CN102134141A - Method for treating garbage leachate - Google Patents
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- CN102134141A CN102134141A CN2010106001353A CN201010600135A CN102134141A CN 102134141 A CN102134141 A CN 102134141A CN 2010106001353 A CN2010106001353 A CN 2010106001353A CN 201010600135 A CN201010600135 A CN 201010600135A CN 102134141 A CN102134141 A CN 102134141A
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Abstract
The invention discloses a method for treating garbage leachate, comprising the following steps: firstly discharging the garbage leachate into an adjusting tank for homogenizing the water quality for 9-15 days; then discharging the treated garbage leachate into a coagulation reaction tank; then adding a coagulant and a coagulant aid; carrying out precipitation on the garbage leachate; discharging precipitated leachate into a heating system; pumping the heated garbage leachate into an expanded granular sludge bed for anaerobic reaction; discharging the reacted leachate into a sequence intermittent activated sludge reactor for aerobic reaction; filtering the garbage leachate by a nanofiltration membrane of a nanofiltration system; discharging the filtered liquid into a concentration tank for precipitation; discharging supernatant back to the adjusting tank; and discharging precipitated sludge slag into a pressure filter. The sludge slag is discharged into a pressure filter for pressure filtering, and then is conveyed to a landfill site for landfill, and the pressure-filtered liquid is discharged back to the adjusting tank. In the method, the purposes of leading the biochemical treatment effect to be stable, realizing comprehensive utilization of methane, reducing the membrane operation cost and membrane module replacement cost can be achieved.
Description
Technical field
The present invention relates to a kind of sewage water treatment method, particularly a kind of rubbish leachate treatment method.
Background technology
Along with the raising of rapid economy development and living standards of the people, with 9% speed increment, the quantity of sanitary filling field increases China's municipal wastes output thereupon every year on average.Consequent percolate becomes very important problem.Percolate be rubbish stack and the landfill process in, because of free-water, precipitation, runoff and underground water in its organic aerobic or anaerobically fermenting and rubbish infiltrate the high concentrated organic wastewater of complicated component of leaching refuse formation.Contain a large amount of organism, germ, virus, parasite and some hazardous and noxious substances etc. in the percolate, wherein COD and BOD
5Concentration is up to several ten thousand mg/L, but biochemical indicator then changes between 0.1 ~ 0.7; Ammonia nitrogen concentration then can be up to 2000mg/L ~ 3000mg/L; C:N:P is out of proportion.
" household refuse landfill sites pollution control criterion " (GB 16889-2008) requires " household refuse landfill sites should be provided with waste disposal plant; after consumer waste infiltration liquid sewage such as (the containing equalizing tank waste water) pollutant emission standard treated and up to specification, can directly discharge ".Leading indicator is COD
Cr: 100mg/L, BOD
5: 30mg/L, suspended substance: 30mg/L, ammonia nitrogen: 25mg/L, excrement colibacillus group number: 10000/L.Higher special emission standard is then carried out in the area of, ecological environment frailty less for environmental capacity.
Combination procesies such as biochemical process, physico-chemical process, embrane method are present major technology means.Biochemical process is difficult to reach emission standard separately, need be aided with physico-chemical process, embrane method or other treatment processs.Physico-chemical process need consume a large amount of medicaments, and the mud of generation still needs otherwise processed.The embrane method advanced treatment has the characteristics of high efficient and reliable, convenient management, further promotes the use of but defectives such as membrane module cost height, operation and replacement charge height have hindered it.
Summary of the invention
Goal of the invention: at the deficiencies in the prior art, it is low to the invention discloses a kind of cost of manufacture, the method for a kind for the treatment of refuse percolate that running cost is few.
Technical scheme: the invention discloses a kind of method for the treatment of refuse percolate, may further comprise the steps:
(1) percolate is entered the homogenizing water quality of carrying out in the equalizing tank 9 ~ 15 days;
(2) percolate after will handling enters coagulation reaction tank, drops into coagulating agent and coagulant aids and percolate then and carries out precipitating after 8 ~ 15 minutes the reaction, sedimentation time 〉=2 hour; Described coagulating agent is ferric sulfate, bodied ferric sulfate, poly aluminium chloride iron or polymerize aluminum chloride; Described coagulant aids is polyacrylamide, Poly Dimethyl Diallyl Ammonium Chloride or sodium polyacrylate.
(3) percolate with post precipitation enters heating system, and percolate is heated to 36 ~ 38 ℃; Described heating system adopts the tubular heat exchange heating, and thermal source is a steam.
(4) percolate after will heating pumps into the expanded granular sludge bed anaerobic reaction that carries out, and the biogas that reaction produces is delivered to generating set, and electric energy is used for power devices, and waste heat is delivered to heating system; Percolate is reaction times 6 ~ 12h in expanded granular sludge bed, and expanded granular sludge bed temperature-stable is at 35 ~ 37 ℃, and the pH value stabilization of percolate is 7.0 ~ 8.0; Expanded granular sludge bed volumetric loading is 12 ~ 17kgCOD/ (m
3D), expanded granular sludge bed interior percolate upflow velocity is 4 ~ 6m/h;
(5) reacted percolate is entered sequence sequencing batch reactor activated sludge reaction device and carry out aerobic reaction, sequence sequencing batch reactor activated sludge reaction device volumetric loading is 0.1 ~ 0.18kgBOD/ (kgMLSSd), and percolate is 7 ~ 15 days residence time in reactor; Then percolate is entered in the dynamic film bio reaction tank.
(6) be provided with bioreactor of dynamic membrane in the dynamic film bio reaction tank, percolate filters by bioreactor of dynamic membrane, at first carries out 30 minutes preliminary filtration, makes the active sludge flco form stable Dynamic Membrane on bioreactor of dynamic membrane; Preliminary filtering percolate returns and drains into the dynamic film bio reaction tank, after Dynamic Membrane forms percolate is filtered, and the organic pollutant removal rate in the percolate is 70% ~ 80%; Behind the dynamic film bio reaction tank intermediate pool is set, the intermediate pool volume is 30 minutes a bioreactor of dynamic membrane aquifer yield; Intermediate pool is used to hold back the water outlet of initial operating stage after first operation and the back flushing, and the filtered liquid in the intermediate pool is by being pumped back to the dynamic film bio reaction tank; The bioreactor of dynamic membrane bottom is provided with aeration, and gas-water ratio is 15:1; When the Dynamic Membrane water outlet water yield less than designed water 75% the time, utilize clear water and air that membrane module is carried out back flushing, the back flushing water yield is 2 times of aquifer yield; Filtered liquid enters nanofiltration system.
(7) percolate filters by the nanofiltration membrane of nanofiltration system, and filtered liquid enters concentration basin; Nanofiltration membrane is the nanofiltration film.。
(8) filtered liquid enters concentration basin and precipitates, and supernatant liquor returns and drains into equalizing tank, and sedimentary sewage sludge waste slag enters pressure filter.
(9) sewage sludge waste slag carries out press filtration after entering pressure filter, and pressing filtering liquid returns and drains into equalizing tank, and the compression mud after the press filtration is discharged, and is transported to landfill yard and carries out landfill.
The aperture of the described Dynamic Membrane of step 6 is 0.5 ~ 2.0 μ m, and the fenestra road is crooked duct; Go out stream under gravity condition, the water outlet pressure head is 3cm ~ 15cmH
2O, membrane flux are 30L/m
2H.
Sludge loading is 0.2 ~ 0.5kgBOD/ (kgMLSSd) in the described dynamic film bio reaction tank of step 6, and sludge concentration is 4.0g/L ~ 10.0g/L in the reaction tank, and volumetric loading is controlled at 0.5 ~ 2.0 kgCOD/ (m
3D).
The percolate water yield changed greatly with season, time, and water quality is extremely unstable.Therefore be necessary to be provided with bigger equalizing tank, its water yield, water quality are carried out homogenizing.The residence time of equalizing tank is set at 9 days ~ and 15 days, not only can regulate the ununiformity of leachate quality, the water yield, and can produce anaerobism effect preferably.It removes mechanism: remove most suspended substances by precipitation; Be partly dissolved organic matter by anaerobic biological degraded removal; Reduce the influence of waterpower, pollutent impact load, guarantee the steady running of system subsequent technique.
Dosing coagulant and coagulant aids in reaction tank are through the organism, ammonia nitrogen, heavy metal substance and the most suspended substance that react, post precipitation can be removed part in the percolate.Clearance to COD is about 15 ~ 25%, is 75% ~ 90% to the clearance of SS, is about 15% to ammonia-N removal rate.
The waste heat that utilizes the marsh gas power generation unit to produce heats percolate, and its temperature is brought up to 36 ℃ ~ 38 ℃.The lifting of temperature can guarantee stable, the efficient operation of follow-up anaerobic technique, and the stable and high effective operation of anaerobic technique has guaranteed competent biogas generation again, and the two has formed benign cycle preferably.
The grain expansion Sludge Bed obtains higher liquid up-flow speed by effluent recycling, can improve the contact between waste water and the microorganism, has strengthened mass transfer effect, especially is fit to handle the organic waste water of high density.Percolate is after the grain expansion Sludge Bed is handled, and the COD clearance can reach 75% ~ 80%.
Sequence sequencing batch reactor activated sludge reaction device carries out aerobic reaction, can remove most of organism, ammonia nitrogen and toxicant.The delivery ratio of reactor is less, and mixed solution can play the effect of dilution higher concentration water inlet, has capacity of resisting impact load preferably.Long hydraulic detention time helps long nitrifier and the growth of denitrifying bacteria in mud age, and periodic running has guaranteed the effective removal to ammonia nitrogen simultaneously.Reactor is not intake during precipitation, can improve effluent quality.
Aerobic biochemical through sequence sequencing batch reactor activated sludge reaction device is handled, and the biodegradability of waste water reduces, and the conventional activated sludge method is difficult to reach the ideal treatment effect.Bioreactor of dynamic membrane is bred the special bacteria of some hardly degraded organic substances of degradable by the effectively catching to microorganism, and higher sludge concentration also makes bioreactor of dynamic membrane that the treatment effect of waste water is improved greatly simultaneously.The aperture of Dynamic Membrane is controlled at 0.5 μ m ~ 2.0 μ m during steady running, and water outlet SS is almost nil, and turbidity remains on below the 3.0NTU.Adopt gravity-elution, have the low advantage of running cost.
The nanofiltration membrane system is that 200 ~ 1000 organism has very high rejection to molecular weight, can further remove the COD in the waste water, simultaneously ammonia nitrogen, colourity is all had treatment effect preferably.The producing water ratio of nanofiltration membrane system remains on 75%, and dense water is back to the sequence sequencing batch reactor activated sludge reaction and thinks highly of new processing.
Mud/excess sludge that coagulative precipitation tank, grain expansion Sludge Bed, sequence sequencing batch reactor activated sludge reaction device and bioreactor of dynamic membrane produce enters concentration basin, is transported to the landfill yard landfill after press filtration.
Beneficial effect.
Description of drawings
Accompanying drawing is a process flow sheet of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention is further explained.
The invention discloses a kind of method for the treatment of refuse percolate, may further comprise the steps:
(1) percolate is entered the homogenizing water quality of carrying out in the equalizing tank 9 ~ 15 days;
(2) percolate after will handling enters coagulation reaction tank, drops into coagulating agent and coagulant aids and percolate then and carries out precipitating after 8 ~ 15 minutes the reaction, sedimentation time 〉=2 hour; Described coagulating agent is ferric sulfate, bodied ferric sulfate, poly aluminium chloride iron or polymerize aluminum chloride; Described coagulant aids is polyacrylamide, Poly Dimethyl Diallyl Ammonium Chloride or sodium polyacrylate.
(3) percolate with post precipitation enters heating system, and percolate is heated to 36 ~ 38 ℃; Described heating system adopts the tubular heat exchange heating, and thermal source is a steam.
(4) percolate after will heating pumps into the expanded granular sludge bed anaerobic reaction that carries out, and the biogas that reaction produces is delivered to generating set, and electric energy is used for power devices, and waste heat is delivered to heating system; Percolate is reaction times 6 ~ 12h in expanded granular sludge bed, and expanded granular sludge bed temperature-stable is at 35 ~ 37 ℃, and the pH value stabilization of percolate is 7.0 ~ 8.0; Expanded granular sludge bed volumetric loading is 12 ~ 17kgCOD/ (m
3D), expanded granular sludge bed interior percolate upflow velocity is 4 ~ 6m/h;
(5) reacted percolate is entered sequence sequencing batch reactor activated sludge reaction device and carry out aerobic reaction, sequence sequencing batch reactor activated sludge reaction device volumetric loading is 0.1 ~ 0.18kgBOD/ (kgMLSSd), and percolate is 7 ~ 15 days residence time in reactor; Then percolate is entered in the dynamic film bio reaction tank.
(6) be provided with bioreactor of dynamic membrane in the dynamic film bio reaction tank, percolate filters by bioreactor of dynamic membrane, at first carries out 30 minutes preliminary filtration, makes the active sludge flco form stable Dynamic Membrane on bioreactor of dynamic membrane; Preliminary filtering percolate returns and drains into the dynamic film bio reaction tank, after Dynamic Membrane forms percolate is filtered, and the organic pollutant removal rate in the percolate is 70% ~ 80%; Behind the dynamic film bio reaction tank intermediate pool is set, the intermediate pool volume is 30 minutes a bioreactor of dynamic membrane aquifer yield; Intermediate pool is used to hold back the water outlet of initial operating stage after first operation and the back flushing, and the filtered liquid in the intermediate pool is by being pumped back to the dynamic film bio reaction tank; The bioreactor of dynamic membrane bottom is provided with aeration, and gas-water ratio is 15:1; When the Dynamic Membrane water outlet water yield less than designed water 75% the time, utilize clear water and air that membrane module is carried out back flushing, the back flushing water yield is 2 times of aquifer yield; Filtered liquid enters nanofiltration system.
(7) percolate filters by the nanofiltration membrane of nanofiltration system, and filtered liquid enters concentration basin; Nanofiltration membrane is the nanofiltration film.。
(8) filtered liquid enters concentration basin and precipitates, and supernatant liquor returns and drains into equalizing tank, and sedimentary sewage sludge waste slag enters pressure filter.
(9) sewage sludge waste slag carries out press filtration after entering pressure filter, and pressing filtering liquid returns and drains into equalizing tank, and the compression mud after the press filtration is discharged, and is transported to landfill yard and carries out landfill.
Below in conjunction with specific embodiment, the present invention is further specified, but the present invention is not limited to these embodiments.
Embodiment 1:
Adopt the present invention to handle early stage percolate, raw water quality is: COD concentration is 16000 mg/L ~ 30000mg/L, BOD
5Concentration is 11000mg/L ~ 16000mg/L, and ammonia nitrogen concentration is 1080mg/L ~ 1920mg/L, and pH is 6.8 ~ 7.5.It is 80 tons that day is handled the water yield.In this embodiment, the COD mean concns of percolate is about 24000mg/L, BOD
5Mean concns is 13000mg/L, and the ammonia nitrogen mean concns is 1600mg/L.
As shown in the figure, percolate at first passes through equalizing tank, and the residence time is 12 days.The pump hole is established in the equalizing tank bottom, regularly takes the equalizing tank bottom sludge away.
The effusive sewage of equalizing tank enters coagulation basin, drops into bodied ferric sulfate, and dosage is 30mg/L.Drop into polyacrylamide, dosage is 3mg/L.Adopt mechanical stirring, the reaction times is 10 minutes.The settling tank form is a horizontal sedimentation tank, precipitates that supernatant liquor enters heating system after 2 hours.Handle through this unit coagulating sedimentation, macromole suspended particle, COD and part ammonia nitrogen are effectively removed.
Utilize marsh gas power generation unit waste heat, with percolate temperature increase to 36 ℃ ~ 38 ℃.With pump grain expansion Sludge Bed anaerobic reaction tower is sent in the percolate lifting.
Percolate evenly enters reaction zone by the water distributor of grain expansion Sludge Bed bottom.The height of reaction tower is 15m, and diameter is 3.5m, and useful volume is 110m
3, the residence time is 33 hours.Upflow velocity is controlled at 5m/h.Per 7 days spoil disposals of reactor once, by the discharging of the mud discharging mouth of bottom.Adopt tubular heater exchhanger to be incubated, be equipped with automatic temp controller.The biogas that produces is sent into the marsh gas power generation unit, and the waste heat of generation is sent into heating system.Reactor is about 75% to the COD clearance, BOD
5Clearance is about 80%.
Sequence sequencing batch reactor activated sludge reaction device is made as 2, and total hrt is 7.5d.Single pond volume is 320m
3, being of a size of 16 m * 4 m * 5m, delivery ratio is 1:16, moves 2 cycles every day, and wherein the reaction times is 8h, and sedimentation time is 1h, and straining the water time is 1h, begins aeration behind the water inlet 2h.Sequence sequencing batch reactor activated sludge reaction device is about 85% to the COD clearance, and ammonia nitrogen removal frank is about 80%.
The bioreactor of dynamic membrane volume is 24m
3, the residence time is 7.2h.Adopt built-in tubular self-generative dynamic membrane component, the effective film area is 120m
2Wherein the monolithic membrane area is 10m
2, water production rate is 0.3m
3/ h.The water outlet head is that sludge concentration is that 3000mg/L, gas-water ratio start reactor during for 15:1 in the 6cm, reaction tank.The initial stage water outlet enters rearmounted intermediate pool, and useful volume is 2m
3, and use sump pump that it is back to membrane cisterna.After 30 minutes, water outlet is limpid, enters the nanofiltration treatment system.Bioreactor of dynamic membrane is 80% to sequence sequencing batch reactor activated sludge reaction device water outlet COD clearance, BOD
5Clearance is 95%.After the steady running 35 days, effluent flux drops to 0.25m
3/ h utilizes clear water and air that membrane module is carried out back flushing, and the back flushing water yield is 2 times of aquifer yield.Subsequently Dynamic Membrane is regenerated, repeat filtration-cleaning-regenerative process.
The bioreactor of dynamic membrane water outlet is further handled discharging through nanofiltration.Adopt 4 antipollution nanofiltration membrane components, water production rate is greater than 4.5m
3/ h.The control of employing constant pressure frequency conversion, pressure-controlling is at 0.35 ~ 0.40Mpa.
Since the system operation 6 months, stable effluent quality meets the standard of " household refuse landfill sites pollution control criterion " (GB 16889-2008) " the existing and special emission limit of newly-built household refuse landfill sites water pollutant of table 3 " defined fully.
Embodiment 2:
Adopt the present invention to handle the percolate in mid-term, raw water quality is: COD concentration is 5800 ~ 9600mg/L, BOD
5Concentration is 3000mg/L ~ 5250mg/L, and ammonia nitrogen concentration is 800mg/L ~ 1050mg/L, and pH is 7.2 ~ 7.6.It is 100 tons that day is handled the water yield.In this embodiment, the COD mean concns of percolate is about 7600mg/L, BOD
5Mean concns is 3800mg/L, and the ammonia nitrogen mean concns is 950mg/L.
As shown in the figure, percolate at first passes through equalizing tank, and the residence time is 15 days.The pump hole is established in the equalizing tank bottom, regularly takes the equalizing tank bottom sludge away.
The effusive sewage of equalizing tank enters coagulation basin, drops into bodied ferric sulfate, and dosage is 30mg/L.Drop into polyacrylamide, dosage is 3mg/L.Adopt mechanical stirring, the reaction times is 10 minutes.The settling tank form is a horizontal sedimentation tank, precipitates that supernatant liquor enters heating system after 2 hours.Handle through this unit coagulating sedimentation, macromole suspended particle, COD and part ammonia nitrogen are effectively removed.
Utilize marsh gas power generation unit waste heat, with percolate temperature increase to 36 ℃ ~ 38 ℃.With pump grain expansion Sludge Bed anaerobic reaction tower is sent in the percolate lifting.
Percolate evenly enters reaction zone by the water distributor of grain expansion Sludge Bed bottom.The height of reaction tower is 8m, and diameter is 3m, and useful volume is 56m
3, the residence time is 15 hours.Upflow velocity is controlled at 5m/h.Per 7 days spoil disposals of reactor once, by the discharging of the mud discharging mouth of bottom.Adopt tubular heater exchhanger to be incubated, be equipped with automatic temp controller.The biogas that produces is sent into the marsh gas power generation unit, and the waste heat of generation is sent into heating system.Reactor is about 65% to the COD clearance, BOD
5Clearance is about 70%.
Sequence sequencing batch reactor activated sludge reaction device is made as 2, and total hrt is 7d.Single pond volume is 350m
3, being of a size of 18m * 4 m * 5m, delivery ratio is 1:6, moves 2 cycles every day.Sequence sequencing batch reactor activated sludge reaction device is about 75% to the COD clearance, and ammonia nitrogen removal frank is about 80%.
The bioreactor of dynamic membrane volume is 25m
3, the residence time is 6.0h.Adopt built-in tubular self-generative dynamic membrane component, the effective film area is 140m
2Wherein the monolithic membrane area is 10m
2, water production rate is 0.3m
3/ h.The water outlet head is that sludge concentration is that 3000mg/L, gas-water ratio start reactor during for 15:1 in the 6cm, reaction tank.The initial stage water outlet enters rearmounted intermediate pool, and useful volume is 4m
3, and use sump pump that it is back to membrane cisterna.After 30 minutes, water outlet is limpid, enters the nanofiltration treatment system.Bioreactor of dynamic membrane is 70% to sequence sequencing batch reactor activated sludge reaction device water outlet COD clearance, BOD
5Clearance is 80%.After the steady running 35 days, effluent flux drops to 0.25m
3/ h utilizes clear water and air that membrane module is carried out back flushing, and the back flushing water yield is 2 times of aquifer yield.Subsequently Dynamic Membrane is regenerated, repeat filtration-cleaning-regenerative process.
The bioreactor of dynamic membrane water outlet is further handled discharging through nanofiltration.Adopt 4 antipollution nanofiltration membrane components, water production rate is greater than 3.2m
3/ h.The control of employing constant pressure frequency conversion, pressure-controlling is at 0.35 ~ 0.40Mpa.
Since the system operation 12 months, stable effluent quality meets the standard of " household refuse landfill sites pollution control criterion " (GB 16889-2008) " the existing and special emission limit of newly-built household refuse landfill sites water pollutant of table 3 " defined fully.
Embodiment 3:
Adopt the present invention to handle the percolate in late period, raw water quality is: COD concentration is 1800 ~ 2600mg/L, BOD
5Concentration is 300mg/L ~ 550mg/L, and ammonia nitrogen concentration is 400mg/L ~ 750mg/L, and pH is 7.2 ~ 7.7.It is 50 tons that day is handled the water yield.In this embodiment, the COD mean concns of percolate is about 1900mg/L, BOD
5Mean concns is 420mg/L, and the ammonia nitrogen mean concns is 650mg/L.
As shown in the figure, percolate at first passes through equalizing tank, and the residence time is 15 days.The pump hole is established in the equalizing tank bottom, regularly takes the equalizing tank bottom sludge away.
The effusive sewage of equalizing tank enters coagulation basin, drops into bodied ferric sulfate, and dosage is 30mg/L.Drop into polyacrylamide, dosage is 3mg/L.Adopt mechanical stirring, the reaction times is 10 minutes.The settling tank form is a horizontal sedimentation tank, precipitates that supernatant liquor enters heating system after 2 hours.Handle through this unit coagulating sedimentation, macromole suspended particle, COD and part ammonia nitrogen are effectively removed.
Utilize marsh gas power generation unit waste heat, with percolate temperature increase to 36 ℃ ~ 38 ℃.With pump grain expansion Sludge Bed anaerobic reaction tower is sent in the percolate lifting.
Percolate evenly enters reaction zone by the water distributor of grain expansion Sludge Bed bottom.The height of reaction tower is 7m, and diameter is 3m, and useful volume is 50m
3, the residence time is 24 hours.Upflow velocity is controlled at 5m/h.Per 7 days spoil disposals of reactor once, by the discharging of the mud discharging mouth of bottom.Adopt tubular heater exchhanger to be incubated, be equipped with automatic temp controller.The biogas that produces is sent into the marsh gas power generation unit, and the waste heat of generation is sent into heating system.Reactor is about 65% to the COD clearance, BOD
5Clearance is about 70%.
Sequence sequencing batch reactor activated sludge reaction device is made as 2, and total hrt is 7d.Single pond volume is 180m
3, being of a size of 9 m * 4 m * 5m, delivery ratio is 1:8, moves 2 cycles every day, and wherein the reaction times is 4h, and sedimentation time is 1h, and straining the water time is 1h.Sequence sequencing batch reactor activated sludge reaction device is about 75% to the COD clearance, and ammonia nitrogen removal frank is about 80%.
The bioreactor of dynamic membrane volume is 15m
3, the residence time is 7.2h.Adopt built-in tubular self-generative dynamic membrane component, the effective film area is 70m
2Wherein the monolithic membrane area is 10m
2, water production rate is 0.3m
3/ h.The water outlet head is that sludge concentration is that 3000mg/L, gas-water ratio start reactor during for 15:1 in the 6cm, reaction tank.The initial stage water outlet enters rearmounted intermediate pool, and useful volume is 2m
3, and use sump pump that it is back to membrane cisterna.After 30 minutes, water outlet is limpid, enters the nanofiltration treatment system.Bioreactor of dynamic membrane is 70% to sequence sequencing batch reactor activated sludge reaction device water outlet COD clearance, BOD
5Clearance is 80%.After the steady running 35 days, effluent flux drops to 0.25m
3/ h utilizes clear water and air that membrane module is carried out back flushing, and the back flushing water yield is 2 times of aquifer yield.Subsequently Dynamic Membrane is regenerated, repeat filtration-cleaning-regenerative process.
The bioreactor of dynamic membrane water outlet is further handled discharging through nanofiltration.Adopt 3 antipollution nanofiltration membrane components, water production rate is greater than 3.2m
3/ h.The control of employing constant pressure frequency conversion, pressure-controlling is at 0.35 ~ 0.40Mpa.
Since the system operation 8 months, stable effluent quality meets the standard of " household refuse landfill sites pollution control criterion " (GB 16889-2008) " the existing and special emission limit of newly-built household refuse landfill sites water pollutant of table 3 " defined fully.
The invention provides a kind of thinking and method for the treatment of refuse percolate; the method and the approach of this technical scheme of specific implementation are a lot; the above only is a preferred implementation of the present invention; should be understood that; for those skilled in the art, under the prerequisite that does not break away from the principle of the invention, can also make some improvements and modifications; these improvements and modifications also should be considered as protection scope of the present invention, and all available prior art of each integral part not clear and definite in the present embodiment is realized.
Claims (8)
1. the method for a treating refuse percolate is characterized in that, may further comprise the steps:
(1) percolate is entered the homogenizing water quality of carrying out in the equalizing tank 9 ~ 15 days;
(2) percolate after will handling enters coagulation reaction tank, drops into coagulating agent and coagulant aids and percolate then and carries out precipitating after 8 ~ 15 minutes the reaction, sedimentation time 〉=2 hour;
(3) percolate with post precipitation enters heating system, and percolate is heated to 36 ~ 38 ℃;
(4) percolate after will heating pumps into the expanded granular sludge bed anaerobic reaction that carries out, and the biogas that reaction produces is delivered to generating set, and electric energy is used for power devices, and waste heat is delivered to heating system; Percolate is reaction times 6 ~ 12h in expanded granular sludge bed, and expanded granular sludge bed temperature-stable is at 35 ~ 37 ℃, and the pH value stabilization of percolate is 7.0 ~ 8.0; Expanded granular sludge bed volumetric loading is 12 ~ 17kgCOD/ (m
3D), expanded granular sludge bed interior percolate upflow velocity is 4 ~ 6m/h;
(5) reacted percolate is entered sequence sequencing batch reactor activated sludge reaction device and carry out aerobic reaction, sequence sequencing batch reactor activated sludge reaction device volumetric loading is 0.1 ~ 0.18kgBOD/ (kgMLSSd), and percolate is 7 ~ 15 days residence time in reactor; Percolate is entered in the dynamic film bio reaction tank then;
(6) be provided with bioreactor of dynamic membrane in the dynamic film bio reaction tank, percolate filters by bioreactor of dynamic membrane, at first carries out 30 minutes preliminary filtration, makes the active sludge flco form stable Dynamic Membrane on bioreactor of dynamic membrane; Preliminary filtering percolate returns and drains into the dynamic film bio reaction tank, after Dynamic Membrane forms percolate is filtered, and the organic pollutant removal rate in the percolate is 70% ~ 80%; Behind the dynamic film bio reaction tank intermediate pool is set, holds back the water outlet of initial operating stage after first operation and the back flushing, the filtered liquid in the intermediate pool is by being pumped back to the dynamic film bio reaction tank; The bioreactor of dynamic membrane bottom is provided with aeration, and gas-water ratio is 15:1; When the Dynamic Membrane water outlet water yield less than designed water 75% the time, utilize clear water and air that membrane module is carried out back flushing, the back flushing water yield is 2 times of aquifer yield; Filtered liquid enters nanofiltration system;
(7) percolate filters by the nanofiltration membrane of nanofiltration system, and filtered liquid enters concentration basin;
(8) filtered liquid enters concentration basin and precipitates, and supernatant liquor returns and drains into equalizing tank, and sedimentary sewage sludge waste slag enters pressure filter;
(9) sewage sludge waste slag carries out press filtration after entering pressure filter, and pressing filtering liquid returns and drains into equalizing tank, and the compression mud after the press filtration is discharged, and is transported to landfill yard and carries out landfill.
2. the method for a kind for the treatment of refuse percolate according to claim 1 is characterized in that, the described coagulating agent of step 2 is ferric sulfate, bodied ferric sulfate, poly aluminium chloride iron or polymerize aluminum chloride.
3. the method for a kind for the treatment of refuse percolate according to claim 1 is characterized in that, the described coagulant aids of step 2 is polyacrylamide, Poly Dimethyl Diallyl Ammonium Chloride or sodium polyacrylate.
4. the method for a kind for the treatment of refuse percolate according to claim 1 is characterized in that, the described heating system of step 3 adopts the tubular heat exchange heating, and thermal source is a steam.
5. the method for a kind for the treatment of refuse percolate according to claim 1 is characterized in that, the aperture of the described Dynamic Membrane of step 6 is 0.5 ~ 2.0 μ m, and the fenestra road is crooked duct; Go out stream under gravity condition, the water outlet pressure head is 3cm ~ 15cmH
2O, membrane flux are 30L/m
2H.
6. the method for a kind for the treatment of refuse percolate according to claim 1, it is characterized in that, sludge loading is 0.2 ~ 0.5kgBOD/ (kgMLSSd) in the described dynamic film bio reaction tank of step 6, sludge concentration is 4.0g/L ~ 10.0g/L in the reaction tank, and volumetric loading is controlled at 0.5 ~ 2.0 kgCOD/ (m
3D).
7. the method for a kind for the treatment of refuse percolate according to claim 1 is characterized in that, the described intermediate pool volume of step 6 is 30 minutes a bioreactor of dynamic membrane aquifer yield.
8. the method for a kind for the treatment of refuse percolate according to claim 1 is characterized in that, the described nanofiltration membrane of step 7 is the nanofiltration film.
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|---|---|---|---|
| CN2010106001353A CN102134141A (en) | 2010-12-22 | 2010-12-22 | Method for treating garbage leachate |
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|---|---|---|---|
| CN2010106001353A CN102134141A (en) | 2010-12-22 | 2010-12-22 | Method for treating garbage leachate |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491598A (en) * | 2011-12-16 | 2012-06-13 | 东莞理文造纸厂有限公司 | Sewage disposal system |
| CN103011488A (en) * | 2011-09-22 | 2013-04-03 | 北京朗新明环保科技有限公司 | Domestic waste leachate treatment method |
| CN105712593A (en) * | 2016-05-06 | 2016-06-29 | 武汉市润之达石化设备有限公司 | Sewage treatment system |
| CN105859042A (en) * | 2016-05-18 | 2016-08-17 | 哈尔滨工业大学深圳研究生院 | Sewage treatment method and system |
| CN106277587A (en) * | 2016-08-24 | 2017-01-04 | 江苏众胜灭菌设备科技有限公司 | The backwash filter method that a kind of effluent cycle processes |
| CN108585378A (en) * | 2018-05-24 | 2018-09-28 | 河北南风环保科技有限公司 | A kind of High-concentration organic wastewater treatment method |
| CN109052811A (en) * | 2018-08-02 | 2018-12-21 | 苏州无为环境科技有限公司 | A kind of leachate in garbage transfer station processing method |
| CN111592198A (en) * | 2020-06-11 | 2020-08-28 | 安徽蓝鼎环保能源科技有限公司 | Biochemical treatment method and device for landfill leachate |
| CN114988570A (en) * | 2022-06-24 | 2022-09-02 | 广州市山水生态环保建设有限公司 | Intelligent anaerobic reaction system for rural domestic sewage treatment |
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2010
- 2010-12-22 CN CN2010106001353A patent/CN102134141A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103011488A (en) * | 2011-09-22 | 2013-04-03 | 北京朗新明环保科技有限公司 | Domestic waste leachate treatment method |
| CN102491598A (en) * | 2011-12-16 | 2012-06-13 | 东莞理文造纸厂有限公司 | Sewage disposal system |
| CN105712593A (en) * | 2016-05-06 | 2016-06-29 | 武汉市润之达石化设备有限公司 | Sewage treatment system |
| CN105859042A (en) * | 2016-05-18 | 2016-08-17 | 哈尔滨工业大学深圳研究生院 | Sewage treatment method and system |
| CN106277587A (en) * | 2016-08-24 | 2017-01-04 | 江苏众胜灭菌设备科技有限公司 | The backwash filter method that a kind of effluent cycle processes |
| CN108585378A (en) * | 2018-05-24 | 2018-09-28 | 河北南风环保科技有限公司 | A kind of High-concentration organic wastewater treatment method |
| CN109052811A (en) * | 2018-08-02 | 2018-12-21 | 苏州无为环境科技有限公司 | A kind of leachate in garbage transfer station processing method |
| CN111592198A (en) * | 2020-06-11 | 2020-08-28 | 安徽蓝鼎环保能源科技有限公司 | Biochemical treatment method and device for landfill leachate |
| CN114988570A (en) * | 2022-06-24 | 2022-09-02 | 广州市山水生态环保建设有限公司 | Intelligent anaerobic reaction system for rural domestic sewage treatment |
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