CN102040301A - 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 any one or compound of two or more of polyaluminium chloride, poly-ferric chloride, aluminum sulphate, ferric sulphate, quicklime and calcium hydroxide, and adding coagulant aid polyacrylamide simultaneously, wherein the CODCr 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 the ammonia nitrogen removal rate is 80%, and the effluent CODCr is about 800-1000 mg/L. The second coagulation-sedimentation is used for removing the rest organic component and metal ion, the effulent CODCr can be reduced to be less than 500 mg/L, the ammonia nitrogen concentrate ion is reduced to 50 mg/L; and finally, the filtering unit is used for filtering flocs and suspended matter having large particle size.
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 domestic extensive employing at present.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.Up to standard fully 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 bigger, has increased membrane pollution problem, and cleaning strength increases the weak point in work-ing life of film.Although nanofiltration and reverse osmosis membrane have splendid rejection to organic pollutant,, cause the water outlet ammonia nitrogen concentration to exceed standard easily to the cutoff performance instability of ammonia nitrogen.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 handled, 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, and a kind of is that concentrated solution is recharged in the landfill yard, and 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, employing method usually has coagulant sedimentation, evaporation mummification method and absorption burning method etc.Wherein evaporate the mummification method to the equipment requirements height, working cost height, operational administrative complexity; The absorption burning method moves more abroad, still to the requirement height of sorbent material, and the common gac bad mechanical strength that adopts, regeneration difficulty.In addition, the Li Aimin of Nanjing University professor and the joint study of German Wei Erli company are the treatment process of core with ion exchange resin, it is reported that water after the processing meets the first discharge standard among the GB16889-97.This method is main processing means with the adsorb organic compound of antipollution resin, 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 handle.
Summary of the invention
The treatment process that the purpose of this invention is to provide membrane concentration liquid in a kind of consumer waste infiltration liquid processing.
Technology disclosed by the invention mainly comprises the coagulating sedimentation pre-treatment, photoelectricity oxide treatment, second coagulation precipitation and filter four unit.Wherein coagulating sedimentation, second coagulation precipitation and be filtered into relative sophisticated treatment technology, we only carry out concise and to the point introduction to it, and the photoelectricity oxidation unit is treated to the core cell of the technology of patent disclosure of the present invention.
The 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, is the bio-refractory 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 polymeric flocculants such as traditional calcium hydroxide, aluminum chloride, iron(ic) chloride and Tai-Ace S 150, needs simultaneously to add to help to coagulate medicament polyacrylamide (PAM).The throwing amount of coagulating agent is about 500-800mg/L, and the throwing amount of PAM is less, is approximately 10mg/L.Through the water of coagulation, by precipitating action flco is precipitated, precipitated outlet water enters next unit and handles then.About about 30%, percent of decolourization is 60% to the clearance of COD greatly in the coagulation process.Most of metal ion in the percolate can be removed in the coagulating sedimentation unit simultaneously.
Photoelectricity oxidation unit:, be mainly the less component of molecular weight through containing remaining dissolved organic matter and ammonia nitrogen in the unitary water outlet of coagulating sedimentation.Photoelectrocatalysis is handled 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, wherein most microorganism of deactivation and germ.Principle and method about photoelectricity oxide treatment percolate are discussed in patent (200810227020) in detail.The residence time of photoelectricity oxide treatment is 2-3 hour, and the current density that is adopted is 200-500A/m
2, electrode materials is a dimensional stable anode, and negative electrode adopts stainless steel or dimensional stable anode, and electrode connection mode is multipole type or acyclic type.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 unitary water outlet of photoelectricity oxide treatment.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 greatly about 500mg/L.Add calcium hydroxide or unslaked lime solution simultaneously, concentration is controlled at 500mg/L.We are used for the oxidation ferrous sulfate with the unnecessary hypochlorous acid in the electrochemistry production process in this process, make it be converted into ferric ion, ferric ion and then hydrolysis generate ferriferous oxide, hypochlorous acid also can generate the oxygenant Losantin with interpolation calcium hydroxide or unslaked lime reaction simultaneously, through precipitation and filtering unit, water outlet COD and ammonia nitrogen can be effectively controlled at last.
Filtering unit: filtering unit is connected on the back of second coagulation water outlet, and filtrate can be traditional filter materials such as manganese sand, quartz sand and flyash.
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 handle certain rubbish percolation liquid membrane and go out concentrated liquid, this landfill yard picks up from Beijing 1 landfill yard.This landfill yard at first adopts anaerobic technique to handle, and adopts aerobic membrane bioreactor to carry out aerobic biochemical then and handles, and bio-chemical effluent is through nanofiltration membrane treatment, and the oxidation water outlet promptly can the water outlet qualified discharge at process absorption/oxidation filtering unit.Concentrated solution water outlet COD
CrConcentration 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 coagulant aids polyacrylamide (20mg/L) simultaneously, 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 COD
CrConcentration is 480mg/L, and ammonia nitrogen concentration is 45mg/L.
Embodiment 2
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 industrial polymerize aluminum chloride as coagulating agent, and consuming amount of concrete is 600mg/L; Add coagulant aids polyacrylamide (20mg/L) simultaneously.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 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 calcium hydroxide as coagulating agent, and consuming amount of concrete is 5g/L; Add coagulant aids polyacrylamide (50mg/L) simultaneously.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 coagulating agent throwing amount always is 800mg/L; Add coagulant aids polyacrylamide (60mg/L) simultaneously.The photoelectricity oxidation residence time is 2.0 hours,, 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 (5)
1. treatment process based on the rubbish percolation liquid membrane concentrated solution of coagulating sedimentation → photoelectricity oxidation → second coagulation precipitation → filtering unit, it is characterized in that: it adopts following steps:
A. coagulating sedimentation unit: contain the macromolecule organic pollutant of a large amount of difficult for biological degradation in the bio-chemical effluent, can remove most of this type of material, guarantee to enter the requirement of photoelectricity oxidation unit influent quality by the coagulating sedimentation unit;
B. photoelectricity oxidation unit: through containing remaining dissolved organic matter and ammonia nitrogen in the unitary water outlet of coagulating sedimentation, the photoelectricity oxidation unit can carry out oxide treatment with remaining dissolved organic matter, simultaneously can oxidation removal overwhelming majority ammonia nitrogen class material, and ammonia nitrogen is converted into nitrogen, guarantee that total nitrogen effectively removes, about the method for fosterization of photoelectricity processing percolate in patent (200810227020) have a detailed description;
C. second coagulation precipitation process unit: will add calcium hydroxide or unslaked lime in the photoelectricity water outlet, and remove most of residue chemical oxygen demand (COD) (COD) and ammonia nitrogen and metal ion, the assurance effluent quality by oxidation, precipitation and filteration.
D. filtering unit adopts simple sand filtration filtration to get final product, and mainly removes the suspended substance and the flco that may contain in the coagulating sedimentation water outlet.
2. the garbage leachate treatment process of a coagulating sedimentation according to claim 1 → photoelectricity oxidation → second coagulation precipitation → filtering unit, it is characterized in that coagulating sedimentation coagulating agent that the unit adopts can be any or several flocculation agents composite in iron(ic) chloride, aluminum chloride, ferric sulfate and the Tai-Ace S 150, consuming amount of concrete is controlled at 300-600mg/L, add the coagulant aids polyacrylamide simultaneously, concentration is 10-20mg/L.
3. the garbage leachate treatment process of amalgamation according to claim 1 time coagulating sedimentation → photoelectricity oxidation → second coagulation precipitation → filtering unit is characterized in that current density that the photoelectricity oxidation unit applied is at 200-500A/m
2In the scope, the residence time is 1.0-2.0 hour, and electrode materials is the steady electrode of shape, and light source is a ultraviolet lamp, sees patent (200810227020) about the specific descriptions of photoelectricity method for oxidation.
4. the garbage leachate treatment process of a coagulating sedimentation according to claim 1 → photoelectricity oxidation → second coagulation precipitation → filtering unit, it is characterized in that the oxidation precipitation unit can remaining solvability COD of the efficient oxidation and ammonia nitrogen, and pass through precipitating action, organism after the oxidation is precipitated, reduce COD and ammonia nitrogen and metal ion content.
5. the rubbish percolation liquid membrane concentrated solution treatment process based on a coagulating sedimentation → photoelectricity oxidation → second coagulation precipitation → filtering unit can effectively be handled the percolation liquid membrane concentrated solution, makes COD
CrBe reduced to 500mg/L, ammonia nitrogen concentration is reduced to 50mg/L.
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| CN102491465A (en) * | 2011-11-25 | 2012-06-13 | 亿利资源集团有限公司 | Flocculant and preparation method thereof |
| CN102633388A (en) * | 2012-05-03 | 2012-08-15 | 瓮福（集团）有限责任公司 | Reclaimed water reprocessing method |
| CN102786183A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Method for processing garbage leachate |
| CN103232133A (en) * | 2012-06-15 | 2013-08-07 | 北京新创宏力科技发展有限公司 | Composite biochemical, coupled physicochemical, and heavy-metal-removing sewage treatment process and technology |
| 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 |
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| 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 |
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| CN102786183A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Method for processing garbage leachate |
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| CN102633388A (en) * | 2012-05-03 | 2012-08-15 | 瓮福（集团）有限责任公司 | Reclaimed water reprocessing method |
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| 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 |
| CN111470731A (en) * | 2020-04-26 | 2020-07-31 | 厦门嘉戎技术股份有限公司 | Method and system for treating leachate of refuse landfill |
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