CN102786183B - Method for processing garbage leachate - Google Patents

Method for processing garbage leachate Download PDF

Info

Publication number
CN102786183B
CN102786183B CN2012100865958A CN201210086595A CN102786183B CN 102786183 B CN102786183 B CN 102786183B CN 2012100865958 A CN2012100865958 A CN 2012100865958A CN 201210086595 A CN201210086595 A CN 201210086595A CN 102786183 B CN102786183 B CN 102786183B
Authority
CN
China
Prior art keywords
percolate
electrolysis
treatment
membrane
ammonia nitrogen
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.)
Active
Application number
CN2012100865958A
Other languages
Chinese (zh)
Other versions
CN102786183A (en
Inventor
张世文
李丹
殷明彩
秦婧
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Boying Xiamen Science and Technology Co Ltd
Original Assignee
Boying Xiamen Science and Technology Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Boying Xiamen Science and Technology Co Ltd filed Critical Boying Xiamen Science and Technology Co Ltd
Priority to CN2012100865958A priority Critical patent/CN102786183B/en
Publication of CN102786183A publication Critical patent/CN102786183A/en
Application granted granted Critical
Publication of CN102786183B publication Critical patent/CN102786183B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00Multistage treatment of water, waste water, or sewage
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/46Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/46Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4691Capacitive deionisation
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5254Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using magnesium compounds and phosphoric acid for removing ammonia
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56Macromolecular compounds
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/66Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/06Contaminated groundwater or leachate
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic processes
    • C02F3/12Activated sludge processes
    • C02F3/1236Particular type of activated sludge installations
    • C02F3/1268Membrane bioreactor systems
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/30Aerobic and anaerobic processes
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124Water desalination
    • Y02A20/131Reverse-osmosis
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage

Abstract

The invention discloses a method for processing a landfill leachate, which comprises the following steps of ammonia nitrogen removal, flocculent precipitate, electrolysis, capacitance desalination, anaerobic treatment, aerobic treatment, membrane filtration and membrane concentrate treatment. The method for processing the landfill leachate has the advantages that an electrolysis technology, a membrane technology and a bio-chemical technology are combined to form a method for processing the landfill leachate, the method has the characteristics of stable operation, strong adaptive capacity on water quality change, low cost, high treatment efficiency, effective reduction of index of ammonia nitrogen, COD, SS, chromaticity in the landfill leachate and standard discharge of effluent.

Description

The treatment process of percolate
Technical field
The invention belongs to field of environment engineering, it relates to a kind for the treatment of process of sewage, refers to especially that a kind of cost is lower, the effect treatment process of percolate preferably.
Background technology
Percolate is a kind of high density organic garbage filter liquid that is difficult to process, and it is mainly from following three aspects: 1, natural precipitation and the runoff in landfill yard; 2, the water that contains of rubbish self; 3, the water that produces due to the anaerobic digestion of microorganism after garbage loading embeading; Wherein the precipitation in landfill yard is major portion.City garbage percolate pollutant load representative value is as shown in table 1.
The main component (except pH and sense index, unit is mg/L) of the general percolate of table 1
Project The change in concentration scope Project The change in concentration scope
Sense index Black/stench Muriate 189~3262
The pH value 3.7~8.5 Fe 50~600
Total hardness 3000~10000 Cu 0.1~1.43
COD Cr 1200~300000 Ca 200~300
BOD 5 200~60000 Pb 0.1~2.0
NH3-N 20~7400 Cr 0.01~2.61
Total phosphorus 1~70 Hg 0~0.032
As shown in Table 1, the water quality of percolate has following essential characteristic:
(1) Pollutant levels are high, more than COD, BOD and ammonia nitrogen mostly are greatly tens~hundred times of industrial pollutants discharging standards.
(2) existing organic contamination composition, also have inorganic pollutant component, also contains simultaneously some micro heavy pollutant components, and the comprehensive pollution feature is obvious.
(3) organic pollutant category is many, complicated component.In percolate, organic pollutant is many, up to 77 kinds, non-chlorination aromatics, chlorination aromatic series compounds such as being difficult to biodegradable naphthalene, phenanthrene is arranged wherein, phosphoric acid ester, phthalic ester, phenolic compound and amino benzenes compounds etc.
(4) contain 10 many kinds of metal ions in percolate, heavy metal ion wherein can produce the severe inhibition effect to biological treatment process.
(5) in percolate, the microbial nutrition element ratio is seriously lacked of proper care.Ammonia nitrogen concentration wherein is very high, and C/N is out of proportion, and when its nutritive props is processed than biological process, the needed nutritive props of microorganism growth greatly differs from each other, and brings certain difficulty to biological treatment.
The ammonia-nitrogen content of percolate and COD concentration are high, make the surface water body anoxic, water quality deterioration; The nutritive substances such as nitrogen phosphorus are the inducements that causes body eutrophication, also may have a strong impact on drinking water source; Generally speaking, COD, BOD, BOD/COD can increase with landfill yard " age " and reduce, and level of alkalinity raises.In addition, along with the increase of stacking the time limit, new refuse gradually becomes old rubbish, and Organic Pollutants of Landfill Leachate content descends to some extent, but the ammonia-nitrogen content increase, and the biodegradability reduction, so intractability is very large.
The emphasis that percolate is administered is the processing of the processing of COD and ammonia nitrogen, especially ammonia nitrogen.Multiple technology and equipment for percolate is processed has appearred in prior art.For example disclose a kind for the treatment of process that utilizes submerged combustion evaporation technique to come the landfill waste percolate in patent document CN1485280A, this technique is mainly by oxidation operation being become carbonic acid gas and water, and processes penetrating fluid by evaporation and concentrated mode.The technology of utilizing anaerobism molecular breakdown method to come the treating refuse percolate is disclosed in patent document CN1440941, the method comprises predecomposition step, anaerobism step, decomposes oxidation step, adsorption step, step of flocculation precipitation and filtration step, and the method combines the means of physical chemistry processing and two aspects of carrying out a biological disposal upon.Similarly, in patent document CN1478737, disclosed percolate adopts electrolytic oxidation to process with film the scheme that combines, and in this technique, carries out reverse-osmosis treated after the percolate that utilizes ceramic membrane that the process electrolytic oxidation is processed filters again.
In addition, existing known electrolysis tech can effectively be removed the objectionable impurities in percolate, but the current density of traditional electrolysis is low, operating potential is high, electrical efficiency is very low, the power consumption is large, the life-span is short, cost is high, therefore is applied to percolate processing aspect effect unsatisfactory.
Summary of the invention
The object of the invention is to overcome complex treatment process that prior art exists, the chemical consumption amount is large, cost is high, process after the defectives such as the percolate discharging is not up to standard, organically combine by electrolysis process, membrane process and biochemical process, learn from other's strong points to offset one's weaknesses, thereby form a kind of high ammonia nitrogen removal frank, high chroma clearance and high COD clearance, the method for treating garbage percolation liquid that stable, adaptable to change of water quality, expense is lower, processing efficiency is high.
Technical scheme of the present invention comprises the following steps:
A, ammonia nitrogen removal
Percolate enters the equalizing tank regulating water quality through pipeline, the balanced water yield, and add pH adjusting agent by chemicals dosing plant in equalizing tank, flow in ammonia nitrogen blowing-off device or reaction tank after regulating the pH value, making ammonia nitrogen in high density in percolate convert free ammonia to by steam or air stripping in ammonia nitrogen blowing-off device is blown, perhaps adds appropriate Mg(OH by chemicals dosing plant in reaction tank) 2And H 3PO 4, with NH 4+Reaction generates MgNH 4PO 46H 2The O(struvite) precipitation to reach the purpose of removing ammonia nitrogen, enters the subsequent disposal operation after making its ammonia nitrogen concentration≤200mg/L;
B, flocculation sediment
Flow into coagulation basin after the percolate ammonia nitrogen removal, add appropriate flocculation agent by chemicals dosing plant in coagulation basin, enter preliminary sedimentation tank after reacting completely, the throw out of preliminary sedimentation tank (being mud) is sent in sludge sump through pump and pipeline, carry out at last filtering separation in sludge dehydration device, with the COD reduction by 10~35% of percolate;
C, electrolysis
Percolate after flocculation sediment is processed pumps into the electrolysis machine electrolysis, enters intermediate pool after electrolysis, and adds reductive agent, removes the remaining free radical that electrolysis produces; Adjacent two interelectrode voltages of electrolysis machine are 2~12V, and current density is 10~320mA/cm 2
D, capacitive desalination
During the specific conductivity of percolate after through step c electrolysis treatment 〉=5000 μ s/cm, first process through the steps d capacitive desalination, make its specific conductivity be reduced to 500~3000 μ s/cm, then enter step e anaerobic treatment; During the specific conductivity of percolate after through step c electrolysis treatment<5000 μ s/cm, directly enter step e anaerobic treatment;
E, anaerobic treatment
Percolate after electrolysis treatment or capacitive desalination are processed enters in hydrolysis acidification pool and anoxic pond successively, the residence time is 8~72 hours, larger molecular organics in hydrolysis acidification pool in percolate acidication under the effect of acid-producing bacteria becomes small organic molecule, resolve into methane and carbon dioxide under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane in the process anoxic pond again, improve the B/C value, improve biodegradability; Denitrification by denitrifying bacterium in anoxic pond simultaneously further removes the ammonia nitrogen in percolate;
F, aerobic treatment
Percolate after anaerobic treatment enters in the Aerobic Pond of microorganisms such as containing aerobic bacteria, nitrobacteria and nitrite bacteria, the residence time is 16~360 hours, make good use of the organism in the further oxygenolysis percolate of oxygen animalcule, the degree of depth is removed COD and the BOD in percolate, utilizes simultaneously the nitrification of nitrobacteria and the nitrosification of nitrite bacteria to make ammonia-state nitrogen be converted into nitric nitrogen or nitrite nitrogen; In addition, the partially mixed liquid of Aerobic Pond is back to anoxic pond by reflux pump;
G, re-electrolysis
When through the COD of the percolate after aerobic treatment 〉=400mg/L, to carry out re-electrolysis through the percolate after aerobic treatment, make wherein larger molecular organics open loop chain rupture, improve biodegradability, and during electrolysis, adjacent two interelectrode voltages of electrolysis machine are 3~18V, and current density is 20~320mA/cm 2When through the COD of the percolate after aerobic treatment<400mg/L, directly enter step h membrane filtration;
H, membrane filtration
Percolate after aerobic treatment or re-electrolysis are processed flows into second pond, after further COD, the BOD and SS that removes in percolate of precipitation, make water outlet reach the reuse water standard through membrane filtration, the mud part of second pond bottom through pump reflux to anoxic pond, another part flows in sludge sump by pipeline, become filtrate and mud cake through the sludge dehydration device filtering separation again, filtrate flow in equalizing tank through back of pipeline, and mud cake is transported outward;
I, film filtration concentrated processing
After the concentrated solution that step h membrane filtration produces is processed through capacitive desalination, then be circulated to anoxic pond through pump reflux.
In step a, described ammonia nitrogen blowing-off device is a kind of of stripping tower, packing tower or gravity machine; The ammonia that described stripping goes out can be back to soda ash production with absorption by Hydrochloric Acid generation ammonium chloride and make mother liquor, and also used water absorbs and produces ammoniacal liquor or produce the ammonium sulfate byproduct with sulfuric acid absorption;
In step a, described MgNH 4PO 46H 2The O(struvite) throw out after the processes such as granulation, can be developed as composite fertilizer and use.
In step b, described flocculation agent is a kind of or any two the above combination in aluminium salt (Tai-Ace S 150, aluminum chloride), molysite (ferric sulfate, ferrous sulfate, iron(ic) chloride), poly-aluminium (polymerize aluminum chloride, polyaluminium sulfate, polymer aluminium silicate), Polyferric Sulfate (poly-ferric chloride, bodied ferric sulfate, polymeric silicicacid iron), organic polymer coargulator or microbial flocculant; Described pH adjusting agent is a kind of in sulfuric acid, hydrochloric acid, sodium hydroxide, sodium carbonate, sodium bicarbonate, lime.
In step b, optimum flocculent is bodied ferric sulfate (PFS), and its dosage is percolate 200~2000g per ton.
In step b, optimum flocculent is ferrous sulfate (FeSO 4), its dosage is percolate 230~1800g per ton.
In step c, described electrolysis machine is provided with power supply and electrolyzer, and the electrode materials in electrolyzer is a kind of in the alloy of graphite, titanium, iron, aluminium, zinc, copper, lead, nickel, molybdenum, chromium, metal and nano-catalytic noble electrode etc.; The top layer of described nano-catalytic noble electrode is coated with the metal oxide inertia catalyst coatings that crystal grain is 10~35nm; The substrate of described nano-catalytic noble electrode can be titanium plate or plastic plate.
Further, in step c, described best electrolysis is the nano-catalytic electrolysis, the structure of described nano-catalytic electrolysis machine is seen Chinese patent CN102010038A, the operating voltage of electrolysis is 2~500V, and adjacent two interelectrode voltages are 2~8 V, and current density is 10~300mA/cm 2
During nano-catalytic electrolysis percolate, the strong oxidizing property materials such as radical chlorine [Cl], radical oxygen [O] and hydroxyl [OH] that produce are killed organism, the ammonium ion in microorganism in percolate, oxygenolysis percolate, make the large ring open loop of organic substance in percolate, the long-chain chain rupture, both eliminated the colourity of percolate, also removed stink, also improve the biodegradability of percolate, and percolate is taken off surely under electric field action, suspended substance in percolate, colloid, charged corpuscle form larger particles.In addition, the positively charged ion in percolate, negatively charged ion move to negative electrode and anode respectively, in negative electrode and anode generation Effect of Electric Double Layer and the effect of many electricity layers, form precipitation and bring out throwing out, accelerating impurity sedimentation; The hydrogen small bubbles that electrolysis produces also have air flotation effect.
Adopt the nano-catalytic electrolysis to have following outstanding effect:
At first, make macrocylc compound open loop in percolate, long-chain chain rupture by electrolysis, the radical oxygenolysis organism that produces, fast reducing COD has improved the biodegradability of percolate, thereby has created better biochemical condition for follow-up anaerobic unit.
Secondly, kill the microorganism in percolate by the multiple radical (strong oxidizing property material) that electrolysis produces, make in follow-up anaerobic treatment and can cultivate larger dominant microflora, bring into play better biochemical effect, make the effluent quality of anaerobic treatment better.
The 3rd, the Inorganic Ammonium in the oxygenolysis percolate makes ammonium ion be converted into nitrogen, nitrate radical, nitrite anions and water, and the decreasing ratio of ammonia nitrogen can reach 80~90%, makes the ammonia nitrogen that enters biochemical front percolate less than 100mg/L, eliminates simultaneously stink in water.
The 4th, the colourity of decrease percolate, the strong oxidizing property free radicals such as chlorine [Cl], hydroxyl [OH] and oxygen [O] that electrolysis produces can oxygenolysis residue in chromophoric group in percolate, auxochrome group, reduce percolate colourity, reach the purpose of decolouring.
The 5th, deodorizing, the osmophore in multiple radical (strong oxidizing property material) the oxygenolysis percolate that electrolysis produces is removed the stench in percolate.
The 6th, positively charged ion during electrolysis in percolate and negatively charged ion move to negative electrode and the anode of electrolysis machine electrolyzer respectively, Effect of Electric Double Layer occurs, form precipitation near negative electrode and anode, thereby the heavy metal ion content in the reduction percolate, thereby alleviate heavy metal ion to inhibition, the toxic action of anaerobism, aerobic microbiological in follow-up unit.
In step f, the reflux ratio of described mixed solution is 3:1 or 2:1, is conducive to the ammonia nitrogen that the denitrification of denitrifying bacterium in anoxic pond removes percolate.
In step h, described membrane filtration filters for the percolate through the second pond precipitate and separate passes through membrane bioreactor (MBR) again; Described MBR membrane module is selected from a kind of in Pvdf Microporous Hollow Fiber Membrane, polypropylene hollow fiber membrane, ps hollow fiber uf membrane, polyethersulfone, polyacrylonitrile and PVC hollow fiber membrane, membrane pore size is 0.10~0.2 μ m, operating pressure is-1~-50kPa, working temperature is 5~45 ℃.
In step h, after the percolate process immersion ultrafiltration or pillar ultra-filtration filters of described membrane filtration for process second pond precipitate and separate, then filter through nanofiltration; Described ultrafiltration is a kind of of immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000~100000MWCO, working conditions is: normal temperature~45 ℃, the operating pressure of immersion ultrafiltration is-1~-50kPa, the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3~300kPa; The membrane module of described nanofiltration is rolled membrane module, and the mould material of nanofiltration membrane is cellulose acetate film or composite nanometer filtering film in organic membrane, and the molecular weight cut-off of nanofiltration membrane is 200~500MWCO, and entrance pressure is 6.0~45.0bar, and going out to press is 4.5~43.5 bar.
In step h, after the percolate process ultra-filtration filters of described membrane filtration for process second pond precipitate and separate, then pass through reverse osmosis (RO) and filter; The membrane module of described reverse osmosis is rolled membrane module, and mould material is cellulose acetate film or composite membrane in organic membrane, and the molecular weight cut-off of mould material is 50~200MWCO, and entrance pressure can be 6.0~45.0bar, goes out to press to can be 4.5~35 bar.
By the above-mentioned description of this invention as can be known, compared to the prior art, the invention has the advantages that:
(1) pass through electrolysis step, make non-chlorination aromatics, chlorination aromatic series compounds such as being difficult to biodegradable naphthalene, phenanthrene in percolate, phosphoric acid ester, phthalic ester, the open loop such as phenolic compound and amino benzenes compounds, chain rupture, not only can reduce COD, and improved the biodegradability of percolate, can reach 80~90% to the decreasing ratio of the remaining ammonia nitrogen after ammonia nitrogen removal simultaneously, effectively remove heavy metal ion in percolate by the electrolytic flocculation precipitating action simultaneously, for follow-up treatment process is created better biochemical condition.
(2) nano-catalytic electrolysis machine employing surface coverage has and has good catalytic effect crystal grain the noble electrode of the nano-catalytic coating that is 10~35nm to make anode, anode does not consume, cost is low, electrical efficiency is high, be more than 10 times of ordinary electrode electrolytic efficiency, the ton percolate is processed the electric energy that consumes and is significantly reduced.
(3) bioremediation by anaerobic treatment and aerobic treatment can further effectively reduce ammonia nitrogen, COD and the BOD in percolate.
(4) by above steps coordinate in order can guarantee percolate process after indices all reach " household refuse landfill sites pollution control criterion " (GB16889-2008) requirement of emission standard, for the processing of landfill percolate provides reliable assurance.
(5) by with film filtration concentrated pass through again the desalination of electric capacity ionic adsorption after, then pass back into biosystem, thoroughly solve film filtration concentrated emission problem.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
1 the specific embodiment of the present invention is described with reference to the accompanying drawings.
Embodiment 1
The percolate of certain garbage sanitary filling field 1000 ton per day is processed engineering
The water quality situation is as shown in table 2 after measured for the former water of described percolate.
The water quality situation of the former water of table 2 percolate.
Sequence number Project Unit Measured value Sequence number Project Unit Measured value
1 COD Cr mg/L 16800 5 Ammonia nitrogen mg/L 1240
2 SS mg/L 570 6 Colourity Doubly 1200
3 Turbidity NTU 505 7 The pH value - 6.8
4 BOD 5 mg/L 2866 8 Specific conductivity μS/cm 4300
Step a, ammonia nitrogen removal
Percolate enters the equalizing tank regulating water quality through pipeline, and the balanced water yield makes flow and parameter from refuse landfill percolate of different nature everywhere be able to abundant adjusting, is convenient to the processing of follow-up unit.And add sodium hydroxide solution to regulate pH value to 9 ~ 11 by chemicals dosing plant in equalizing tank, then flow in reaction tank, add Mg(OH by chemicals dosing plant in reaction tank) 2And H 3PO 4, make itself and NH 4+Reaction generates MgNH 4PO 46H 2The O(struvite) precipitation to reach the purpose of removing ammonia nitrogen, enters coagulation basin after making its ammonia nitrogen concentration≤200mg/L; The struvite throw out after the processes such as granulation, use as composite fertilizer by exploitation.
Step b, flocculation sediment
Flow into coagulation basin after the percolate ammonia nitrogen removal, percolate per ton enters preliminary sedimentation tank after adding 200g bodied ferric sulfate (PFS) to react completely, the precipitation of preliminary sedimentation tank (being mud) is sent in sludge sump through pump and pipeline, carries out at last filtering separation in sludge dehydration device; Enter electrolysis machine after COD reduction by 10~35% with percolate.
Above-mentioned bodied ferric sulfate is flocculation agent.Flocculation agent can be a kind of or any two the above combination in aluminium salt (Tai-Ace S 150, aluminum chloride), molysite (ferric sulfate, ferrous sulfate, iron(ic) chloride), poly-aluminium (polymerize aluminum chloride, polyaluminium sulfate, polymer aluminium silicate), Polyferric Sulfate (poly-ferric chloride, bodied ferric sulfate, polymeric silicicacid iron), organic polymer coargulator or microbial flocculant.
Step c, electrolysis
Then percolate enters intermediate pool, and adds reductive agent through flowing into the electrolysis machine electrolysis after flocculation sediment, removes the remaining free radical that electrolysis produces.Described electrolysis machine is the nano-catalytic electrolysis machine, and its operating voltage is 40V, and current density is 20mA/cm 2, the voltage of two interpolars is 3.5 V.The free radical chlorine [Cl] of the strong oxidizing property that the little electrolysis of nano-catalytic produces, oxygen [O] and hydroxyl [OH] energy Quick Oxidation decompose the organic substance in percolate, make the large organic molecule open loop, chain rupture, the macromole that are difficult to biochemical degradation in percolate be decomposed into small molecules, that reduces COD and improve percolate can be biochemical, for biochemistry provides better condition; Make simultaneously chromophoric group, the auxochrome group oxidation of the dye molecule in percolate or be reduced to colourless group, reaching the purpose of decolouring; Moreover, positively charged ion in percolate and negatively charged ion move to negative electrode and the anode of electrolysis machine electrolyzer respectively, form precipitation near negative electrode and anode, thereby the heavy metal ion content in the reduction percolate, thereby alleviate heavy metal ion to inhibition, the toxic action of anaerobism, aerobic microbiological in follow-up unit; In addition, can also kill microorganism in percolate, and make suspended substance, colloid, charged corpuscle in percolate form larger particles under electric field action.
Steps d, anaerobic treatment
The specific conductivity of the percolate after electrolysis treatment<5000 μ s/cm, therefore directly enter in hydrolysis acidification pool and anoxic pond, the residence time is 10 hours, larger molecular organics in hydrolysis acidification pool in percolate acidication under the effect of acid-producing bacteria becomes small organic molecule, resolve into methane and carbon dioxide under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane in the process anoxic pond again, improve the B/C value, improve biodegradability; Denitrification by denitrifying bacterium in anoxic pond simultaneously further removes the ammonia nitrogen in percolate.
Step e, aerobic treatment
Percolate after anaerobic treatment enters in the Aerobic Pond of microorganisms such as containing aerobic bacteria, nitrobacteria and nitrite bacteria, the residence time is 18 hours, make good use of the organism in the further oxygenolysis percolate of oxygen animalcule, the degree of depth is removed COD and the BOD in percolate, utilizes simultaneously the nitrification of nitrobacteria and the nitrosification of nitrite bacteria to make ammonia-state nitrogen be converted into nitric nitrogen or nitrite nitrogen; In addition, the mixed solution of Aerobic Pond is back to anoxic pond with the ratio of 2:1 by reflux pump.
Step f, membrane filtration
COD<the 400mg/L of the percolate after aerobic treatment, flow directly into second pond, through COD, BOD in the further removal of precipitation percolate, SS etc., make water outlet reach the reuse water standard through the MBR filtering separation, to anoxic pond, another part flows in sludge sump by pipeline the mud part of second pond bottom, then becomes filtrate and mud cake through the sludge dehydration device filtering separation through pump reflux, filtrate flow in equalizing tank through back of pipeline, and mud cake is transported outward.
Described MBR membrane module is polypropylene hollow fiber membrane, and membrane pore size is 0.10~0.2 μ m, operating pressure is-1~-50kPa, working temperature is 5~45 ℃.
G, film filtration concentrated processing
After in step f, MBR filters the concentrated solution process capacitive desalination processing that produces, then be circulated to anoxic pond through pump reflux.
The effluent quality situation of the percolate after table 3 is processed
Sequence number Project Unit Measured value Sequence number Project Unit Measured value
1 COD Cr mg/L 58 5 Ammonia nitrogen mg/L ≤5
2 SS mg/L ≤5 6 Colourity Doubly 8
3 Turbidity NTU ≤5 7 The pH value - 7.2
4 BOD 5 mg/L 16 8 Specific conductivity μS/cm ≤3500
Embodiment 2
The percolate of certain garbage sanitary filling field 300 ton per day is processed engineering
Index is as shown in table 4 after measured for the former water of described percolate.
The water quality situation of the former water of table 4 percolate.
Sequence number Project Unit Measured value Sequence number Project Unit Measured value
1 COD Cr mg/L 89600 5 Ammonia nitrogen mg/L 3660
2 SS mg/L 802 6 Colourity Doubly 2500
3 Turbidity NTU 730 7 The pH value - 9.3
4 BOD 5 mg/L 17900 8 Specific conductivity μS/cm 9030
Step a, ammonia nitrogen removal
Percolate enters the equalizing tank regulating water quality through pipeline, and the balanced water yield makes flow and parameter from refuse landfill percolate of different nature everywhere be able to abundant adjusting, is convenient to the processing of follow-up unit.And add lime to regulate pH value to 10 ~ 11 by chemicals dosing plant in equalizing tank, then flow in stripping tower, making ammonia nitrogen in high density in percolate convert free ammonia to by the steam stripping is blown, to reach the purpose of removing ammonia nitrogen, enter rear coagulation basin after making its ammonia nitrogen concentration≤200mg/L; The ammonia that stripping goes out is back to soda ash production with absorption by Hydrochloric Acid generation ammonium chloride and makes mother liquor.
Step b, flocculation sediment
Flow into coagulation basin after the percolate ammonia nitrogen removal, percolate per ton adds 250g ferrous sulfate (FeSO 4), entering preliminary sedimentation tank after reacting completely, the precipitation of preliminary sedimentation tank (being mud) is sent in sludge sump through pump and pipeline, carries out at last filtering separation in sludge dehydration device; The COD of percolate reduces by 10~35% rear inflow electrolysis machines.
Above-mentioned ferrous sulfate is flocculation agent.Flocculation agent can be a kind of or any two the above combination in aluminium salt (Tai-Ace S 150, aluminum chloride), molysite (ferric sulfate, ferrous sulfate, iron(ic) chloride), poly-aluminium (polymerize aluminum chloride, polyaluminium sulfate, polymer aluminium silicate), Polyferric Sulfate (poly-ferric chloride, bodied ferric sulfate, polymeric silicicacid iron), organic polymer coargulator or microbial flocculant.
Step c, electrolysis
Percolate enters intermediate pool, and adds reductive agent through flowing into the electrolysis machine electrolysis after flocculation sediment after electrolysis, remove the remaining free radical that electrolysis produces; The electrolysis machine operating voltage is 4V, and current density is 150mA/cm 2, the voltage between two neighboring pole is 2 V.
Steps d, capacitive desalination
The specific conductivity of percolate after step c electrolysis treatment>5000 μ s/cm first carry out capacitive desalination and process, and enter step e anaerobic treatment after making its specific conductivity be reduced to 500~3000 μ s/cm.
Step e, anaerobic treatment
Percolate after capacitive desalination is processed enters in hydrolysis acidification pool and anoxic pond successively, the residence time is 36 hours, larger molecular organics in hydrolysis acidification pool in percolate acidication under the effect of acid-producing bacteria becomes small organic molecule, resolve into methane and carbon dioxide under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane in the process anoxic pond again, improve the B/C value, improve biodegradability; Denitrification by denitrifying bacterium in anoxic pond simultaneously further removes the ammonia nitrogen in percolate.
Step f, aerobic treatment
Percolate after anaerobic treatment enters in the Aerobic Pond of microorganisms such as containing aerobic bacteria, nitrobacteria and nitrite bacteria, the residence time is 180 hours, make good use of the organism in the further oxygenolysis percolate of oxygen animalcule, the degree of depth is removed the COD in percolate CrAnd BOD 5, utilize simultaneously the nitrification of nitrobacteria and the nitrosification of nitrite bacteria to make ammonia-state nitrogen be converted into nitric nitrogen or nitrite nitrogen; In addition, the mixed solution of Aerobic Pond is back to anoxic pond with the ratio of 2:1 by reflux pump.
Step g, re-electrolysis
COD 〉=the 400mg/L of the percolate after aerobic treatment, therefore flowing into electrolysis machine carries out re-electrolysis, makes wherein larger molecular organics open loop chain rupture, improve biodegradability, and during electrolysis, adjacent two interelectrode voltages of electrolysis machine are 5V, and current density is 190mA/cm 2
Step h, membrane filtration
Percolate after re-electrolysis is processed flows into second pond, after further COD, the BOD and SS that removes in percolate of precipitation, make water outlet reach the reuse water standard through immersion ultrafiltration and nanofiltration filtration successively, the mud part of second pond bottom through pump reflux to anoxic pond, another part flows in sludge sump by pipeline, become filtrate and mud cake through the sludge dehydration device filtering separation again, filtrate flow in equalizing tank through back of pipeline, and mud cake is transported outward.
The working conditions of described immersion ultrafiltration is: normal temperature~45 ℃, operating pressure are-1~-50kPa; The membrane module of described nanofiltration is rolled membrane module, and mould material is composite nanometer filtering film, and entrance pressure is 6.0~45.0bar, and going out to press is 4.5~43.5 bar.
Above-mentioned ultra-filtration equipment is the immersion ultrafiltration.Ultra-filtration equipment can be a kind of of immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration.
Step I, film filtration concentrated processing
After the concentrated solution process capacitive desalination processing that produces is filtered in the ultrafiltration of step h immersion and nanofiltration, then be circulated to anoxic pond through pump reflux.
The effluent quality situation of the percolate after table 5 is processed
Sequence number Project Unit Measured value Sequence number Project Unit Measured value
1 COD Cr mg/L 54 5 Ammonia nitrogen mg/L ≤5
2 SS mg/L ≤5 6 Colourity Doubly 3
3 Turbidity NTU ≤5 7 The pH value - 7.2
4 BOD 5 mg/L 17 8 Specific conductivity μS/cm ≤1200
Embodiment 3
The percolate of certain garbage sanitary filling field 1500 ton per day is processed engineering
Index is as shown in table 6 after measured for the former water of described percolate.
The water quality situation of the former water of table 6 percolate.
Sequence number Project Unit Measured value Sequence number Project Unit Measured value
1 COD Cr mg/L 284300 5 Ammonia nitrogen mg/L 4510
2 SS mg/L 1381 6 Colourity Doubly 4500
3 Turbidity NTU 1200 7 The pH value - 9.5
4 BOD 5 mg/L 42800 8 Specific conductivity μS/cm 11290
Step a, ammonia nitrogen removal
Percolate enters the equalizing tank regulating water quality through pipeline, and the balanced water yield makes flow and parameter from refuse landfill percolate of different nature everywhere be able to abundant adjusting, is convenient to the processing of follow-up unit.And add lime to regulate pH value to 10 ~ 11 by chemicals dosing plant in equalizing tank, then flow in gravity machine, making ammonia nitrogen in high density in percolate convert free ammonia to by air stripping is blown, to reach the purpose of removing ammonia nitrogen, enter coagulation basin after making its ammonia nitrogen concentration≤200mg/L, the ammonia that stripping goes out is produced the ammonium sulfate byproduct with sulfuric acid absorption
Step b, flocculation sediment
Flow into coagulation basin after the percolate ammonia nitrogen removal, percolate per ton adds 1500g ferrous sulfate (FeSO 4), entering preliminary sedimentation tank after reacting completely, the precipitation of preliminary sedimentation tank (being mud) is sent in sludge sump through pump and pipeline, carries out at last filtering separation in sludge dehydration device; Enter electrolysis machine after COD reduction by 10~35% with percolate.
Above-mentioned ferrous sulfate is flocculation agent.Flocculation agent can be a kind of or any two the above combination in aluminium salt (Tai-Ace S 150, aluminum chloride), molysite (ferric sulfate, ferrous sulfate, iron(ic) chloride), poly-aluminium (polymerize aluminum chloride, polyaluminium sulfate, polymer aluminium silicate), Polyferric Sulfate (poly-ferric chloride, bodied ferric sulfate, polymeric silicicacid iron), organic polymer coargulator or microbial flocculant.
Step c, electrolysis
Percolate after flocculation sediment is processed pumps into the electrolysis machine electrolysis, enters intermediate pool after electrolysis, and adds reductive agent, removes the remaining free radical that electrolysis produces; The current density of electrolysis machine is 320mA/cm 2, the voltage of two interpolars is 12 V.
Steps d, capacitive desalination
Through the specific conductivity of percolate after step c electrolysis treatment 〉=5000 μ s/cm, therefore first process through capacitive desalination, enter step e anaerobic treatment after making its specific conductivity be reduced to 500~3000 μ s/cm.
Step e, anaerobic treatment
Percolate after capacitive desalination is processed enters in hydrolysis acidification pool and anoxic pond successively, the residence time is 72 hours, larger molecular organics in hydrolysis acidification pool in percolate acidication under the effect of acid-producing bacteria becomes small organic molecule, resolve into methane and carbon dioxide under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane in the process anoxic pond again, improve the B/C value, improve biodegradability; Denitrification by denitrifying bacterium in anoxic pond simultaneously further removes the ammonia nitrogen in percolate.
Step f, aerobic treatment
Percolate after anaerobic treatment enters in the Aerobic Pond of microorganisms such as containing aerobic bacteria, nitrobacteria and nitrite bacteria, the residence time is 280 hours, make good use of the organism in the further oxygenolysis percolate of oxygen animalcule, the degree of depth is removed the COD in percolate CrAnd BOD 5, utilize simultaneously the nitrification of nitrobacteria and the nitrosification of nitrite bacteria to make ammonia-state nitrogen be converted into nitric nitrogen or nitrite nitrogen; In addition, the mixed solution of Aerobic Pond is back to anoxic pond with the ratio of 3:1 by reflux pump.
Step g, re-electrolysis
COD 〉=the 400mg/L of the percolate after aerobic treatment, therefore flowing into electrolysis machine carries out re-electrolysis, makes wherein larger molecular organics open loop chain rupture, improve biodegradability, and during electrolysis, adjacent two interelectrode voltages of electrolysis machine are 16V, and current density is 300mA/cm 2
Step h, membrane filtration
Percolate after re-electrolysis is processed flows into second pond, after further COD, the BOD and SS that removes in percolate of precipitation, make water outlet reach the reuse water standard through pillar ultrafiltration and osmosis filtration successively, the mud part of second pond bottom through pump reflux to anoxic pond, another part flows in sludge sump by pipeline, become filtrate and mud cake through the sludge dehydration device filtering separation again, filtrate flow in equalizing tank through back of pipeline, and mud cake is transported outward.
The working conditions of described pillar ultrafiltration is: normal temperature~45 ℃, and operating pressure is 3~300kPa; The membrane module of described reverse osmosis is rolled membrane module, and mould material is composite membrane, and entrance pressure can be 6.0~45.0bar, goes out to press to can be 4.5~35 bar.
Above-mentioned ultra-filtration equipment is the pillar ultrafiltration.Ultra-filtration equipment can be a kind of of immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration.
Step I, film filtration concentrated processing
After the concentrated solution that the ultrafiltration of step h pillar and osmosis filtration produce is processed through capacitive desalination, then be circulated to anoxic pond through pump reflux.
The effluent quality situation of the percolate after table 7 is processed
Sequence number Project Unit Measured value Sequence number Project Unit Measured value
1 COD Cr mg/L 46 5 Ammonia nitrogen mg/L ≤5
2 SS mg/L ≤5 6 Colourity Doubly 5
3 Turbidity NTU ≤5 7 The pH value - 7.2
4 BOD 5 mg/L 21 8 Specific conductivity μS/cm ≤100
Above-mentioned is only the specific embodiment of the present invention, but design concept of the present invention is not limited to this, allly utilizes this design to carry out the change of unsubstantiality to the present invention, all should belong to the behavior of invading protection domain of the present invention.

Claims (12)

1. the treatment process of a percolate is characterized in that it comprises the following steps:
A, ammonia nitrogen removal
Percolate enters the equalizing tank regulating water quality through pipeline, the balanced water yield, and add pH adjusting agent by chemicals dosing plant in equalizing tank, flow in ammonia nitrogen blowing-off device or reaction tank after regulating the pH value, making ammonia nitrogen in high density in percolate convert free ammonia to by steam or air stripping in ammonia nitrogen blowing-off device is blown, perhaps adds appropriate Mg(OH by chemicals dosing plant in reaction tank) 2And H 3PO 4, with NH 4+Reaction generates MgNH 4PO 46H 2O precipitation to reach the purpose of removing ammonia nitrogen, enters the subsequent disposal operation after making its ammonia nitrogen concentration≤200mg/L;
B, flocculation sediment
Flow into coagulation basin after the percolate ammonia nitrogen removal, add appropriate flocculation agent by chemicals dosing plant in coagulation basin, enter preliminary sedimentation tank after reacting completely, the throw out of preliminary sedimentation tank is sent in sludge sump through pump and pipeline, carry out at last filtering separation in sludge dehydration device, with the COD reduction by 10~35% of percolate;
C, electrolysis
Percolate after flocculation sediment is processed pumps into the electrolysis machine electrolysis, enters intermediate pool after electrolysis, and adds reductive agent, removes the remaining free radical that electrolysis produces; Adjacent two interelectrode voltages of electrolysis machine are 2~12V, and current density is 10~320mA/cm 2
D, capacitive desalination
During the specific conductivity of percolate after through step c electrolysis treatment 〉=5000 μ s/cm, first process through the steps d capacitive desalination, make its specific conductivity be reduced to 500~3000 μ s/cm, then enter step e anaerobic treatment; During the specific conductivity of percolate after through step c electrolysis treatment<5000 μ s/cm, directly enter step e anaerobic treatment;
E, anaerobic treatment
Percolate after electrolysis treatment or capacitive desalination are processed enters in hydrolysis acidification pool and anoxic pond successively, the residence time is 8~72 hours, larger molecular organics in hydrolysis acidification pool in percolate acidication under the effect of acid-producing bacteria becomes small organic molecule, resolve into methane and carbon dioxide under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane in the process anoxic pond again, improve the B/C value, improve biodegradability; Denitrification by denitrifying bacterium in anoxic pond simultaneously further removes the ammonia nitrogen in percolate;
F, aerobic treatment
Percolate after anaerobic treatment enters in the Aerobic Pond that contains aerobic bacteria, nitrobacteria and nitrite bacteria, the residence time is 16~360 hours, make good use of the organism in the further oxygenolysis percolate of oxygen animalcule, the degree of depth is removed COD and the BOD in percolate, utilizes simultaneously the nitrification of nitrobacteria and the nitrosification of nitrite bacteria to make ammonia-state nitrogen be converted into nitric nitrogen or nitrite nitrogen; In addition, the partially mixed liquid of Aerobic Pond is back to anoxic pond by reflux pump;
G, re-electrolysis
When through the COD of the percolate after aerobic treatment 〉=400mg/L, to carry out re-electrolysis through the percolate after aerobic treatment, make wherein larger molecular organics open loop chain rupture, improve biodegradability, and during electrolysis, adjacent two interelectrode voltages of electrolysis machine are 3~18V, and current density is 20~320mA/cm 2When through the COD of the percolate after aerobic treatment<400mg/L, directly enter step h membrane filtration;
H, membrane filtration
Percolate after aerobic treatment or re-electrolysis are processed flows into second pond, after further COD, the BOD and SS that removes in percolate of precipitation, make water outlet reach the reuse water standard through membrane filtration, the mud part of second pond bottom through pump reflux to anoxic pond, another part flows in sludge sump by pipeline, become filtrate and mud cake through the sludge dehydration device filtering separation again, filtrate flow in equalizing tank through back of pipeline, and mud cake is transported outward;
I, film filtration concentrated processing
After the concentrated solution that step h membrane filtration produces is processed through capacitive desalination, then be circulated to anoxic pond through pump reflux.
2. the treatment process of a kind of percolate as claimed in claim 1, it is characterized in that: ammonia nitrogen blowing-off device described in step a is stripping tower, packing tower or gravity machine; The ammonia that described stripping goes out is back to soda ash production with absorption by Hydrochloric Acid generation ammonium chloride and makes mother liquor, or water absorbs production ammoniacal liquor or produces the ammonium sulfate byproduct with sulfuric acid absorption.
3. the treatment process of a kind of percolate as claimed in claim 1, is characterized in that: MgNH described in step a 4PO 46H 2The O throw out is after granulation process, and exploitation is used as composite fertilizer.
4. the treatment process of a kind of percolate as claimed in claim 1, it is characterized in that: flocculation agent described in step b is a kind of or any two the above combination in aluminium salt, molysite, poly-aluminium, Polyferric Sulfate, organic polymer coargulator or microbial flocculant, described aluminium salt is Tai-Ace S 150 or aluminum chloride, described molysite is ferric sulfate, ferrous sulfate or iron(ic) chloride, described poly-aluminium is polymerize aluminum chloride, polyaluminium sulfate or polymer aluminium silicate, and described Polyferric Sulfate is poly-ferric chloride, bodied ferric sulfate or polymeric silicicacid iron; Described pH adjusting agent is a kind of in sulfuric acid, hydrochloric acid, sodium hydroxide, sodium carbonate, sodium bicarbonate, lime.
5. as the treatment process of claim 1 or 4 described a kind of percolate, it is characterized in that: optimum flocculent described in step b is bodied ferric sulfate, and its dosage is percolate 200~2000g per ton.
6. as the treatment process of claim 1 or 4 described a kind of percolate, it is characterized in that: optimum flocculent described in step b is ferrous sulfate, and its dosage is percolate 230~1800g per ton.
7. the treatment process of a kind of percolate as claimed in claim 1, it is characterized in that: electrolysis machine described in step c is provided with power supply and electrolyzer, and the electrode materials in electrolyzer is a kind of in the alloy of graphite, titanium, iron, aluminium, zinc, copper, lead, nickel, molybdenum, chromium, metal and nano-catalytic noble electrode; The top layer of described nano-catalytic noble electrode is coated with the metal oxide inertia catalyst coatings that crystal grain is 10~35nm; The substrate of described nano-catalytic noble electrode is titanium plate or plastic plate.
8. as the treatment process of claim 1 or 7 described a kind of percolate, it is characterized in that: best electrolysis described in step c is the nano-catalytic electrolysis, the operating voltage of electrolysis is 2~500V, and adjacent two interelectrode voltages are 2~8 V, and current density is 10~300mA/cm 2
9. the treatment process of a kind of percolate as claimed in claim 1, it is characterized in that: the reflux ratio of mixed solution described in step f is 3:1 or 2:1.
10. the treatment process of a kind of percolate as claimed in claim 1, is characterized in that: the percolate again process membrane bioreactor filtration of membrane filtration described in step h for passing through the second pond precipitate and separate; Described membrane bioreactor membrane module is selected from a kind of in Pvdf Microporous Hollow Fiber Membrane, polypropylene hollow fiber membrane, ps hollow fiber uf membrane, polyethersulfone, polyacrylonitrile and PVC hollow fiber membrane, membrane pore size is 0.10~0.2 μ m, operating pressure is-1~-50kPa, working temperature is 5~45 ℃.
11. the treatment process of a kind of percolate as claimed in claim 1 is characterized in that: after the percolate process ultra-filtration filters of membrane filtration described in step h for process second pond precipitate and separate, then filter through nanofiltration; Described ultrafiltration is immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000~100000MWCO, working conditions is: normal temperature~45 ℃, the operating pressure of immersion ultrafiltration is-1~-50kPa, the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3~300kPa; The membrane module of described nanofiltration is rolled membrane module, and the mould material of nanofiltration membrane is cellulose acetate film or composite nanometer filtering film in organic membrane, and the molecular weight cut-off of nanofiltration membrane is 200~500MWCO, and entrance pressure is 6.0~45.0bar, and going out to press is 4.5~43.5 bar.
12. the treatment process of a kind of percolate as claimed in claim 1 is characterized in that: membrane filtration described in step h is after the percolate of process second pond precipitate and separate first passes through ultra-filtration filters, then passes through reverse osmosis (RO) and filter; The membrane module of described reverse osmosis is rolled membrane module, and mould material is cellulose acetate film or composite membrane in organic membrane, and the molecular weight cut-off of mould material is 50~200MWCO, and entrance pressure is 6.0~45.0bar, and going out to press is 4.5~35 bar.
CN2012100865958A 2012-03-29 2012-03-29 Method for processing garbage leachate Active CN102786183B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2012100865958A CN102786183B (en) 2012-03-29 2012-03-29 Method for processing garbage leachate

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN2012100865958A CN102786183B (en) 2012-03-29 2012-03-29 Method for processing garbage leachate
PCT/CN2013/076203 WO2013143506A1 (en) 2012-03-29 2013-05-24 Waste percolate treatment method

Publications (2)

Publication Number Publication Date
CN102786183A CN102786183A (en) 2012-11-21
CN102786183B true CN102786183B (en) 2013-06-12

Family

ID=47151796

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2012100865958A Active CN102786183B (en) 2012-03-29 2012-03-29 Method for processing garbage leachate

Country Status (2)

Country Link
CN (1) CN102786183B (en)
WO (1) WO2013143506A1 (en)

Families Citing this family (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102786183B (en) * 2012-03-29 2013-06-12 波鹰(厦门)科技有限公司 Method for processing garbage leachate
CN103172217A (en) * 2013-02-26 2013-06-26 吉林市环境保护科学研究院 Large-scale livestock breeding sewage treatment method and equipment
CN103241912B (en) * 2013-05-31 2014-04-02 波鹰(厦门)科技有限公司 Method for processing waste water generated in production of tobacco sheet
CN103265151B (en) * 2013-06-09 2014-12-03 广东新大禹环境工程有限公司 Treatment method of heavy metal wastewater
CN103539319B (en) * 2013-10-31 2014-10-08 华北电力大学 Garbage leachate treating device
CN103626251A (en) * 2013-12-04 2014-03-12 彭传义 Three-phase azeotropic ammonia removal method
CN103951141B (en) * 2014-05-08 2015-12-30 东莞市环境科学研究所 A kind of garbage leachate treatment process and treatment unit
CN105271477A (en) * 2014-06-06 2016-01-27 蒋寿悟 Deep treatment method of municipal waste landfill leachate
CN104787867A (en) * 2015-05-04 2015-07-22 李练红 Flocculant for river/lake water body original ecological restoration and application thereof
CN105018961B (en) * 2015-07-02 2017-09-05 北京师范大学 It is a kind of that the method that percolate prepares alcohols is reduced with electro-catalysis
CN105859042A (en) * 2016-05-18 2016-08-17 哈尔滨工业大学深圳研究生院 Sewage treatment method and system
CN106520527B (en) * 2016-10-20 2018-09-04 山东科技大学 A kind of device and method generated using microorganism induction guanite
CN106430863A (en) * 2016-12-19 2017-02-22 宜兴市宜刚环保工程材料有限公司 Landfill leachate treatment method
CN108623085B (en) * 2017-03-18 2022-05-31 深圳市深水生态环境技术有限公司 Advanced treatment method for high-nitrogen organic wastewater membrane filtration concentrate
DE102017207286A1 (en) * 2017-04-28 2018-10-31 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. METHOD AND DEVICE FOR PREPARING WASTE PRODUCTS
CN109665651A (en) * 2017-10-13 2019-04-23 中国石油化工股份有限公司 The processing method of paranitroanilinum production waste water
CN108675518A (en) * 2018-05-17 2018-10-19 师海荣 A kind of preprocess method of aged refuse in MSW landfill percolate
CN112110601A (en) * 2019-06-19 2020-12-22 祝来宏 Method and device for treating landfill leachate
CN110668633A (en) * 2019-07-31 2020-01-10 南京万德斯环保科技股份有限公司 Kitchen waste sorting wastewater treatment system and process
CN111253013A (en) * 2020-03-13 2020-06-09 桂润环境科技股份有限公司 Method and device for treating landfill leachate membrane concentrated solution
CN111547939B (en) * 2020-05-09 2022-03-22 四川省生态环境科学研究院 High-concentration wastewater dephosphorization process
CN111825220A (en) * 2020-06-30 2020-10-27 深圳文科园林股份有限公司 Method for treating anaerobic digestion liquid and wastewater treatment device
CN112108500B (en) * 2020-09-14 2021-11-30 安徽清扬水处理设备科技有限公司 High-efficiency treatment process for landfill leachate
CN112266129A (en) * 2020-09-29 2021-01-26 武汉大学 Wastewater treatment apparatus and wastewater treatment method
CN112875992A (en) * 2021-01-25 2021-06-01 新地环保技术有限公司 Landfill leachate disposal method and system
CN113003726A (en) * 2021-03-04 2021-06-22 重庆理工大学 Treatment method of reverse osmosis membrane filtration concentrated solution of landfill leachate
CN113045113A (en) * 2021-03-12 2021-06-29 佛山市诚德新材料有限公司 Waste residue drying processing system
CN113371905A (en) * 2021-05-27 2021-09-10 南京万德斯环保科技股份有限公司 Treatment method of high-ammonia nitrogen high-salinity leachate
CN113443794A (en) * 2021-08-11 2021-09-28 南通固润环保科技有限公司 Landfill leachate treatment system

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1209304C (en) * 2003-07-14 2005-07-06 宜兴鹏鹞阳光环保有限公司 Garbage percolation liquid treatment process
TWI313187B (en) * 2003-11-21 2009-08-11 Ind Tech Res Inst System for the treatment of organic containing waste water
KR20060058198A (en) * 2004-11-24 2006-05-30 (주)첨단종합기술개발 Recycling system for daily life sewage and organic waste
CN102040301B (en) * 2009-10-19 2013-04-17 中国科学院生态环境研究中心 Method for treating municipal waste leachate membrane concentrated solution
CN101891336B (en) * 2010-06-25 2012-07-04 北京伊普国际水务有限公司 System and method for leachate treatment in sanitary landfill
CN102276117A (en) * 2011-07-21 2011-12-14 波鹰(厦门)科技有限公司 Treatment device and method for garbage percolate
CN102786183B (en) * 2012-03-29 2013-06-12 波鹰(厦门)科技有限公司 Method for processing garbage leachate

Also Published As

Publication number Publication date
CN102786183A (en) 2012-11-21
WO2013143506A1 (en) 2013-10-03

Similar Documents

Publication Publication Date Title
CN102786183B (en) Method for processing garbage leachate
CN102603119B (en) Garbage leachate treatment device and treatment method thereof
CN102786182B (en) Device for processing landfill leachate
CN104016547B (en) A kind of coking waste water deep treatment zero-emission process
CN102344227B (en) Hairwork waste water cyclic utilization device and treatment method thereof
US20130264197A1 (en) Nanocatalytic electrolysis and flocculation apparatus
CN103359896B (en) A treatment, regeneration and cyclic utilization method for tobacco sheet production wastewater
CN203568944U (en) Coking wastewater reuse treatment system
CN103241910B (en) Treatment method of tobacco sheet production wastewater
JP2006068617A (en) Method and apparatus for treating water medium
CN103351088B (en) Treatment and regenerative cyclic utilization device for tobacco sheet production wastewater
CN106800356A (en) A kind of advanced treatment of wastewater regeneration device based on biochemical and electrolysis tech
CN107055937A (en) A kind of advanced treatment of wastewater regeneration method based on biochemical and electrolysis tech
CN103553282B (en) Advanced treatment process of coking waste water
CN105481168A (en) Coal gasification sewage comprehensive treatment method
CN107698037A (en) The method of the three-dimensional biological advanced treatment of landfill leachate reverse osmosis concentrated water of electricity of three-dimensional electrochemical coupling
CN103241912B (en) Method for processing waste water generated in production of tobacco sheet
CN103241909B (en) Process device for waste water generated in tobacco sheet production
CN202610073U (en) Processing apparatus of garbage percolating liquid
CN102249501B (en) Device and method for treating wastewater produced by hair-product manufacturing
KR101102443B1 (en) complexed water treatment method and the apparatus preparing for water-lack situation
CN109851160B (en) Advanced sewage treatment method
CN103241911B (en) Treatment device for tobacco sheet production wastewater
CN203360236U (en) Treatment, regeneration and recycling device for production wastewater of reconstituted tobacco
KR20020018572A (en) Electro coagulation and Bio-wrinkled circulation nutrients removal system

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model