CN101891336A - System and method for leachate treatment in sanitary landfill - Google Patents
System and method for leachate treatment in sanitary landfill Download PDFInfo
- Publication number
- CN101891336A CN101891336A CN 201010218510 CN201010218510A CN101891336A CN 101891336 A CN101891336 A CN 101891336A CN 201010218510 CN201010218510 CN 201010218510 CN 201010218510 A CN201010218510 A CN 201010218510A CN 101891336 A CN101891336 A CN 101891336A
- Authority
- CN
- China
- Prior art keywords
- treatment
- handled
- nanofiltration
- water outlet
- percolate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Abstract
The invention belongs to the field of recycling economy and water treatment and discloses a system and a method for leachate treatment in a sanitary landfill. The system is formed by sequentially connecting a regulating tank, an upflow anaerobic reaction tank, an anaerobic and aerobic biochemical reaction tank, a secondary sedimentation tank, a coagulation sedimentation tank, an immersion-type ultra-filtration system, a nano-filtration system and an advanced oxidation system. The system is capable of carrying out the overall treatment on waste leachate, achieving the advanced treatment of the waste leachate in the sanitary landfill in a way that the physical treatment, chemical treatment and biological treatment are integrated based on the principle that the contaminants having different particle sizes and properties in the waste leachate are classified and achieving the classification of nearly 90 organic contaminants in the waste leachate, thus the treated effluent can fully meet the requirement for the effluent concentration limit of water pollution according to 'the standard for pollution control on the landfill site of municipal solid waste' (GB16889-2008), the system can operate stably for a long time, and the treatment cost is lower than that according to the secondary disc tube reverse osmosis (DT-RO) process.
Description
Technical field
The present invention relates to the processing of percolate, belong to the circulating water treatment field, particularly relate to a kind of treatment system and method for garbage sanitary filling field percolate.
Background technology
The treatment process that can reach the present percolate emission standard of China is also few, mainly contains following several:
(1) deammoniation tower-UASB-SBR-micro-filtration/ultrafiltration-RO reverse osmosis membrane;
(2) UASB-A/O MBR-NF nanofiltration;
(3) micro-filtration-secondary disc tube reverse osmosis (dt-ro) film (DT-RO);
In the above-mentioned technology (1), adopting the physical chemistry method removal of ammonia and nitrogen can bring a series of problem with deammoniation tower, mainly is to exist deammoniation tower to cause problems such as the secondary pollution of ammonia nitrogen, absorption liquid can't be handled, ammonia nitrogen burning power consumption height; There is the halfway problem of removing in intermittent activated sludge process (SBR) technology for the ammonia nitrogen of removing in the percolate; RO reverse osmosis membrane technology then causes containing in the concentrated solution of percolate the salt of higher concentration, if concentrated solution is carried out evaporative crystallization to be handled, then need to expend a large amount of energy consumptions, if the landfill district with concentrated solution recharges landfill yard then can cause the accumulation of salinity, percolate circulates through on-site after a while, its water outlet worsens, the influent quality of biochemical system is worsened, and the operating pressure of reverse osmosis raises, can't steady running.
In the technology (2), though the ammonia nitrogen in the water can effectively be removed by the nitration denitrification process, but because the organism anti-nitration reaction speed in the percolate is less, cause denitrification to carry out slowly, denitrification is incomplete, if do not add the denitrifying carbon source that is easy to biological utilisation, total nitrogen concentration can't reach emission standard.And topmost problem is the macromole organic pollutant in the percolate (wherein being to be difficult to biodegradable organic pollutant greatly) not to be removed in the MBR system, but in the MBR system, accumulate, cause the larger molecular organics concentration in the system to raise gradually, have influence on the normal steady running of biochemical system.In addition, the small organic molecule of bio-refractory (as the small molecules humic acids) can pass through ultra-filtration membrane fully, and these organism are to cause the dirty major cause of blocking up and moving of nanofiltration membrane system.Though the nanofiltration membrane system can the exclusive segment salinity, because its dirty stifled situation is also more outstanding, clean difficulty, make membrane lifetime shorter, can't steady running, bring big difficulty for the promotion and application of this technology.
In the technology (3), DTRO is the advanced treatment technology that is derived from Germany, in Germany extremely successful application precedent has been arranged.Yet the fact shows, the technology of Germany also is not suitable for the percolate from garbage filling field that China handles without any classification, especially be not suitable for the percolate of metropolitan high concentration COD and ammonia nitrogen feature, such as: the DTRO treatment process that Beijing refuse landfill is used in earlier stage, just can't continue operation in 3 months as a result, have to adopt MBR biochemical process and NF membrane process to handle at last.In addition, the concentrated solution after German DTRO handles all is the way that adopts evaporating, concentrating and crystallizing, makes the thorough detachment system of pollutent and salt, and domestic existing concentrated solution treatment process is to adopt to recharge the landfill district, and ammonia nitrogen and salt all do not have to remove.Ammonia nitrogen has the obvious suppression effect to anaerobion, and salt more can cause the percolate salinity accumulation in the landfill yard, therefore, it is the process that artificially landfill percolate water quality is worsened that the dense water of reverse osmosis recharges, and finally react on expensive treatment system, cause the reverse osmotic pressure after for some time sharply to increase, effluent quality worsens.
Therefore, how the garbage sanitary filling field percolate without refuse classification is handled, making processing back water outlet reach the requirement that among " refuse landfill pollutent control criterion " GB16889-2008 the water pollutant emission concentration is limited, is a urgent problem.
Summary of the invention
Based on above-mentioned existing in prior technology problem, the embodiment of the invention provides a kind of treatment system and method for garbage sanitary filling field percolate, realize that biochemical treatment combines with membrane filtration technique, the percolate that can form the rubbish of non-classified is effectively handled, and makes processing back water outlet reach emission standard.
The objective of the invention is to be achieved through the following technical solutions:
The embodiment of the invention provides a kind of treatment system of garbage sanitary filling field percolate, and this system comprises:
Equalizing tank, flow lifting type anaerobic reation pool, anoxic and aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system and nanofiltration system;
Described equalizing tank is connected with nanofiltration system with aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system successively with flow lifting type anaerobic reation pool, anoxic, and the water outlet of described nanofiltration system is as water port; Wherein, be provided with submersible agitator in the described equalizing tank; Be provided with whipping appts, aerating apparatus and reflux pump in described anoxic and the aerobic biochemical reaction tank; Be provided with coagulating agent and coagulant aids input port in the described coagulative precipitation tank; Be provided with the ultrasonic wave utility appliance in the described advanced oxidation system.
The embodiment of the invention also provides a kind of treatment process of garbage sanitary filling field percolate, and this method comprises:
Regulate and handle: institute is handled the garbage sanitary filling field percolate mix, make the Pollutant levels in the percolate after mixing even, the water outlet after adjusting is handled is carried out anaerobic biochemical reaction and is handled;
Anaerobic biochemical reaction is handled: carry out anaerobic biochemical reaction and handle regulating water outlet after handling, part macromolecule organic in the water is decomposed into the organism of lower molecular weight, anoxic and aerobic biochemical processing are carried out in the water outlet after anaerobic biochemical reaction is handled;
Anoxic and aerobic biochemical are handled: anoxic, aerobic and biochemical treatment are carried out in the water outlet after anaerobic biochemical reaction is handled successively, remove the ammonia nitrogen in high density in the percolate, at a certain temperature, cultivation by the nitration denitrification bacterium, guarantee parameters such as the residence time and reflux ratio, remove the ammonia nitrogen in the water, the water outlet after anoxic and the aerobic biochemical processing is carried out carrying out the coagulating sedimentation processing after the secondary sedimentation;
Coagulating sedimentation is handled: carry out coagulating treatment to above-mentioned earlier through the water outlet after the secondary sedimentation, in the coagulating treatment process, the pH value of regulating treating water is 5.2～5.5, dosing coagulant and coagulant aids, precipitate after the coagulating treatment, remove most of humic acids in the percolate, the water outlet after coagulating sedimentation is handled is carried out ultra-filtration filters and is handled;
Ultra-filtration filters is handled: to the water outlet after coagulating sedimentation is handled by hollow-fibre membrane or board-like film in the submerged ultrafiltration filtering system, carry out carrying out pre-treatment before ultra-filtration filters is handled entering nanofiltration system, not removed macromole organic pollutant in the water is isolated from system, be enriched in the ultra-filtration membrane membrane cisterna, prevent its enrichment in biochemical system, ultra-filtration filters is handled the back water outlet carry out the nanofiltration filtration treatment;
Nanofiltration filtration treatment: the water outlet after the nanofiltration filtration treatment is entered nanofiltration system carry out the nanofiltration filtration treatment, by the nanofiltration filtration not removed residue humic acids and partial organic substances in the water are separated removal, concentrated solution after nanofiltration is filtered effluxes to be handled, and the water outlet after nanofiltration is filtered is directly discharged reuse as water up to standard.
The technical scheme that provides by the invention described above embodiment as can be seen, pass through in the embodiment of the invention equalizing tank, the flow lifting type anaerobic reation pool, anoxic and aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system and nanofiltration system connect and compose treatment system successively, can physics, the mode that chemistry and bioremediation organically combine is handled the garbage sanitary filling field percolate, realized at the organism of handling each stage different molecular structures and molecular weight, the colloidalmaterial of different-grain diameter and particulate matter, realize pointed processing, effectively improved the garbage sanitary filling field percolate, particularly to treatment effect, make water outlet reach among " refuse landfill pollutent control criterion " GB16889-2008 requirement to the restriction of water pollutant emission concentration without the sanitary filling field percolate of refuse classification.Particularly in the middle of Biochemistry Reaction System and immersion ultrafiltration system, increased coagulative precipitation tank, with at specific coagulating sedimentation medicament of humic acids, larger molecular organics and colloidal in the percolate and addition method, compared with prior art, solved many difficult problems and disadvantage in the conventional garbage percolate treating process, can make system be able to the operation of stability and high efficiency ground.
Description of drawings
The treatment system each several part connection diagram that Fig. 1 provides for the embodiment of the invention 1;
The process flow figure that Fig. 2 provides for the embodiment of the invention 2;
Each label is respectively among Fig. 1: 1, equalizing tank; 2, flow lifting type anaerobic reation pool (UASB); 3, anoxic and aerobic biochemical reaction tank; 4, second pond; 5, coagulative precipitation tank; 6, immersion ultrafiltration system; 7, nanofiltration system; 8, advanced oxidation system.
Embodiment
The invention will be further described below in conjunction with the drawings and specific embodiments.
Embodiment 1
Present embodiment 1 provides a kind of treatment system of garbage sanitary filling field percolate, and as shown in Figure 1, this system comprises:
Equalizing tank, flow lifting type anaerobic reation pool, anoxic and aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system and nanofiltration system;
Described equalizing tank is connected with nanofiltration system with aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system successively with flow lifting type anaerobic reation pool, anoxic, and the water outlet of described nanofiltration system is as water port; Wherein, be provided with submersible agitator in the described equalizing tank; Be provided with whipping appts, aerating apparatus and reflux pump in described anoxic and the aerobic biochemical reaction tank; Be provided with coagulating agent and coagulant aids input port in the described coagulative precipitation tank; Be provided with the ultrasonic wave utility appliance in the described advanced oxidation system.
The treatment system of above-mentioned garbage sanitary filling field percolate, compared with prior art in the middle of Biochemistry Reaction System and immersion ultrafiltration system, increased the coagulating sedimentation pool process and at percolate in humic acids, larger molecular organics and specific coagulating sedimentation medicament of colloidal and addition method.This technology has solved many difficult problems and the disadvantage in the garbage leachate treatment process, thereby makes system be able to the operation of stability and high efficiency ground.
In the said system advanced oxidation system can also be set, this advanced oxidation system is connected between the concentrated solution outlet and anoxic and aerobic biochemical reaction tank of described nanofiltration system by the road, the concentrated solution outlet that makes nanofiltration system by the road with described advanced oxidation system tieback to anoxic and aerobic biochemical reaction tank.This advanced oxidation treatment unit is provided with the dosing mouth that is used to add the Fenton oxidising agent, and described dosing mouth and advanced oxidation treatment unit internal communication are provided with the ultrasonic wave supplementary unit in the described advanced oxidation treatment unit.
Immersion ultrafiltration system in the said system is formed by connecting by membrane cisterna, polysulfone hollow fiber ultrafiltration membrane system, aerating system, suction pump, chemical cleaning system, instrument and valve line; Be provided with the required perforated pipe of aeration, ultra-filtration membrane film silk, rising pipe successively by putting in order from top to bottom in the described membrane cisterna.Wherein, hollow-fibre membrane can adopt the hollow-fibre membrane that the PVDF material is made.The immersion ultrafiltration system also can adopt existing immersion ultrafiltration system.
Nanofiltration system in the said system is formed by connecting by intake pump, high-pressure pump, recycle pump, film framework, nanofiltration membrane component, backwashing pump, medicine system, chemical cleaning system, instrument and valve line; Described nanofiltration membrane component is arranged in the film framework, comprises rolling nanofiltration membrane and pressure-bearing putamina.Nanofiltration system also can adopt existing nanofiltration system.
Anoxic is separated setting with the aerobic biochemical reaction tank with the immersion ultrafiltration system in the said system, and between is connected with coagulative precipitation tank by second pond, water outlet after making anoxic and aerobic biochemical reaction tank handle is carried out the coagulating sedimentation processing through second pond secondary sedimentation and coagulative precipitation tank, by in coagulating sedimentation is handled, adding coagulating agent the hardly degraded organic substance humic acids is effectively removed, water outlet after coagulating sedimentation is handled enters again to be carried out ultra-filtration filters and handles in the immersion ultrafiltration system, also reduced the pressure of ultrafiltration system.
The treatment system of present embodiment, by equalizing tank, the flow lifting type anaerobic reation pool, anoxic and aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system and nanofiltration system organically combine, can realize anoxic, aerobic, biochemical treatment, coagulating sedimentation is handled, four treating processess such as ultra-filtration filters processing and nanofiltration processing organically combine to be handled the garbage sanitary filling field percolate, formation is with physics, the rational Application of chemistry and bioremediation has reached leachate in refuse landfill site has been carried out the requirement that advanced treatment can reach discharging standards.Utilize the treatment system of present embodiment can realize the classification of nearly 90 kinds of organic pollutants in the percolate is handled, thereby the water outlet strictness after guaranteeing to handle reaches the water disposal of pollutants concentration limit requirement among " household refuse landfill sites pollution control criterion " GB16889-2008, and system's long-time running is stable, processing cost is lower than secondary disc tube reverse osmosis (dt-ro) membrane process.
The embodiment of the invention provides a kind of treatment process of garbage sanitary filling field percolate, and the treatment system that can utilize the foregoing description 1 to provide is handled the garbage sanitary filling field percolate, and as shown in Figure 2, this method comprises:
Regulate and handle: institute is handled the garbage sanitary filling field percolate mix, make the Pollutant levels in the percolate after mixing even, the water outlet after adjusting is handled is carried out anaerobic biochemical reaction and is handled;
Anaerobic biochemical reaction is handled: carry out anaerobic biochemical reaction and handle regulating water outlet after handling, part macromolecule organic in the water is decomposed into the organism of lower molecular weight, anoxic and aerobic biochemical processing are carried out in the water outlet after anaerobic biochemical reaction is handled;
Anoxic and aerobic biochemical are handled: anoxic, aerobic and biochemical treatment are carried out in the water outlet after anaerobic biochemical reaction is handled successively, remove the ammonia nitrogen in high density in the percolate, specifically be to be controlled at more than 20 ℃ the water temperature, making the anaerobic pond residence time is 48～60 hours, the Aerobic Pond residence time is 84～96 hours, reflux ratio is 300～500%, substantially remove ammonia nitrogen in the water by the cultivation of nitration denitrification bacterium, the water outlet after anoxic and aerobic biochemical are handled is carried out carrying out coagulating sedimentation after the secondary sedimentation and is handled;
Coagulating sedimentation is handled: carry out coagulating treatment to above-mentioned earlier through the water outlet after the secondary sedimentation, in the coagulating treatment process, the pH value of regulating treating water is 5.2～5.5, dosing coagulant and coagulant aids, precipitate after the coagulating treatment, remove most of humic acids in the percolate, the water outlet after coagulating sedimentation is handled is carried out ultra-filtration filters and is handled;
The coagulating agent that above-mentioned coagulating sedimentation adds in handling can adopt polymerize aluminum chloride and calcium chloride powder, wherein, the dosage of polymerize aluminum chloride is for adding 100～300mg in corresponding every liter of percolate, the dosage of calcium chloride powder is for being that 75: 1 ratio adds in the mass ratio of polymerize aluminum chloride and calcium chloride powder, order of adding is for adding earlier polymerize aluminum chloride in percolate, after add the calcium chloride powder, sedimentation time is 15 minutes; The coagulant aids that adds during coagulating is handled is a polyacrylamide.
Ultra-filtration filters is handled: to the water outlet after coagulating sedimentation is handled by hollow-fibre membrane or board-like film in the submerged ultrafiltration filtering system, carry out carrying out pre-treatment before ultra-filtration filters is handled entering nanofiltration system, not removed macromole organic pollutant in the water is isolated from system, be enriched in the ultra-filtration membrane membrane cisterna, prevent its enrichment in biochemical system, ultra-filtration filters is handled the back water outlet carry out the nanofiltration filtration treatment;
Nanofiltration filtration treatment: the water outlet after the nanofiltration filtration treatment is entered nanofiltration system carry out the nanofiltration filtration treatment, by the nanofiltration filtration not removed residue humic acids and partial organic substances in the water are separated removal, concentrated solution after nanofiltration is filtered effluxes to be handled, and the water outlet after nanofiltration is filtered is directly discharged reuse as water up to standard.
Above-mentioned treatment process also comprises the advanced oxidation processing: the concentrated solution that effluxes after the nanofiltration filtration treatment is carried out advanced oxidation by Fenton reagent and ultrasonic synergistic handle, organism in the concentrated solution is decomposed into the small organic molecule that is easy to carry out a biological disposal upon, improve concentrated solution water quality, and the concentrated solution after advanced oxidation is handled is back to anoxic and carries out anoxic and aerobic biochemical processing with the aerobic biochemical pond, provide available organic carbon source to denitrification process simultaneously, it is low that the mode of this supplementary carbon source is compared artificial supplementation carbon source cost.
The reaction times of the Fenton reagent during above-mentioned advanced oxidation is handled is 30 minutes, pH value in reaction is 4.0, adding ferrous sulfate and hydrogen peroxide during processing in reactor, be 40～80mg/L in the dosage of Fe2+ ferrous sulfate, and the dosage of hydrogen peroxide is 200～400mg/L; The operating frequency of ultrasonic wave utility appliance is 0.5MHz, and sound density is 0.1W/ml.
Above-mentioned treatment process organically combines anoxic and aerobic biochemical processing, coagulating sedimentation processing, ultra-filtration filters processing and nanofiltration filtration treatment, realized the garbage sanitary filling field percolate being handled in the mode that physics, chemistry and bioremediation organically combine, at the organism of handling each stage different molecular structures and molecular weight, the colloidalmaterial of different-grain diameter and particulate matter, adopt pointed treatment technology, realized effective processing, made water outlet after the processing can reach the requirement of discharging standards the percolate of moiety complexity.
Below in conjunction with the treatment system that provides among the embodiment shown in Figure 11, the treating processes of garbage sanitary filling field percolate is described utilizing above-mentioned treatment process.
This treatment system is to consumer waste landfill percolate (being generally the landfill time less than 8 years) when handling, the percolate water inlet at first enters the equalizing tank of treatment system, by the diving mixer that is provided with in the equalizing tank, the water quality of percolate is mixed, the instantaneous concentration that prevents hazardous contaminant is too high, causes the influence to biochemical system; Former water lifting enters flow lifting type anaerobic reation pool (UASB) through the percolate after the equalizing tank adjusting, carry out anaerobic biochemical reaction, the anaerobic reaction of flow lifting type anaerobic reation pool (UASB) is owing to be subjected to the influence of ammonia nitrogen concentration, it is removed efficient and can not determine, but anaerobic sludge is to the degraded of organic pollutant in the percolate, can improve the water quality of percolate, a part of macromolecule organic is decomposed into the organism of lower molecular weight, the organism that a part of aerobic biochemical reaction is difficult to degrade is converted into the organism that is easy to the aerobic biochemical reaction, thereby helps the carrying out of follow-up aerobic biochemical reaction; The water outlet of flow lifting type anaerobic reation pool (UASB) enters anoxic and aerobic biochemical reaction tank (A/O biochemistry pool), anoxic and aerobic biochemical reaction tank (A/O biochemistry pool) are the preposition reactive system of denitrification, finish removal by nitrated, denitrifying process to ammonia nitrogen in high density in the percolate and organic pollutant, anoxic pond is provided with mixing agitator in (A pond), to realize uniform anaerobic environment, the nitrogen that can help simultaneously to produce in the denitrification process spreads, and promotes the carrying out of anti-nitration reaction; Aerobic Pond is provided with micro-hole aerator in (O pond), by gas blower aeration in the pond, for aerobic microbiological provides dissolved oxygen, is back to anoxic pond (A pond) through the mud mixture after the nitration reaction by sludge reflux pump simultaneously, realizes denitrification process; The water outlet of anoxic and aerobic biochemical reaction tank (A/O biochemistry pool) enters second pond, realize that in second pond mud-water separation, mud are back to anoxic pond (A pond), and comparatively clarifying water outlet enters coagulative precipitation tank; Before entering coagulative precipitation tank, add certain density hydrochloric acid by line mixer, regulate water pH value to 5.2～5.5 (being generally about 5.3), add two kinds of coagulating agent (polymerize aluminum chloride (PAC) and calcium chloride (CaCl then
2), both mass ratioes are 75: 1) and a kind of with fixed attention medicament that helps, add polymerize aluminum chloride (PAC) earlier, after add calcium chloride (CaCl
2), mass ratio is 75: 1, after the quick stirring of 10min, add coagulant aids cationic polyacrylamide (PAM), enter the settling tank precipitation after stirring 30min, water outlet directly enters the immersion ultrafiltration system, the water inlet of immersion ultrafiltration system is that coagulating sedimentation is handled pH value the water outlet 5.2～5.5 between of back without neutralizing treatment, acid water quality helps avoid the inorganics fouling of nanofiltration membrane system, therefore still need not to regulate pH, the immersion ultrafiltration system adopts the hollow-fibre membrane of PVDF material that filtration treatment is carried out in the water outlet of coagulative precipitation tank, adopt suction pump suction water outlet, stifled for fear of the dirt of film, in the hollow fiber film assembly bottom boring aeration device is set, drive water body and the disturbance of film silk by air bubble, stifled with the dirt that slows down film; The water outlet of immersion ultrafiltration system enters into nanofiltration system, nanofiltration system adopts uses comparatively sophisticated rolled membrane module and corollary apparatus, can realize preferably the filtration of residual organic substances in the water body is removed, finally realize the complete qualified discharge of water outlet (effluxing again after can neutralizing to the nanofiltration water outlet).
The concentrated solution that nanofiltration system is discharged enters the advanced oxidation system, carrying out advanced oxidation in the advanced oxidation treatment system handles, specifically be in the advanced oxidation treatment system, to add Fenton Fenton reagent (Fenton reagent) and auxiliary 0.5MHz ultrasonic wave, free radical by the generation of Fenton reagent with strong oxidation capacity, larger molecular organics is decomposed into medium molecule organism and small organic molecule, and effluent recycling is to the anoxic pond (A pond) of anoxic and aerobic biochemical reaction tank (A/O biochemistry pool).
In addition, because the running cost of advanced oxidation system is higher, therefore present application at home is very limited, usually also can adopt the mode that concentrated solution is recharged directly concentrated solution to be recharged landfill district, and carry out being back to after advanced oxidation is handled the anoxic pond (A pond) of anoxic and aerobic biochemical reaction tank (A/O biochemistry pool) without the advanced oxidation system to landfill yard.
In the above-mentioned treatment process, it is the novel method of comprehensive treating process percolate that biochemical process is combined with membrane technique, and it mainly is based on the principle that the composition of percolate is classified and disposed.Progressively cultivation and domestication by microorganism, biodegradable organic and ammonia nitrogen treatment stage of making through anaerobic and aerobic are effectively removed, the non-biodegradable macromolecular substance of remainder then effectively filters by membrane technique, thereby guaranteeing that water outlet can be stablized reaches emission standard.And in the middle of Biochemistry Reaction System and immersion ultrafiltration system, increased the coagulating sedimentation pool process, compared with prior art, solved many difficult problems and disadvantage in the conventional garbage percolate treating process, thereby made system be able to the operation of stability and high efficiency ground.
In the aforesaid method, the technology of biochemical process and MBR+NF (RO) combination comprehensive treating process percolate is effective combination of low-cost and high stability, but can strengthen the pretreating effect of biochemical stage by adopting means such as anaerobic-aerobic combination, can reach the pollutant load that alleviates film and increase means such as coagulating sedimentation, advanced oxidation, and solve and followingly eliminate dense water and recharge the problems brought etc.
In sum, the treatment system of the embodiment of the invention and treatment process can effectively be removed the high-enriched organics in the biochemical refuse landfill percolate, the organism, the ammonia nitrogen in high density that comprise difficult for biological degradation, make water outlet can reach the requirement of the water pollutant emission concentration restriction among " refuse landfill pollutent control criterion " GB16889-2008 steadily in the long term, it also has following advantage:
(1) physics, chemistry and bioremediation are organically combined, at the organism of handling each stage different molecular structures and molecular weight, the colloidalmaterial of different-grain diameter and particulate matter, adopt pointed treatment technology, and every kind of treatment technology all is comparatively advanced treatment process, and the effective combination between them is based on the moiety of percolate complexity furtherd investigate and draws.
(2) in coagulative precipitation tank, regulate pH value to 5.2～about 5.5 innovatively earlier, after added the polymerize aluminum chloride (PAC) and the calcium chloride powder of certain proportioning, coagulation effect to humic acids is good, slowed down the stifled situation of dirt of nanofiltration membrane system widely, made the long-term stability operation of film system become possibility.
(3) adopt A/O biochemistry pool technology, the ammonia nitrogen in high density in the percolate realized removing fully, be lower than the percolate of 1500mg/L for influent ammonium concentration, if temperature guarantee, can make the water outlet of A/O biochemistry pool can reach standard-required.
(4) kept the higher ammonia nitrogen removal ability of A/O biochemistry pool, adopt coagulation-settlement process and immersion ultrafiltration system simultaneously, the organism (as protein, superpolymer etc.) that has so just solved macromolecule in the existing A/OMBR system is in the continuous cumulative drawback of biochemistry pool, original A/O MBR system is because the interception of ultra-filtration membrane, the larger molecular organics that makes biology be difficult to degrade rests on internal system all the time, caused the microorganism disadvantageous effect, simultaneously operation and detection have also been disturbed.
(5) combination of Fenton reagent and ultrasonic wave utility appliance, the organism of the difficult for biological degradation in the concentrated solution can be carried out chemical oxidation treatment, with the partial organic substances complete oxidation is water and carbonic acid gas, and perhaps the oxidation operation with intermediate molecular weight is the less organism of molecular weight.In this course, because the concentration of concentrated solution is higher, if can't reach the requirement of emission standard after handling, can be to the A pond of A/O biochemistry pool with the effluent recycling behind the advanced oxidation, these small organic molecules can be used as the organic carbon source of anti-nitration reaction, participate in anti-nitration reaction, thereby it is finally effectively removed.
The above; only for the preferable embodiment of the present invention, but protection scope of the present invention is not limited thereto, and anyly is familiar with those skilled in the art in the technical scope that the present invention discloses; the variation that can expect easily or replacement all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claims.
Claims (10)
1. the treatment system of a garbage sanitary filling field percolate is characterized in that, this system comprises:
Equalizing tank, flow lifting type anaerobic reation pool, anoxic and aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system and nanofiltration system;
Described equalizing tank is connected with nanofiltration system with aerobic biochemical reaction tank, second pond, coagulative precipitation tank, immersion ultrafiltration system successively with flow lifting type anaerobic reation pool, anoxic, and the water outlet of described nanofiltration system is as water port; Wherein, be provided with submersible agitator in the described equalizing tank; Be provided with whipping appts, aerating apparatus and reflux pump in described anoxic and the aerobic biochemical reaction tank; Be provided with coagulating agent and coagulant aids input port in the described coagulative precipitation tank; Be provided with the ultrasonic wave utility appliance in the described advanced oxidation system.
2. the treatment system of garbage sanitary filling field percolate according to claim 1, it is characterized in that, described system also comprises: the advanced oxidation system, the concentrated solution outlet of described nanofiltration system by the road with described advanced oxidation system tieback to described anoxic and aerobic biochemical reaction tank.
3. the treatment system of garbage sanitary filling field percolate according to claim 2, it is characterized in that, described advanced oxidation treatment unit is provided with the dosing mouth that is used to add the Fenton oxidising agent, described dosing mouth and advanced oxidation treatment unit internal communication are provided with the ultrasonic wave supplementary unit in the described advanced oxidation treatment unit.
4. the treatment system of garbage sanitary filling field percolate according to claim 1, it is characterized in that described immersion ultrafiltration system is formed by connecting by membrane cisterna, polysulfone hollow fiber ultrafiltration membrane system, aerating system, suction pump, chemical cleaning system, instrument and valve line; Be provided with the required perforated pipe of aeration, ultra-filtration membrane film silk and rising pipe successively by putting in order from top to bottom in the described membrane cisterna.
5. the treatment system of garbage sanitary filling field percolate according to claim 4 is characterized in that, the hollow-fibre membrane of the hollow-fibre membrane of described polysulfone hollow fiber ultrafiltration membrane system for adopting the PVDF material to make.
6. the treatment system of garbage sanitary filling field percolate according to claim 1, it is characterized in that described nanofiltration system is formed by connecting by intake pump, high-pressure pump, recycle pump, film framework, nanofiltration membrane component, backwashing pump, medicine system, chemical cleaning system, instrument and valve line; Described nanofiltration membrane component is arranged in the film framework, comprises rolling nanofiltration membrane and pressure-bearing putamina.
7. the treatment process of a garbage sanitary filling field percolate is characterized in that, this method comprises:
Regulate and handle: institute is handled the garbage sanitary filling field percolate mix, make the Pollutant levels in the percolate after mixing even, the water outlet after adjusting is handled is carried out anaerobic biochemical reaction and is handled;
Anaerobic biochemical reaction is handled: carry out anaerobic biochemical reaction and handle regulating water outlet after handling, part macromolecule organic in the water is decomposed into the organism of lower molecular weight, anoxic and aerobic biochemical processing are carried out in the water outlet after anaerobic biochemical reaction is handled;
Anoxic and aerobic biochemical are handled: anoxic, aerobic and biochemical treatment are carried out in the water outlet after anaerobic biochemical reaction is handled successively, remove the ammonia nitrogen in high density in the percolate, make water temperature remain on 20 ℃ during processing, making the anaerobic pond residence time is 48～60 hours, the Aerobic Pond residence time is 84～96 hours, reflux ratio is 300～500%, and the water outlet after anoxic and the aerobic biochemical processing is carried out carrying out the coagulating sedimentation processing after the secondary sedimentation;
Coagulating sedimentation is handled: carry out coagulating treatment to above-mentioned earlier through the water outlet after the secondary sedimentation, in the coagulating treatment process, the pH value of regulating treating water is 5.2～5.5, dosing coagulant and coagulant aids, precipitate after the coagulating treatment, remove most of humic acids in the percolate, the water outlet after coagulating sedimentation is handled is carried out ultra-filtration filters and is handled;
Ultra-filtration filters is handled: to the water outlet after coagulating sedimentation is handled by hollow-fibre membrane or board-like film in the submerged ultrafiltration filtering system, carry out carrying out pre-treatment before ultra-filtration filters is handled entering nanofiltration system, not removed macromole organic pollutant in the water is isolated from system, be enriched in the ultra-filtration membrane membrane cisterna, prevent its enrichment in biochemical system, ultra-filtration filters is handled the back water outlet carry out the nanofiltration filtration treatment;
Nanofiltration filtration treatment: the water outlet after the nanofiltration filtration treatment is entered nanofiltration system carry out the nanofiltration filtration treatment, by the nanofiltration filtration not removed residue humic acids and partial organic substances in the water are separated removal, concentrated solution after nanofiltration is filtered effluxes to be handled, and the water outlet after nanofiltration is filtered is directly discharged reuse as water up to standard.
8. the treatment process of garbage sanitary filling field percolate according to claim 7 is characterized in that, described method also comprises:
Advanced oxidation is handled: the concentrated solution that effluxes after the nanofiltration filtration treatment is carried out advanced oxidation by Fenton reagent and ultrasonic synergistic handle, organism in the concentrated solution is decomposed into the small organic molecule that is easy to carry out a biological disposal upon, improve concentrated solution water quality, and the concentrated solution after advanced oxidation is handled is back to anoxic and carries out anoxic with the aerobic biochemical pond and handle with aerobic biochemical, with additional as the denitrifying carbon source of ammonia nitrogen in anoxic and the aerobic biochemical processing.
9. the treatment process of garbage sanitary filling field percolate according to claim 8 is characterized in that,
The reaction times of the Fenton reagent during described advanced oxidation is handled is 30 minutes, and pH value in reaction is 4.0, adds ferrous sulfate and hydrogen peroxide during processing in reactor, with Fe
2+The dosage of meter ferrous sulfate is 40～80mg/L, and the dosage of hydrogen peroxide is 200～400mg/L; The operating frequency of ultrasonic wave utility appliance is 0.5MHz, and sound density is 0.1W/ml.
10. the treatment process of garbage sanitary filling field percolate according to claim 7, it is characterized in that, the coagulating agent that described coagulating sedimentation adds in handling is polymerize aluminum chloride and calcium chloride powder, wherein, the dosage of polymerize aluminum chloride is for adding 100～300mg in corresponding every liter of percolate, the dosage of calcium chloride powder is for being that 75: 1 ratio adds in the mass ratio of polymerize aluminum chloride and calcium chloride powder, order of adding is for adding earlier polymerize aluminum chloride in percolate, after add the calcium chloride powder, sedimentation time is 15 minutes;
The coagulant aids that adds during described coagulating is handled is a polyacrylamide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102185108A CN101891336B (en) | 2010-06-25 | 2010-06-25 | System and method for leachate treatment in sanitary landfill |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102185108A CN101891336B (en) | 2010-06-25 | 2010-06-25 | System and method for leachate treatment in sanitary landfill |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101891336A true CN101891336A (en) | 2010-11-24 |
| CN101891336B CN101891336B (en) | 2012-07-04 |
Family
ID=43100716
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102185108A Expired - Fee Related CN101891336B (en) | 2010-06-25 | 2010-06-25 | System and method for leachate treatment in sanitary landfill |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101891336B (en) |
Cited By (34)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102139990A (en) * | 2011-01-21 | 2011-08-03 | 樊利华 | Ultrasonic combined waste water treatment process and system of refuse leachate |
| CN102503046A (en) * | 2011-11-18 | 2012-06-20 | 北京伊普国际水务有限公司 | Advanced treatment system and method for high-concentration percolate in comprehensive garbage disposal plant |
| CN102786182A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Device for processing landfill leachat |
| CN102786183A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Method for processing garbage leachate |
| CN102921385A (en) * | 2012-11-29 | 2013-02-13 | 四川师范大学 | Process for preparing modified humic acid fluorine-removal adsorption material |
| CN103130378A (en) * | 2011-11-24 | 2013-06-05 | 马志文 | System for treating household garbage leachate |
| CN103663849A (en) * | 2012-09-13 | 2014-03-26 | 天津森诺过滤技术有限公司 | Method for treating papermaking wastewater based on combined process including integrated membrane technology and advanced oxidation technology |
| CN103663860A (en) * | 2013-10-30 | 2014-03-26 | 郭强 | Treatment method of high-concentration wastewater |
| CN103992001A (en) * | 2014-03-13 | 2014-08-20 | 浙江海洋学院 | Method for treating garbage seepage fluid |
| CN105693029A (en) * | 2016-03-21 | 2016-06-22 | 珠海市海宜环境投资有限公司 | Landfill leachate treatment process |
| CN106242163A (en) * | 2016-08-18 | 2016-12-21 | 江苏环保产业技术研究院股份公司 | A kind of processing method of percolate embrane method concentrated solution |
| CN106365378A (en) * | 2016-08-30 | 2017-02-01 | 芜湖华海生物工程有限公司 | Allantoin wastewater treatment process |
| CN106517618A (en) * | 2016-12-28 | 2017-03-22 | 厦门绿动力环境治理工程有限公司 | Integrated garbage-percolator water purifying unit |
| CN107029697A (en) * | 2017-05-26 | 2017-08-11 | 河海大学 | A kind of method of supersonic synergic zinc oxide/graphene photocatalysis combined pretreatment mature landfill leachate |
| CN107055963A (en) * | 2017-04-26 | 2017-08-18 | 湖南净源环境工程有限公司 | The efficient advanced treatment apparatus of percolate and processing method |
| CN107445403A (en) * | 2017-09-01 | 2017-12-08 | 光大环保技术研究院（南京）有限公司 | A kind of method for cooperateing with processing landfill percolate and burning electricity generation factory percolate |
| CN107827290A (en) * | 2017-12-26 | 2018-03-23 | 浙江巨星生物材料有限公司 | A kind of acid Industrial sewage treatment system |
| CN108147605A (en) * | 2018-01-16 | 2018-06-12 | 厦门嘉戎技术股份有限公司 | A kind of leachate processing method and system for high salinity biodegradability difference |
| CN108996848A (en) * | 2018-09-06 | 2018-12-14 | 杨镒玮 | A kind of sewage-treatment plant and method |
| CN109020097A (en) * | 2018-09-29 | 2018-12-18 | 北京环境工程技术有限公司 | A kind of garbage leachate full dose processing equipment and method |
| CN109081522A (en) * | 2018-09-21 | 2018-12-25 | 南宁市桂润环境工程有限公司 | A kind of processing unit and method of aged refuse in MSW landfill percolate |
| CN109607942A (en) * | 2018-12-14 | 2019-04-12 | 杭州市环境集团有限公司 | The processing system and technique of a kind of flying dust and consumer waste infiltration liquid combined sewage |
| CN109761441A (en) * | 2019-01-23 | 2019-05-17 | 广州故乡源水处理有限公司 | A kind of processing method and processing device of landfill leachate |
| CN110563265A (en) * | 2019-09-10 | 2019-12-13 | 贵州欧瑞欣合环保股份有限公司 | Landfill leachate treatment process |
| CN110902962A (en) * | 2019-12-10 | 2020-03-24 | 东莞市贝辉装饰材料有限公司 | Wastewater system for treating melamine adhesive film paper |
| CN111675433A (en) * | 2020-06-16 | 2020-09-18 | 兰州大学 | Ecological strengthening treatment method for landfill leachate in northwest loess area |
| CN111943436A (en) * | 2020-08-12 | 2020-11-17 | 湖南现代环境科技股份有限公司 | Landfill leachate treatment system and landfill leachate treatment process |
| CN112266128A (en) * | 2020-09-23 | 2021-01-26 | 佛山市绿能环保有限公司 | Leachate treatment process and system for sanitary landfill |
| CN112520950A (en) * | 2020-12-17 | 2021-03-19 | 扬州力齐机械有限公司 | Domestic garbage leachate treatment process |
| CN112794583A (en) * | 2021-01-30 | 2021-05-14 | 浙江自贸区一谦环保技术工作室 | Method for treating landfill leachate by using rhodobacter |
| CN112811750A (en) * | 2021-03-29 | 2021-05-18 | 北京首创环境科技有限公司 | Full-quantitative treatment system and treatment method for leachate of domestic garbage landfill |
| CN113173643A (en) * | 2021-04-22 | 2021-07-27 | 浙江工业大学 | Method for efficiently and stably degrading DBP in landfill leachate based on A/A/O system |
| CN114084999A (en) * | 2021-11-12 | 2022-02-25 | 老河口瑞祥化工有限公司 | Fenton process landfill leachate treatment method |
| CN114315028A (en) * | 2021-12-29 | 2022-04-12 | 中铁二局集团有限公司 | Landfill leachate treatment process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1669958A (en) * | 2005-01-14 | 2005-09-21 | 清华大学 | Infiltration liquid treatment method in domestic refuse burying field |
| CN101148307A (en) * | 2007-08-28 | 2008-03-26 | 北京盖雅环境科技有限公司 | Anaerobic-aerobic-film processing technique for urban domestic refuse percolate |
| CN101357812A (en) * | 2007-07-31 | 2009-02-04 | 深圳百斯特环保工程有限公司 | Processing method for domestic garbage leachate |
| CN101357813A (en) * | 2007-07-31 | 2009-02-04 | 深圳百斯特环保工程有限公司 | Processing method for domestic garbage leachate |
| CN201785287U (en) * | 2010-06-25 | 2011-04-06 | 北京伊普国际水务有限公司 | System for treating leachate of refuse sanitary landfill site |
-
2010
- 2010-06-25 CN CN2010102185108A patent/CN101891336B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1669958A (en) * | 2005-01-14 | 2005-09-21 | 清华大学 | Infiltration liquid treatment method in domestic refuse burying field |
| CN101357812A (en) * | 2007-07-31 | 2009-02-04 | 深圳百斯特环保工程有限公司 | Processing method for domestic garbage leachate |
| CN101357813A (en) * | 2007-07-31 | 2009-02-04 | 深圳百斯特环保工程有限公司 | Processing method for domestic garbage leachate |
| CN101148307A (en) * | 2007-08-28 | 2008-03-26 | 北京盖雅环境科技有限公司 | Anaerobic-aerobic-film processing technique for urban domestic refuse percolate |
| CN201785287U (en) * | 2010-06-25 | 2011-04-06 | 北京伊普国际水务有限公司 | System for treating leachate of refuse sanitary landfill site |
Cited By (43)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102139990B (en) * | 2011-01-21 | 2012-10-17 | 樊利华 | Ultrasonic combined waste water treatment process and system of refuse leachate |
| CN102139990A (en) * | 2011-01-21 | 2011-08-03 | 樊利华 | Ultrasonic combined waste water treatment process and system of refuse leachate |
| CN102503046A (en) * | 2011-11-18 | 2012-06-20 | 北京伊普国际水务有限公司 | Advanced treatment system and method for high-concentration percolate in comprehensive garbage disposal plant |
| CN102503046B (en) * | 2011-11-18 | 2013-08-14 | 北京伊普国际水务有限公司 | Advanced treatment system and method for high-concentration percolate in comprehensive garbage disposal plant |
| CN103130378A (en) * | 2011-11-24 | 2013-06-05 | 马志文 | System for treating household garbage leachate |
| CN103130378B (en) * | 2011-11-24 | 2014-03-26 | 马志文 | System for treating household garbage leachate |
| CN102786182A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Device for processing landfill leachat |
| CN102786183A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Method for processing garbage leachate |
| CN103663849A (en) * | 2012-09-13 | 2014-03-26 | 天津森诺过滤技术有限公司 | Method for treating papermaking wastewater based on combined process including integrated membrane technology and advanced oxidation technology |
| CN102921385A (en) * | 2012-11-29 | 2013-02-13 | 四川师范大学 | Process for preparing modified humic acid fluorine-removal adsorption material |
| CN102921385B (en) * | 2012-11-29 | 2014-03-12 | 四川师范大学 | Process for preparing modified humic acid fluorine-removal adsorption material |
| CN103663860A (en) * | 2013-10-30 | 2014-03-26 | 郭强 | Treatment method of high-concentration wastewater |
| CN103663860B (en) * | 2013-10-30 | 2015-04-08 | 郭强 | Treatment method of high-concentration wastewater |
| CN103992001A (en) * | 2014-03-13 | 2014-08-20 | 浙江海洋学院 | Method for treating garbage seepage fluid |
| CN103992001B (en) * | 2014-03-13 | 2015-08-19 | 浙江海洋学院 | A kind for the treatment of process of refuse leachate |
| CN105693029A (en) * | 2016-03-21 | 2016-06-22 | 珠海市海宜环境投资有限公司 | Landfill leachate treatment process |
| CN106242163A (en) * | 2016-08-18 | 2016-12-21 | 江苏环保产业技术研究院股份公司 | A kind of processing method of percolate embrane method concentrated solution |
| CN106365378A (en) * | 2016-08-30 | 2017-02-01 | 芜湖华海生物工程有限公司 | Allantoin wastewater treatment process |
| CN106517618A (en) * | 2016-12-28 | 2017-03-22 | 厦门绿动力环境治理工程有限公司 | Integrated garbage-percolator water purifying unit |
| CN106517618B (en) * | 2016-12-28 | 2023-06-09 | 厦门绿动力环境治理工程有限公司 | Integrated garbage percolator water purifying unit |
| CN107055963A (en) * | 2017-04-26 | 2017-08-18 | 湖南净源环境工程有限公司 | The efficient advanced treatment apparatus of percolate and processing method |
| CN107029697A (en) * | 2017-05-26 | 2017-08-11 | 河海大学 | A kind of method of supersonic synergic zinc oxide/graphene photocatalysis combined pretreatment mature landfill leachate |
| CN107445403A (en) * | 2017-09-01 | 2017-12-08 | 光大环保技术研究院（南京）有限公司 | A kind of method for cooperateing with processing landfill percolate and burning electricity generation factory percolate |
| CN107827290A (en) * | 2017-12-26 | 2018-03-23 | 浙江巨星生物材料有限公司 | A kind of acid Industrial sewage treatment system |
| CN108147605A (en) * | 2018-01-16 | 2018-06-12 | 厦门嘉戎技术股份有限公司 | A kind of leachate processing method and system for high salinity biodegradability difference |
| CN108147605B (en) * | 2018-01-16 | 2023-07-11 | 厦门嘉戎技术股份有限公司 | Percolate treatment method and system for high salinity and poor biodegradability |
| CN108996848A (en) * | 2018-09-06 | 2018-12-14 | 杨镒玮 | A kind of sewage-treatment plant and method |
| CN109081522A (en) * | 2018-09-21 | 2018-12-25 | 南宁市桂润环境工程有限公司 | A kind of processing unit and method of aged refuse in MSW landfill percolate |
| CN109081522B (en) * | 2018-09-21 | 2023-09-19 | 桂润环境科技股份有限公司 | Treatment device and method for landfill leachate of household garbage landfill |
| CN109020097A (en) * | 2018-09-29 | 2018-12-18 | 北京环境工程技术有限公司 | A kind of garbage leachate full dose processing equipment and method |
| CN109607942A (en) * | 2018-12-14 | 2019-04-12 | 杭州市环境集团有限公司 | The processing system and technique of a kind of flying dust and consumer waste infiltration liquid combined sewage |
| CN109761441A (en) * | 2019-01-23 | 2019-05-17 | 广州故乡源水处理有限公司 | A kind of processing method and processing device of landfill leachate |
| CN110563265A (en) * | 2019-09-10 | 2019-12-13 | 贵州欧瑞欣合环保股份有限公司 | Landfill leachate treatment process |
| CN110902962A (en) * | 2019-12-10 | 2020-03-24 | 东莞市贝辉装饰材料有限公司 | Wastewater system for treating melamine adhesive film paper |
| CN111675433A (en) * | 2020-06-16 | 2020-09-18 | 兰州大学 | Ecological strengthening treatment method for landfill leachate in northwest loess area |
| CN111943436A (en) * | 2020-08-12 | 2020-11-17 | 湖南现代环境科技股份有限公司 | Landfill leachate treatment system and landfill leachate treatment process |
| CN112266128A (en) * | 2020-09-23 | 2021-01-26 | 佛山市绿能环保有限公司 | Leachate treatment process and system for sanitary landfill |
| CN112520950A (en) * | 2020-12-17 | 2021-03-19 | 扬州力齐机械有限公司 | Domestic garbage leachate treatment process |
| CN112794583A (en) * | 2021-01-30 | 2021-05-14 | 浙江自贸区一谦环保技术工作室 | Method for treating landfill leachate by using rhodobacter |
| CN112811750A (en) * | 2021-03-29 | 2021-05-18 | 北京首创环境科技有限公司 | Full-quantitative treatment system and treatment method for leachate of domestic garbage landfill |
| CN113173643A (en) * | 2021-04-22 | 2021-07-27 | 浙江工业大学 | Method for efficiently and stably degrading DBP in landfill leachate based on A/A/O system |
| CN114084999A (en) * | 2021-11-12 | 2022-02-25 | 老河口瑞祥化工有限公司 | Fenton process landfill leachate treatment method |
| CN114315028A (en) * | 2021-12-29 | 2022-04-12 | 中铁二局集团有限公司 | Landfill leachate treatment process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101891336B (en) | 2012-07-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101891336B (en) | System and method for leachate treatment in sanitary landfill | |
| CN102503046B (en) | Advanced treatment system and method for high-concentration percolate in comprehensive garbage disposal plant | |
| US8894855B2 (en) | Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods | |
| CN202322568U (en) | Deep treatment system of high-concentration percolate of integrated garbage treatment site | |
| CN109592785A (en) | Anaerobism membrane reactor-partial nitrification-Anammox combination unit and method | |
| CN206767868U (en) | A kind of garbage percolation liquid treating system | |
| CN101219842A (en) | Technique and equipment for recycling leachate of garbage | |
| WO2001064590A1 (en) | Method and system for sustainable treatment of municipal and industrial wastewater | |
| EP2603464A1 (en) | Treatment of municipal wastewater with anaerobic digestion | |
| CN101148302A (en) | Method for treating waste water of livestock and fowl cultivation | |
| CN206476860U (en) | A kind of oily waste water treatment reclamation set | |
| CN105776766A (en) | Advanced treatment system for biorefractory wastewater of industrial park | |
| CN101269903B (en) | Further advanced treatment technique and apparatus for sewage water of oil refining | |
| CN102603128A (en) | Method for advanced treatment and recycling of landfill leachate | |
| CN105481174A (en) | Wastewater treatment system in rubber and synthetic plastic industry | |
| CN105645662B (en) | The removing means and removal methods of hardly degraded organic substance in film-filter concentration liquid | |
| CN104649519A (en) | Sewage treatment device and method by combining bio-ferric process and anaerobic MBR method | |
| CN1970474A (en) | Garbage leachate processing process and system based on membrane bioreactor-nano filtering membrane technology | |
| CN101781056B (en) | Treatment method of waste papermaking water | |
| CN108623085B (en) | Advanced treatment method for high-nitrogen organic wastewater membrane filtration concentrate | |
| CN201785287U (en) | System for treating leachate of refuse sanitary landfill site | |
| CN208265976U (en) | A kind of landfill leachate concentration liquid zero-discharge treatment system | |
| CN200988816Y (en) | Garbage percolating liquid treating system based on film biological reactor-filter film technology | |
| CN208071544U (en) | A kind of railway communication system production wastewater treatment system | |
| CN201553670U (en) | Equipment for recycling garbage percolate through reverse osmosis desalination multistage pretreatment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120704 Termination date: 20190625 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |