CN102040301B - Method for treating municipal waste leachate membrane concentrated solution - Google Patents
Method for treating municipal waste leachate membrane concentrated solution Download PDFInfo
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Abstract
The invention relates to a treatment combination process of municipal waste leachate membrane effluent concentrated solution, consisting of a first coagulation-sedimentation unit, a photoelectric oxidation unit, a second coagulation-sedimentation unit and a filtering unit. The first coagulation-sedimentation unit is used for firstly removing macromolecule soluble matters in the membrane concentration solution, using calcium hydroxide, poly-ferric chloride, polyaluminium chloride or a compound of aluminum sulphate and calcium hydroxide, and adding coagulant aid polyacrylamide with a dosage of 10mg/L simultaneously, wherein the dosage of a flocculant agent is 500-800mg/L, a chemical oxygen demand removal rate is about 40% after the coagulation-sedimentation treatment, and the chromaticity removal rate is over 50%. The photoelectric oxidation unit is capable of effectively removing ammonia nitrogen and a part of hardly-degraded organic matter, wherein a current density applied by the photoelectric oxidation unit is within a range of 200-500A/m<2>, a residual time is 1.0-2.0 hours, an electrode material is a shape stability electrode, a lamp source is a UV lamp, the ammonia nitrogen removal rate is 80%, and the effluent chemical oxygen demand removal rate is about 800-1000 mg/L. The second coagulation-sedimentation is used for removing the rest organic component and metal ion, wherein the dosage of ferrous sulfate is 500mg/L, simultaneously the calcium hydroxide or quick lime solution with a concentration of 500mg/L is added, the effluent chemical oxygen demand can be reduced to be less than 500 mg/L, and the ammonia nitrogen concentrate ion is reduced to 50 mg/L. Finally, a sand filtering unit is used for filtering flocs and suspended matter.
Description
Technical field
The present invention discloses the film filtration concentrated treatment process of a kind of effective treating refuse percolate, belongs to water-treatment technology field.
Background technology
The sanitary landfill of municipal wastes, compost are the treating method for urban garbage of at present domestic extensive employing.The percolate that rubbish produces in landfill, composting process is that a kind of water quality and quantity changes greatly, ammonia-nitrogen content is high, the difficult organic waste water of the high density of complicated component.Along with the raising of national requirements for environmental protection, certain areas come into effect new emission standard policy gradually.Water outlet requires to reach the requirement of GB 16889-2008 " State Standard of the People's Republic of China " table 3.Traditional biochemical treatment and coagulation-settlement process are difficult to satisfy the demands.Thereby how people are exploring the treating refuse percolate of efficient economy always.Fully up to standard in order to guarantee chemical oxygen demand (COD) (COD), ammonia nitrogen and total nitrogen, nanofiltration and reverse osmosis combination technique are usually adopted in certain areas now.The Persistent organic pollutants major part of bio-chemical effluent can be held back by nano-filtration unit, and the nanofiltration water outlet can guarantee almost that through reverse-osmosis treated all contamination indexs all can reach emission request.But there are problems in nanofiltration and reverse osmosis combination process in actual mechanical process.The influent load of nanofiltration and reverse osmosis is larger, has increased membrane pollution problem, and the cleaning strength increase, and the work-ing life of film is short.Although nanofiltration and reverse osmosis membrane have splendid rejection to organic pollutant, unstable to the cutoff performance of ammonia nitrogen, easily cause the water outlet ammonia nitrogen concentration to exceed standard.Membrane process has just been realized holding back to pollutent simultaneously, has the dense water generates of a large amount of films in the film unit process, and the dense glassware for drinking water of the film of generation has higher COD content and salinity.Some landfill yards adopt its method of recharging landfill yard are processed, but because a large amount of reverse osmosis concentrated waters is difficult to by biochemical degradation, therefore enter again again in the percolation liquid treating system, it contains the high density salinity simultaneously, has a strong impact on percolation liquid treating system and normally moves.
Therefore the concentrated solution that produces is in need of immediate treatment.At present both at home and abroad the treatment process of concentrated solution roughly has 2 kinds in garbage leachate treatment process, a kind of be with Concentrated liquid recharge in landfill yard, the essence of this treating method is the concentrated solution infinite reflux, and leachate quality is run down.Be exactly to carry out simple process in addition, usually employing method has coagulant sedimentation, evaporation mummification method and absorption burning method etc.Wherein evaporate the mummification method high to equipment requirements, working cost is high, and operational administrative is complicated; The absorption burning method moves more abroad, but to sorbent material require high, the gac bad mechanical strength that usually adopts, regeneration difficulty.In addition, the Li Aimin of Nanjing University professor and the treatment process of German Wei Erli company's joint study take ion exchange resin as core it is reported that water after the processing meets the first discharge standard among the GB16889-97.This method is take the adsorb organic compound of antipollution resin as main processing means, usually common ion exchange resin uses under high COD condition, operating capacity sharply descends, and the regeneration waste liquid of concentrated solution after resin absorption is saturated of ion exchange resin absorption more is difficult to process.
Summary of the invention
The treatment process that the purpose of this invention is to provide membrane concentration liquid in the processing of one way of life percolate.
Technique disclosed by the invention mainly comprises coagulating sedimentation one time, photoelectricity oxide treatment, second coagulation precipitation and filter four unit.A coagulating sedimentation unit: the nanofiltration membrane water outlet is usually as the follow-up unit of biochemical treatment, the water outlet of nanofiltration membrane mainly is the organism of molecular weight below 500 dalton, therefore the concentrated solution of nanofiltration membrane is mainly the organic pollutant of the macromolecule of difficult for biological degradation, this part is mainly deliquescent soil ulmin, awkward biodegradability component.By adding flocculation agent and coagulant aids pollutent is reacted by coagulating sedimentation, the organic substance of most macromolecule can be removed in the coagulating sedimentation unit, to guarantee to enter the requirement of photoelectricity oxidation unit influent quality.Coagulating agent can adopt the composite of calcium hydroxide, poly-ferric chloride, polymerize aluminum chloride or Tai-Ace S 150 and calcium hydroxide, needs simultaneously to add to help to coagulate medicament polyacrylamide (PAM).The throwing amount of coagulating agent is about 500-800mg/L, and polyacrylamide throwing amount is 10mg/L.About about 30%, percent of decolourization is 60% to the clearance of COD greatly in precipitation process of coagulation.
Photoelectricity oxidation unit: contain remaining dissolved organic matter and ammonia nitrogen in the water outlet through the coagulating sedimentation unit, be mainly the component of molecular weight.Photoelectrocatalysis is processed can carry out oxide treatment with remaining dissolved organic matter, simultaneously can oxidation removal overwhelming majority ammonia nitrogens and total nitrogen class material, and after the processing of photoelectricity oxidising process, can be to the percolate disinfection, deactivation is most microorganism and germ wherein.The residence time of photoelectricity oxide treatment is 1-2 hour, and the current density that adopts is 200-500A/m
2, electrode materials is the steady electrode of shape, light source is ultraviolet lamp.Adopt photoelectricity oxide treatment unit can effectively remove ammonia nitrogen and total nitrogen, the clearance of COD is approximately about 60%.
Second coagulation sedimentation and filtration unit: be approximately about 1000-2000mg/L through COD in the water outlet of photoelectricity oxide treatment unit.We have carried out further coagulating sedimentation processing for this reason.In the treating processes, at first we add copperas solution in the water outlet of photovoltaic element in this section, and concentration is 500mg/L.Add simultaneously calcium hydroxide or unslaked lime solution, concentration is 500mg/L.
Filtering unit: filtering unit is connected on the back of second coagulation precipitation water outlet, and filtrate is manganese sand or quartz sand.
Description of drawings
Fig. 1. rubbish percolation liquid membrane concentrated solution combined treatment process
Embodiment
Embodiment 1
Adopt combination process disclosed by the invention to process certain rubbish percolation liquid membrane and go out concentrated liquid, this landfill yard picks up from Beijing landfill yard.This landfill yard at first adopts anaerobic technique to process, and then adopts aerobic membrane bioreactor to carry out aerobic treatment, and bio-chemical effluent is through nanofiltration membrane treatment, and the oxidation water outlet namely can the water outlet qualified discharge at process absorption/oxidation filtering unit.Concentrated solution water outlet chemical oxygen demand (COD) concentration is 8000-9000mg/L, and ammonia nitrogen concentration is 2000-2500mg/L.A coagulating sedimentation unit adopts the poly-ferric chloride coagulant of commercial grade, add simultaneously coagulant aids polyacrylamide (20mg/L), the photovoltaic element residence time is 1 hour, the second coagulation precipitation adopts ferrous sulfate, calcium hydroxide and unslaked lime, consumption is 1g/L, the coagulating sedimentation time is 1.0 hours, and it is filtrate that filtering unit adopts quartz sand.End reaction water outlet chemical oxygen demand (COD) concentration is 480mg/L, and ammonia nitrogen concentration is 45mg/L.
Embodiment 2
Adopt embodiment 1 described percolate treating process.Percolate picks up from certain landfill yard of south, and percolate treating process is anaerobism → SBR aerobic membrane bioreactor → nanofiltration → water outlet.Percolate nanofiltration membrane concentrated solution COD
CrConcentration is 6000-7000mg/L, and ammonia nitrogen concentration is 1500mg/L.The coagulating sedimentation unit adopts industrial polymerize aluminum chloride as coagulating agent, and consuming amount of concrete is 600mg/L; Add simultaneously coagulant aids polyacrylamide (20mg/L).The photoelectricity oxidation residence time is 2 hours, and the second coagulation precipitation adopts ferric sulfate, calcium hydroxide and unslaked lime, and consumption is 5g/L, and the coagulating sedimentation time is 1.5 hours, and it is filtrate that filtering unit adopts manganese sand.Final outflow water COD
CrConcentration is 350mg/L, and ammonia nitrogen concentration is 30mg/L.
Embodiment 3
Adopt embodiment 1 described percolate treating process.Percolate picks up from certain landfill yard of south, and percolate treating process is anaerobism → SBR aerobic membrane bioreactor → nanofiltration → water outlet.Percolate nanofiltration membrane concentrated solution COD
CrConcentration is 6000-7000mg/L, and ammonia nitrogen concentration is 1500mg/L.One time the coagulating sedimentation unit adopts calcium hydroxide as coagulating agent, and consuming amount of concrete is 5g/L; Add simultaneously coagulant aids polyacrylamide (50mg/L).The photoelectricity oxidation residence time is 3 hours, and the second coagulation precipitation adopts ferrous sulfate and unslaked lime, and consumption is 1g/L, and 15 minutes coagulation time, sedimentation time is 1.0 hours, and it is filtrate that filtering unit adopts flyash.Final outflow water COD
CrConcentration is 380mg/L, and ammonia nitrogen concentration is 27mg/L.
Embodiment 4
Adopt embodiment 1 described percolate treating process.Percolate picks up from southern 1 landfill yard, and percolate treating process is anaerobism → SBR aerobic membrane bioreactor → nanofiltration → water outlet.Percolate nanofiltration membrane concentrated solution COD
CrConcentration is 6000-7000mg/L, and ammonia nitrogen concentration is 1500mg/L.The coagulating sedimentation unit adopts commercial sulphuric acid aluminium and calcium hydroxide as coagulating agent, and always throwing amount of coagulating agent is 800mg/L; Add simultaneously coagulant aids polyacrylamide (60mg/L).The photoelectricity oxidation residence time is 2.0 hours, and the second coagulation precipitation adopts ferrous sulfate and calcium hydroxide, and consumption is 1g/L, and 20 minutes coagulation time, sedimentation time is 2 hours, and it is filtrate that filtering unit adopts manganese sand.Final outflow water COD
CrConcentration is 4750mg/L, and ammonia nitrogen concentration is 70mg/L.
Claims (1)
1. treatment process based on the rubbish percolation liquid membrane concentrated solution of a coagulating sedimentation → photoelectricity oxidation → second coagulation precipitation → filtering unit is characterized in that:
A. coagulating sedimentation unit: membrane concentration liquid contains the macromolecule organic pollutant of a large amount of difficult for biological degradation, removes most of this type of material by the coagulating sedimentation unit, guarantees to enter the requirement of photoelectricity oxidation unit influent quality; Coagulating agent adopts the composite of calcium hydroxide, poly-ferric chloride, polymerize aluminum chloride or Tai-Ace S 150 and calcium hydroxide, needs simultaneously to add to help solidifying medicament polyacrylamide, and the throwing amount of coagulating agent is 500-800mg/L, and the throwing amount of polyacrylamide is 10mg/L;
B. photoelectricity oxidation unit: the current density that the photoelectricity oxidation unit applies is at 200-500A/m
2In the scope, the residence time is 1-2 hour, and electrode materials is the steady electrode of shape, and light source is ultraviolet lamp;
C. second coagulation precipitation process unit: add copperas solution in the water outlet of photoelectricity oxidation unit, concentration is 500mg/L, adds simultaneously calcium hydroxide or unslaked lime solution, and concentration is 500mg/L;
D. filtering unit adopts simple sand filtration, removes suspended substance and flco in the water outlet of second coagulation precipitation.
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Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491465B (en) * | 2011-11-25 | 2013-05-22 | 亿利资源集团有限公司 | Flocculant and preparation method thereof |
| CN102786183B (en) * | 2012-03-29 | 2013-06-12 | 波鹰(厦门)科技有限公司 | Method for processing garbage leachate |
| CN102633388A (en) * | 2012-05-03 | 2012-08-15 | 瓮福（集团）有限责任公司 | Reclaimed water reprocessing method |
| CN103232133B (en) * | 2012-06-15 | 2015-08-12 | 北京新创宏力科技发展有限公司 | Composite bio-chemical, be coupled materialization and shift out the sewage treatment process of heavy metal |
| CN105347448A (en) * | 2015-11-20 | 2016-02-24 | 中国城市建设研究院有限公司 | Pretreatment device of refuse landfill leachate membrane concentration evaporation device |
| CN105460987A (en) * | 2015-12-04 | 2016-04-06 | 佛山市中科院环境与安全检测认证中心有限公司 | Medical wastewater treatment agent |
| CN107098441A (en) * | 2017-05-12 | 2017-08-29 | 浙江工业大学 | The method that electrochemistry removes Determination of Total Nitrogen in Waste Water |
| CN109851118A (en) * | 2019-03-07 | 2019-06-07 | 任旭 | The method for removing hardly degraded organic substance in power generation by waste combustion factory percolation liquid membrane concentrate |
| CN110316802A (en) * | 2019-07-05 | 2019-10-11 | 上海电力大学 | A method of processing garbage burning factory percolate nanofiltration concentrate |
| CN111470731B (en) * | 2020-04-26 | 2022-11-25 | 厦门嘉戎技术股份有限公司 | Method and system for treating leachate of refuse landfill |
| CN113548768A (en) * | 2021-07-02 | 2021-10-26 | 北京津工海水科技有限公司 | Deep treatment method for DTRO discharged garbage penetration accumulated liquid |
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| JP2000237772A (en) * | 1999-02-24 | 2000-09-05 | Nippon Steel Corp | Advanced treatment of water |
| CN1792851A (en) * | 2005-11-15 | 2006-06-28 | 中山大学 | Process for treating urban domestic refuse pressing filtering liquid and equipment thereof |
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| CN101041532A (en) * | 2007-02-15 | 2007-09-26 | 三达膜科技（厦门）有限公司 | Printing and dyeing waste water treatment method based on film technology |
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