nitrogen content is 68mg/L, the total phosphorus content is 4mg/L, and the pH value is 7.6.
The conclusion is that the method of the invention has low investment and operation cost, is suitable for the treatment of the percolate of small and medium-sized refuse transfer stations, and the quality of the percolate waste water of the refuse transfer station can reach the standard after the treatment of the embodiment.
The invention designs a garbage percolate treatment method for a garbage transfer station, which not only can ensure that the treated garbage percolate meets the requirement of A-level discharge standard in GB31962-2015 Water quality Standard for discharging sewage into urban sewer, but also can ensure that various organic matters, heavy metals and salts do not generate secondary pollution, and is environment-friendly and practical; the invention realizes the reduction, harmlessness and reclamation of the landfill leachate to the utmost extent, does not cause the loss of heavy metal ions and highly toxic organic matters in the treatment process, does not generate secondary pollution, does not cause load impact on subsequent treatment, is suitable for the treatment of the landfill leachate of a refuse transfer station, has low investment and operation cost and better popularization prospect.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.

Claims (9)

1. A method suitable for treating percolate of small and medium-sized refuse transfer stations is characterized by comprising the following steps: the method comprises the following steps:
s1, filtering the garbage leachate by using a grating to remove large garbage to obtain primary mixed liquor;
s2, lifting the primary mixed liquid into a pH adjusting tank through a pump, adding an alkaline agent to adjust the pH value under the automatic control of a pH online controller, and adjusting the pH value to obtain a secondary mixed liquid;
s3, electro-catalysis ozone micro-aeration air flotation modification deslagging: introducing the secondary mixed liquid into a heterogeneous catalytic oxidation ozone air floatation tank, performing electrocatalytic oxidation, ozone oxidation and ozone micro-aeration air floatation, separating scum generated by micro-aeration by using a scum scraper, and then introducing the scum into a sludge tank to obtain a third mixed liquid;
s4, denitrifying denitrification, and biochemical degradation of organic matters: introducing the third mixed liquid into a denitrification tank, and combining the third mixed liquid with the mud water refluxed in the aerobic biochemical tank in the denitrification tank to form a fourth mixed liquid; introducing the mixed liquor of the fourth time into an aerobic biochemical tank to obtain mixed liquor of the fifth time, placing an MBR membrane in the aerobic tank, and performing negative pressure suction filtration on the mixed liquor of the fifth time under the physical interception effect of the MBR membrane to obtain mixed liquor of the sixth time;
s5, introducing the mixed liquor for six times into an advanced treatment tank for advanced treatment, and recycling or discharging the treated wastewater;
and S6, recharging the sludge into the garbage heap, compressing and then transferring out along with the station body.
2. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: in the step S1, the grid filtration comprises coarse grid filtration and fine grid filtration, the distance between the coarse grids is 50-60mm, the distance between the fine grids is 9-12mm, and the filtered filtrate is introduced into a collection pool to control the hydraulic retention time of the material to be 8-12 h.
3. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: and step S2, pumping the primary mixed solution into an adjusting tank by a pump, standing for 2-3 h, and adjusting the pH of the primary mixed solution to 6.5-7.5.
4. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: in the step S3, obtaining a tertiary mixed solution after the tertiary mixed solution stays for 4-6 hours, wherein the distance between the electrocatalytic oxidation electrode plates in the heterogeneous catalytic oxidation pool is 10-15 cm; the pole plate is made of iron plate or iron alloy plate; the thickness of the polar plate is 9-11 cm; the voltage of the electrocatalytic oxidation pulse direct current is 50-100V, and the current is 10-100 mA/cm2The frequency is 50-500 Hz; the ozone aeration amount is 50-100 g/h; the ozone aeration adopts a plurality of groups of microporous aeration discs, and the aeration discs are made of antioxidant materials.
5. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 4, wherein the method comprises the following steps: the aeration disc is made of carbon fiber, organic antioxidant plastic, polyvinyl fluoride or titanium alloy.
6. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: in the step S4, the DO concentration of the denitrification pool is 0.3-0.5 mg/L, the pH value is 6.5-7.5, and the HRT is 22-28 h; introducing the mixed solution of the fourth time into an aerobic biochemical tank, wherein the DO concentration is 2-4 mg/L, the pH value is 6.5-7.5, the MLSS is 18-22 g/L, and the HRT is 5-6 d; and (4) carrying out negative pressure suction filtration under the physical action of an MBR membrane, wherein the suction-stop ratio is 8: 3.
7. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: in step S4, the MBR membrane is an MBR flat membrane with sharp lines, which is made of a PEFT material.
8. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: in the step S5, the advanced treatment time is 1-2 h, and the advanced treatment method of the advanced treatment tank is an ozone oxidation method or an ultraviolet light catalysis ozone oxidation method.
9. The method for treating percolate at small and medium-sized refuse transfer stations as claimed in claim 1, characterized in that: in step S6, the sludge or scum produced in steps S1, S2, S3 and S4 is pumped into a sludge tank, the sludge is periodically pumped into a stack of fresh garbage to be compressed by a sludge pump, the sludge is compressed with the garbage and then is transferred out of the station, and the filtrate enters the next stage of circulation.
CN202110296377.6A 2021-03-19 2021-03-19 Method suitable for treating percolate of small and medium-sized refuse transfer stations Withdrawn CN112979090A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114751595A (en) * 2022-04-27 2022-07-15 广州市环境保护工程设计院有限公司 Landfill leachate treatment system and treatment method
CN115321743A (en) * 2022-02-22 2022-11-11 浙江傲世环境服务有限公司 Method for treating garbage leachate of transfer station
CN116813155A (en) * 2023-08-31 2023-09-29 金科环境股份有限公司 System and method for treating silicon wafer cutting fluid wastewater and application

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115321743A (en) * 2022-02-22 2022-11-11 浙江傲世环境服务有限公司 Method for treating garbage leachate of transfer station
CN114751595A (en) * 2022-04-27 2022-07-15 广州市环境保护工程设计院有限公司 Landfill leachate treatment system and treatment method
CN116813155A (en) * 2023-08-31 2023-09-29 金科环境股份有限公司 System and method for treating silicon wafer cutting fluid wastewater and application
CN116813155B (en) * 2023-08-31 2023-12-22 金科环境股份有限公司 System and method for treating silicon wafer cutting fluid wastewater and application

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Application publication date: 20210618