CN101708919A - Method for treating leachate in refuse landfill site - Google Patents
Method for treating leachate in refuse landfill site Download PDFInfo
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Abstract
The invention is applicable to the technical field of wastewater treatment, and provides a method for treating leachate in a refuse landfill site. The method adopts processes of anaerobic treatment, biological aerated treatment, secondary AO treatment, MBR treatment and reverse osmosis treatment, and effluent of the treated leachate wastewater in the refuse landfill site meets the pollution control standard for domestic refuse landfill (GB 16889-2008). The method does not need to adopt blowoff treatment, saves running cost, and adopts a coagulating sedimentation method to treat concentrate after the reverse osmosis treatment so as to avoid accumulation of organic matters and heavy metals in the system.
Description
Technical field
The invention belongs to technical field of waste water processing, relate in particular to a kind of treatment process of leachate in refuse landfill site.
Background technology
The main source of the percolate of sanitary filling field comprises: natural precipitation and runoff in (1) landfill yard; (2) rubbish self is original moisture; (3) water that produces owing to the anaerobic digestion of microorganism.Percolate water quality is very complicated, not only contains the oxygen consumption organic pollutant, also contains each metalloid and nutrient for plants (ammonia nitrogen etc.), also contains poisonous and hazardous pollutent in the industrial refuse percolate; BOD5, COD concentration height are higher than municipal effluent far away; Organic pollutant category is many in the percolate, wherein has to be difficult to non-chlorination fragrance such as biodegradable naphthalene, phenanthrene group compound, chlorination fragrance group compound, phosphoric acid ester, phthalic ester, phenolic compound and amino benzenes compounds etc.Contain more than ten kind of metal ion in the percolate, heavy metal ion wherein can be to the microorganisms restraining effect; The ammonia-nitrogen content height, C/N is out of proportion, and phosphoric lacks, and brings sizable difficulty to subsequent disposal.
In addition on the one hand, country polluted control criterion to refuse landfill and revises the management increasingly stringent of sanitary filling field percolate in 2008 on the basis of GB16889-1997.Secondary, grade III Standard in the primary standard are all cancelled, and all sanitary filling fields are all carried out primary standard; Regulation is from July 1st, 2011, and existing whole household refuse landfill sites are consumer waste infiltration liquid and the emission limit that puts rules into practice by oneself, does not allow to enter sewage work and handles; In primary standard, increase total nitrogen and heavy metal index, made the intractability of percolate strengthen.
Commonly adopt electrolytic process, ammonia blow-off method, chemical method to come the ammonia nitrogen in the rubbish filtrate is handled in the prior art.But common electrolytic process processing efficiency is not high, and the processing of ammonia nitrogen is not reached the pre-treatment requirement; And the method for stripping adopts the blower fan air feed, and steam-water ratio is usually greater than 1000: 1, and needs to regulate about pH to 10.5, and working cost is significantly increased; Adding chemical agent removes in the method for ammonia nitrogen, the medicament that adds is magnesium salts and phosphoric acid salt, generates magnesium ammonium phosphate sediment, and reduces working cost by the recycle chemical agent, but still belong to chemical process on the whole, have the problem that the chemical sludge amount is big, working cost is high.
The method that is usually used at present the ammonia nitrogen processing both at home and abroad also has chlorine break method, ion exchange method etc.Chlorine break method needs a large amount of chlorine and NaOH because of ammonia-nitrogen content is high, and processing cost is higher (30 yuan/m
3), and there is unsafe factor in chlorine at aspects such as storage, transportations; Ion exchange method is only applicable to the advanced treatment of micro-ammonia nitrogen.
With respect to above method, the running cost of biological denitrificaion method is cheap and operational administrative is easy, but traditional biological denitrificaion method is to utilize the nitrification and denitrification principle of microorganism, and carbon-nitrogen ratio reversal of the natural order of things in the percolate, need add a large amount of carbon sources and basicity, will cause cost to rise significantly.In addition for traditional activated sludge process, when ammonia nitrogen concentration during greater than 200mg/L, the activity of nitrobacteria will be suppressed and reduce processing efficiency.Ammonia nitrogen concentration more than 800mg/L, does not adopt suitable processing usually in the percolate, and traditional biochemical treatment is difficult to carry out usually.
And for the processing behind the garbage leachate biological denitrification, usually adopt medicament to carry out, adopt hydrogen peroxide or ozone to be, more because pharmaceutical quantities is very big as oxygenant with the method for oxidation, also there are problems such as chemical mud amount is big, subsequent disposal trouble in this method working cost costliness.
In the various combination procesies that percolate is handled, the technology of " biochemistry+film " is the most common, and is also comparatively successful.This process using membrane bioreactor improves the removal efficient of organism and ammonia nitrogen, and carries out pre-treatment for follow-up reverse osmosis system, but can't handle dense water.In fact, dense water treatment is extremely important in percolate technology.Dense water is that nanofiltration membrane or reverse-osmosis treated unit produce, and accounts for the 15-30% that handles the water yield, and common treatment process is directly to return to drain into landfill yard, utilizes the long-term circulation in the treatment system to reach the purpose of removing pollutent.But this inevitably causes organism and inorganics in intrasystem accumulation, and long-play can influence effluent quality and system stability.In addition, this combination process adopts the denitrogenation of AO technology usually, and the ammonia nitrogen especially removal efficient of total nitrogen is not high, is difficult for reaching the standard-required of new promulgation in 2008.
The another kind of combination process that percolate is handled is " materialization+film " technology, this technology has dual mode, the one, " coagulating sedimentation+multi-stage filter core filtration+reverse osmosis ", be based on physical chemistry method, chemically be the garbage leachate treatment process of assisting, have processing efficiency height, equipment volume is little, treatment scheme is short characteristics; Another is " preaeration+disc tube reverse osmosis (dt-ro) system ", and this mode treatment effect is applicable to the influent quality of household refuse landfill sites different steps and Various Seasonal reliably and with long-term, and effluent quality is good, can reach miscellaneous domestic water quality standard.But this technology is by Physical Separation Technology, and biological treatment does not wait pre-treating technology, can't fundamentally thoroughly decompose all contaminations of removing in the percolate, and its decontamination principle only is the transfer of pollutent phase, and dense water problems is more outstanding.This method is not considered the handling problem of ammonia nitrogen and total nitrogen in addition, is difficult to reach the standard-required of new promulgation in 2008 yet.
Summary of the invention
The object of the present invention is to provide that a kind of working cost is cheap, stable, the leachate in refuse landfill site treatment system of complete process, make effluent quality reach the national standard requirement of promulgation in 2008.
The present invention realizes like this, a kind of treatment process of leachate in refuse landfill site is provided, comprise the step of percolate being carried out biochemical treatment and film processing, wherein said biochemical treatment is to adopt the aeration and biological treatment process that the ammonia nitrogen in the percolate is carried out pre-treatment.
The present invention also provides a kind of treatment process of leachate in refuse landfill site, comprises following steps:
The pre-treatment of S1 anaerobism: collect percolate and in the anaerobic treatment device its be hydrolyzed, fermentation, acidification, with the reduction becoming of the organonitrogen in percolate ammonia nitrogen;
The S2 aeration and biological is handled: carry out the ammonia nitrogen removal pre-treatment in BAF, go total nitrogen pre-treatment and COD to remove processing through the pretreated percolate of anaerobism;
S3 secondary AO processing+MBR handles: ammonia nitrogen and total nitrogen processing are removed in the sewage of percolate after aeration and biological is handled continue to flow through secondary AO system and MBR pond;
The S4 reverse-osmosis treated: effluent stream enters reverse osmosis system after handle in the MBR pond remove the processing of residual organic matter after, draining, blowdown mud.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, the operating load of anaerobic treatment device is 1-5kgCOD/m among the described step S1
3.d, operating temperature 20-35 ℃, pH value＜7.0.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, among the described step S2, contain urethane, haydite or volcanics filtrate in the filler of BAF, the 1-3 days filler residence time.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, described secondary AO system comprises one-level anoxic pond, one-level Aerobic Pond, secondary anoxic pond and secondary aerobic treatment pond.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, the total residence time of sewage is 100-150 hour in the described secondary AO processing+MBR treating processes.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, the reverse osmosis system among the described step S4 comprises security personnel's filter, one section of reverse osmosis, two sections of reverse osmosiss.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, the sewage that enters reverse osmosis system among the described step S4 produces clear water and dense water for one section through security personnel's filter, reverse osmosis, and dense water enters two sections continuation processing of reverse osmosis and produces clear water and dense water; The clear water qualified discharge of one section and two sections generation of reverse osmosis, qualified discharge after the dense water of two sections generations of reverse osmosis enters coagulative precipitation tank to carry out the dosing processing.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, during the dosing of described coagulative precipitation tank is handled, the medicament polymerize aluminum chloride and the polyacrylamide that add.
In the treatment process of above-mentioned leachate in refuse landfill site provided by the invention, the adding consistency of described polymerize aluminum chloride is 500-2000mg/L, and the adding consistency of polyacrylamide is 5-10mg/L.
The treatment process of leachate in refuse landfill site provided by the present invention is that a kind of working cost is cheap, stable, the leachate in refuse landfill site treatment process of complete process, and its effluent quality has reached the national standard requirement of promulgation in 2008.This system has comprised biochemistry+membrane process, and biochemical unit adopts anaerobism+biological aerated filter process+two-stage AO+MBR technology, with the method for coagulating sedimentation dense water is handled simultaneously, has guaranteed that organism and inorganics are not accumulated in system.
Description of drawings
Shown in Figure 1 is the FB(flow block) of one embodiment of the present invention;
Shown in Figure 2 is the schematic flow sheet of one embodiment of the present invention;
Shown in Figure 3 is the formant synoptic diagram of reverse osmosis system in the one embodiment of the invention.
Embodiment
In order to make purpose of the present invention, technical scheme and advantage clearer,, the present invention is further elaborated below in conjunction with drawings and Examples.Should be appreciated that specific embodiment described herein only in order to explanation the present invention, and be not used in qualification the present invention.
As shown in Figure 1, the treatment process of leachate in refuse landfill site provided by the invention is: percolate waste water is removed partial organic substances through anaerobic unit, removes most ammonia-nitrogen, total nitrogen and organism through BAF, secondary AO system and MBR system successively then.The water outlet of MBR system enters reverse osmosis system and handles, and clear water qualified discharge, dense water are got back to landfill yard or equalizing tank after handling through the method for coagulating sedimentation.
The character that is applicable to the percolate of the inventive method is: below the COD 20000mg/L, below the ammonia nitrogen 2000mg/L.Process of the present invention is the method for carrying out a biological disposal upon and membrane filtration combines, active sludge in the biological treatment can be taken from the active sludge in the percolate treatment unit of the same type, also can adopt the residual active sludge of aeration tank, municipal sewage plant or second pond, be used for treating processes of the present invention after the conventional acclimation method of employing is cultivated domestication.Activated sludge concentration is preferably 5-10g/L.
The anaerobic reactor that is used for the present invention can be upflowing activated sludge process (UASB), anaerobic baffle plate (ABR) or multiple-hearth (active sludge and bed of packings) anaerobic reactor.
Be used for BAF of the present invention, adoptable carrier comprises urethane filler, ceramics filling and volcanics biofilter material, but is not limited to these fillers.
Be used for membrane bioreactor of the present invention, the membrane module that adopts has comprised built-in curtain type membrane and external placed type tubular membrane, the type of film is a ultra-filtration membrane, and mould material is olefin polymer such as polyvinyl chloride, polyethylene, polypropylene, poly(vinylidene fluoride) (PVDF) and polysulfones, pottery etc.The film water-out manners adopts the suction function of vacuum pump or the pressurization of topping-up pump to realize.The inventive method can be carried out operate continuously, also can adopt batch operation.
Be used for reverse osmosis units of the present invention, the film of employing is an antipollution type pleurodiaphragmatic in terspace spare, and mould material is composite polyamide material or cellulose acetate membrane.
Be used for coagulating sedimentation device of the present invention, can adopt flat flow, vertical-flow, inclined tube or inclined-plate clarifying basin.
Further specify the process and the effect of the inventive method below in conjunction with accompanying drawing Fig. 2.
The function of equalizing tank 1 is to collect percolate, lift pump 2 is promoted to anaerobic reactor 3 with percolate, the major function of anaerobic reactor is hydrolysis, fermentation, acidification through anaerobion, significantly reduce COD, improve the B/C value of sewage, make wastewater biodegradability be improved significantly, be beneficial to follow-up biochemical treatment, and the organonitrogen in the waste water be reduced to ammonia nitrogen.
Sewage gravity after handling through BAF 4 flow into follow-up secondary AO system (5, the one-level anoxic; 6, one-level is aerobic; 7, the secondary anoxic; 8, secondary is aerobic), in the one-level anoxic pond, denitrifying bacteria utilizes the organism in the sewage to make carbon source, with a large amount of NO that bring in the backflow mixed liquor
3-N and NO
2-N is reduced to N
2Be released into air, so BOD
5Density loss, NO
3-N concentration descends significantly, and the variation of phosphorus is very little.In the one-level Aerobic Pond, organism is degraded by microbial biochemical, and COD, BOD continue to descend; Organonitrogen then by nitrated, is made NH by ammonification
3-N concentration significantly descends, but nitrifying process makes NO
3The concentration of-N raises, and phosphorus concentration is along with the excess ingestion of polyP bacteria also descends with fast speeds.
The major function of secondary anoxic pond is identical with the one-level anoxic pond, i.e. denitrogenation and release phosphorus are based on denitrogenation.The major function of secondary Aerobic Pond for further nitrated, absorb phosphorus and degradation of organic substances.
The main purpose that secondary AO system is set is the removal effect that guarantees ammonia nitrogen and total nitrogen.MBR pond 11 is set after the secondary Aerobic Pond.The MBR technology is the novel wastewater processing technology that membrane separation technique and biotechnology organically combine, it utilizes membrane separation assemblies to hold back active sludge and larger molecular organics in the biochemical reaction tank, replace the second pond in the traditional activated sludge process, thereby significantly improved the ability of system's solid-liquid separation.Activated sludge concentration can significantly improve, and hydraulic detention time (HRT) and sludge retention time (SRT) can be controlled respectively, and constantly reaction and the degraded in reactor of the material of difficult degradation.Therefore, membrane biological reactor process has been strengthened the function of bio-reactor greatly by the isolation technique of film.Membrane module 12 is installed in the MBR pond, is relied on the effect of suction pump 13 that the treating water of biochemical system is delivered to middle pond 17.Reflux pump 10 is set in the MBR pond, and in one-level anoxic pond 5, the effect of backflow has two with mixed-liquor return, and the one, contain the sewage backflow of nitrate and nitrite, purpose is through the anoxic removing total nitrogen; The 2nd, the backflow of mud guarantees that each unit sludge concentration of biochemical system is even.Gas blower 9 is one-level Aerobic Pond 6, secondary Aerobic Pond 8, BAF 4 and 11 oxygen supplys of MBR pond.
Method provided by the invention has shown the good removal ammonia nitrogen and the ability of total nitrogen to percolate.
Because the percolate ammonia-nitrogen content is very high, has suppressed microbic activity in the traditional activated sludge process, thereby has greatly reduced the removal efficient of Sludge System to pollutent.And the BAF technology has solved this difficult problem, and this technology contrasts conventional biotechnology and has the efficient denitrification ability.Its mechanism is:
1. by microbial immobilized, the quantity of nitrifier is higher more than 10 times than conventional mud method, can reach 10-20g/L.Why nitrifier increases significantly is because the carrier specific surface area that adopts in this technology is big, can reach 350000m2/m3, and the specific surface area of general conventional carrier has only several ten thousand m2/m3.
2. with ionic linkage, covalent linkage and hydrogen bonded, bonding force is strong between immobilized microorganism and the carrier, the microorganism difficult drop-off, so microorganism is long generation time, is beneficial to the procreation of nitrifier and nitrococcus.
3. after microbial immobilized, toxin immunity ability and impact resistance strengthen, and this is because the concentration of microorganism has increased on the one hand; In addition on the one hand, microorganism is hit, and the back is difficult to come off from carrier, treats that load restoration also recovers to the normal level microbic activity thereupon.
4. this technology is different with mass transfer mode between suspension activated sludge process phase ratio wastewater and the microorganism.In the suspension activated sludge process microorganism be flow, blended, and microorganism static after immobilization, hive off, microbe species increases greatly, has improved the processing power to the percolate of complicated component.
5. this technology is compared hydraulics with common biomembrance process and mass transfer effect improves greatly.The microbial film of common biomembrance process is very thick, promptly allows to form aerobic, anoxic and anaerobic environment, because water molecules, air molecule are difficult for reaching biomembranous nexine, thereby denitrifying level is not high, and is not good to the removal effect of total nitrogen.And filler porosity height in the present technique, mass transfer condition is good, and nitrification and denitrification can carry out simultaneously, and is good to the removal effect of total nitrogen.According to the chemical equilibrium reaction formula, the reduction significantly of total nitrogen has promoted the treatment effect to ammonia nitrogen.
Two sections AO technologies are adopted in the BAF back, have further guaranteed the clearance of ammonia nitrogen and total nitrogen.
The inventive method is handled dense water, guaranteed that heavy metal and organism do not accumulate in system, and the dense water that nanofiltration membrane and reverse osmosis produce in the ordinary method is directly got back to refuse landfill, increase along with the time, heavy metal and organism can build up in system, not only influence effluent characteristics, also can result in blockage nanofiltration membrane and reverse osmosis membrane.Adopt the method for coagulating sedimentation that dense water is handled among the present invention, remove all very effective organism and heavy metal that can not be biochemical in the percolate.The mechanism that coagulating sedimentation is removed organism and heavy metal no longer is described in detail here.
The inventive method adopts BAF rather than stripping unit to the denitrogenation processing of percolate, has saved working cost.The stripping unit generally adopted steam-water ratio 1000: 1, needed gas blower that the stripping air is provided, and will wastewater pH be adjusted to more than 10.5 with alkali, made that the unitary working cost of stripping is very high.And BAF is the method removal ammonia nitrogen of utilization biological treatment, has saved working cost.
In addition, there is the food chain relation of upstream and downstream in the BAF unit because microbial biomass is big, and the M/F value is lower, and microbe species is various, and therefore the sludge quantity that produces is few.Whole technology reduces 1/4 than prior art sludge quantity.
The advantage of this technology is described below in conjunction with embodiment:
Embodiment 1:
Certain landfill percolate COD 8000-12000mg/L, BOD 2000-3000mg/L, ammonia nitrogen 1600-2400mg/L.Water quality characteristics is the organic concentration height, and wastewater biodegradability is poor, BOD/COD=0.2.
Anaerobic reactor operating load 5kgCOD/m
3.d (d of unit herein represent " my god ", down with), operating temperature is controlled at 20-35 degree centigrade, pH is controlled at below 7.0, COD clearance 30-40%.Anaerobism water outlet COD is 5600-7200mg/L.This unit does not have clearance to ammonia nitrogen.Anaerobism water outlet ammonia nitrogen 1600-2400mg/L, total nitrogen 1600-2400mg/L, total nitrogen mainly exists with the form of ammonia nitrogen in the anaerobism water outlet.
BAF (BAF) plays the pre-treatment effect to ammonia nitrogen in the unit, simultaneously total nitrogen and COD is also had higher removal.BAF unit filling polyurethane-base filler, filler residence time 2d, ammonia nitrogen removal frank reaches 60-70%, water outlet ammonia nitrogen 640-720mg/L, nitrogen removal rate 40-50%, water outlet total nitrogen 640-1200mg/L.COD clearance 30-40%, water outlet COD are 3920-4320mg/L.
Two-stage AO technology+MBR technology, total residence time are 120h.COD clearance 80-85%, water outlet COD are 648-780mg/L.Ammonia nitrogen removal frank 98%, water outlet ammonia nitrogen 12.8-14.4mg/L.Nitrogen removal rate 95%, water outlet total nitrogen 32-60mg/L.
Reverse osmosis units adopts 8040 toray pollution-resistant membranes, and the COD clearance is more than 95%, water outlet COD35-50mg/L.Ammonia nitrogen removal frank is about 50%, more than the nitrogen removal rate 50-70%, and water outlet ammonia nitrogen 6-7mg/L, total nitrogen 9-16mg/L.
Embodiment 2:
Certain landfill percolate COD 2000-4000mg/L, BOD 1000-2000mg/L, ammonia nitrogen 500-800mg/L.Water quality characteristics is for belonging to fresh percolate, and organic concentration is lower, and wastewater biodegradability is better, BOD/COD=0.5.
Anaerobic reactor operating load 1kgCOD/m
3.d (d of unit herein represent " my god ", down with), operating temperature is controlled at 20-35 degree centigrade, pH is controlled at below 7.0, COD clearance 20-30%.Anaerobism water outlet COD is 1600-2800mg/L.This unit does not have clearance to ammonia nitrogen.Anaerobism water outlet ammonia nitrogen 500-800mg/L, total nitrogen 500-800mg/L, total nitrogen mainly exists with the form of ammonia nitrogen in the anaerobism water outlet.
BAF (BAF) unit reaches 40-50% to ammonia nitrogen removal frank, water outlet ammonia nitrogen 300-400mg/L, nitrogen removal rate 30-40%, water outlet total nitrogen 350-480mg/L.COD clearance 25-30%, water outlet COD are 1200-1960mg/L.
Two-stage AO technology+MBR technology, total residence time are 100h.COD clearance 60-70%, water outlet COD are 480-588mg/L.Ammonia nitrogen removal frank 97%, water outlet ammonia nitrogen 9-12mg/L.Nitrogen removal rate 90%, water outlet total nitrogen 35-48mg/L.
Reverse osmosis units adopts 8040 toray pollution-resistant membranes, and the COD clearance is more than 95%, water outlet COD24-29.4mg/L.Ammonia nitrogen removal frank is about 50%, and nitrogen removal rate is more than 50%, water outlet ammonia nitrogen 4-6mg/L, total nitrogen 17-24mg/L.
Embodiment 3:
Certain landfill percolate COD 2000-4000mg/L, BOD 200-400mg/L, ammonia nitrogen 1000-1500mg/L.Water quality characteristics is for belonging to mature landfill leachate, and organic concentration is lower, but ammonia nitrogen is very high, and wastewater biodegradability is poor, BOD/COD=0.1.
Anaerobic reactor operating load 1kgCOD/m
3.d (d of unit herein represent " my god ", down with), operating temperature is controlled at 20-35 degree centigrade, pH is controlled at below 7.0, the COD clearance drops to 10-15%.Anaerobism water outlet COD is 1800-3400mg/L.This unit does not have clearance to ammonia nitrogen.Anaerobism water outlet ammonia nitrogen 1000-1500mg/L, total nitrogen 1000-1500mg/L, total nitrogen mainly exists with the form of ammonia nitrogen in the anaerobism water outlet.
BAF (BAF) unit reaches 60-70% to ammonia nitrogen removal frank, water outlet ammonia nitrogen 400-450mg/L, nitrogen removal rate 40-50%, water outlet total nitrogen 600-750mg/L.COD clearance 25-30%, water outlet COD are 1350-2380mg/L.
Two-stage AO technology+MBR technology, total residence time are 100h.COD clearance 60-70%, water outlet COD are 540-714mg/L.Ammonia nitrogen removal frank 97%, water outlet ammonia nitrogen 12-13.5mg/L.Nitrogen removal rate 90%, water outlet total nitrogen 60-75mg/L.
Reverse osmosis units adopts 8040 toray pollution-resistant membranes, and the COD clearance is more than 95%, water outlet COD27-35.7mg/L.Ammonia nitrogen removal frank is about 50%, and nitrogen removal rate is more than 50%, water outlet ammonia nitrogen 6-7mg/L, total nitrogen 30-37mg/L.
The above only is preferred embodiment of the present invention, not in order to restriction the present invention, all any modifications of being done within the spirit and principles in the present invention, is equal to and replaces and improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. the treatment process of a leachate in refuse landfill site comprises the step of percolate being carried out biochemical treatment and film processing, and wherein said biochemical treatment is to adopt the aeration and biological treatment process that the ammonia nitrogen in the percolate is carried out pre-treatment.
2. the treatment process of a leachate in refuse landfill site is characterized in that, comprises following steps:
The pre-treatment of S1 anaerobism: collect percolate and in the anaerobic treatment device its be hydrolyzed, fermentation, acidification, with the reduction becoming of the organonitrogen in percolate ammonia nitrogen;
The S2 aeration and biological is handled: carry out the ammonia nitrogen removal pre-treatment in BAF, go total nitrogen pre-treatment and COD to remove processing through the pretreated percolate of anaerobism;
S3 secondary AO processing+MBR handles: ammonia nitrogen and total nitrogen processing are removed in the sewage of percolate after aeration and biological is handled continue to flow through secondary AO system and MBR pond;
The S4 reverse-osmosis treated: effluent stream enters reverse osmosis system after handle in the MBR pond remove the processing of residual organic matter after, draining, blowdown mud.
3. the treatment process of leachate in refuse landfill site as claimed in claim 2 is characterized in that, the operating load of anaerobic treatment device is 1-5kgCOD/m among the described step S1
3.d, operating temperature 20-35 ℃, pH value＜7.0.
4. the treatment process of leachate in refuse landfill site as claimed in claim 2 is characterized in that, among the described step S2, contains urethane, haydite or volcanics filtrate in the filler of BAF, the 1-3 days filler residence time.
5. the treatment process of leachate in refuse landfill site as claimed in claim 2 is characterized in that, described secondary AO system comprises one-level anoxic pond, one-level Aerobic Pond, secondary anoxic pond and secondary aerobic treatment pond.
6. the treatment process of leachate in refuse landfill site as claimed in claim 5 is characterized in that, the total residence time of sewage is 100-150 hour in the described secondary AO processing+MBR treating processes.
7. the treatment process of leachate in refuse landfill site as claimed in claim 2 is characterized in that, the reverse osmosis system among the described step S4 comprises security personnel's filter, one section of reverse osmosis, two sections of reverse osmosiss.
8. the treatment process of leachate in refuse landfill site as claimed in claim 7, it is characterized in that, the sewage that enters reverse osmosis system among the described step S4 produces clear water and dense water for one section through security personnel's filter, reverse osmosis, and dense water enters two sections continuation processing of reverse osmosis and produces clear water and dense water; The clear water qualified discharge of one section and two sections generation of reverse osmosis, qualified discharge after the dense water of two sections generations of reverse osmosis enters coagulative precipitation tank to carry out the dosing processing.
9. the treatment process of leachate in refuse landfill site as claimed in claim 8 is characterized in that, during the dosing of described coagulative precipitation tank is handled, and the medicament polymerize aluminum chloride and the polyacrylamide that add.
10. the treatment process of leachate in refuse landfill site as claimed in claim 8 is characterized in that, the adding consistency of described polymerize aluminum chloride is 500-2000mg/L, and the adding consistency of polyacrylamide is 5-10mg/L.
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| CN106396294A (en) * | 2016-12-06 | 2017-02-15 | 大同新成新材料股份有限公司 | Treatment method of lithium battery electrolyte cask washing wastewater |
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| CN110204045A (en) * | 2018-12-31 | 2019-09-06 | 上海康恒环境股份有限公司 | A kind of method of municipal solid waste incinerator percolate treating process drop total nitrogen |
| CN110818179A (en) * | 2019-09-29 | 2020-02-21 | 北京翰祺环境技术有限公司 | Efficient nitrogen and phosphorus removal sewage treatment system and sewage treatment method |
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| CN111847796B (en) * | 2020-07-31 | 2024-04-09 | 中节能工程技术研究院有限公司 | Leachate treatment system and method for garbage incineration plant |
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