CN106242163B - A kind of processing method of percolate embrane method concentrate - Google Patents

A kind of processing method of percolate embrane method concentrate Download PDF

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CN106242163B
CN106242163B CN201610689058.0A CN201610689058A CN106242163B CN 106242163 B CN106242163 B CN 106242163B CN 201610689058 A CN201610689058 A CN 201610689058A CN 106242163 B CN106242163 B CN 106242163B
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percolate
concentrate
embrane method
tank
pond
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CN106242163A (en
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吴海锁
陆继来
谢祥峰
管苏
李月中
田爱军
吴剑
程伟
朱卫兵
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Jiangsu Environmental Protection Industry Technology Research Institute Co Ltd
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    • 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
    • C02F1/442Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • 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
    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • 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
    • C02F1/72Treatment of water, waste water, or sewage by oxidation
    • C02F1/78Treatment of water, waste water, or sewage by oxidation with ozone
    • 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
    • C02F3/28Anaerobic digestion processes
    • 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
    • C02F3/28Anaerobic digestion processes
    • C02F3/2853Anaerobic digestion processes using anaerobic membrane bioreactors

Abstract

The invention discloses a kind of processing method of percolate embrane method concentrate, percolate embrane method concentrate enters nanofiltration system by compound softening coagulative precipitation tank, ozone oxidation reaction device, hydrolytic tank and anaerobism MBR ponds, anaerobism MBR pond water outlets successively;The permeate that nanofiltration system handles to obtain directly is discharged or discharged after more medium filter filters after pressure contact oxidation reactor for treatment;The concentrate that nanofiltration system handles to obtain mixes with percolate, and the concentrate obtained after biochemistry, MBR, embrane method concentration is re-circulated into compound softening coagulative precipitation tank and subsequent operation.The present invention is applicable not only to the processing of percolate film-filter concentration liquid, while is also applied for other film concentrates containing higher hardly degraded organic substance concentration and handles.

Description

A kind of processing method of percolate embrane method concentrate
Technical field
The present invention relates to method for treating garbage percolation liquid, specifically, is related to one kind and passes through reverse osmosis for percolate The method that permeable membrane, NF membrane or concentrate caused by other filtering embrane method processing are handled.
Background technology
Country promulgates within 2008《Household refuse landfill sites contamination control standard》(GB16889-2008), to garbage filter The processing of liquid proposes higher requirement, nowadays handles percolate and uses NF, RO membrane treatment process more.Rubbish percolation liquid membrane Filter concentration liquid is the raffinate that percolate retains after biodegradation through NF films (or RO films), typically without biochemical Property, Main Ingredients and Appearance is humus material, and in brownish black, COD is very high, and contains substantial amounts of inorganic ions, and TDS is 20000 Between~60000mg/L, generally between 1000~5000mg/L, ammonia nitrogen concentration is COD in 100~1000mg/L, electrical conductivity 40000~50000us/cm.
The volume of film-filter concentration liquid accounts for the 20%~30% of percolate stoste volume.Because concentrate contains various difficulties The organic and inorganic pollution of degraded, directly discharge may pollute to generations such as soil, surface water, oceans;If it is discharged into municipal administration Sewage disposal system, growth of the too high total dissolved solid to activated sludge are also unfavorable.Therefore for the production of reduction concentrate The research that amount, concentrate continue with is necessary.
Main processing method is used to have at present:Recharge, evaporation drying, solidification, burning etc..By embrane method Concentrated liquid recharge To refuse landfill, garbage storing hole or percolate storage pool, long-term circulation can cause the tired of salt and organic matter in percolate Product, so as to cause biochemical treatment system effect to be deteriorated, increase the burden and expense of embrane method system operation.It is by embrane method to evaporate drying Soluble solids is separated from water in concentrate, requires high to evaporator corrosion resistance, and energy consumption is big, and operating cost is higher.This Outside, the partial organic substances in embrane method concentrate are volatile, and evaporation process, which is dealt with improperly, easily causes secondary pollution.Curing process is profit Sludge carries out curing process to embrane method concentrate caused by flying dust or sewage disposal, then transports the residue of desiccation to rubbish Landfill yard carries out innoxious landfill.Because the garbage disposal after solidification causes processing cost to increase, to the processing of embrane method concentrate During need to account for reference to soot actual conditions and economic analysis.High-level oxidation technology is current processing garbage filter The proper treatment technology of concentrated liquor, the speed of high-level oxidation technology degradation of organic substances is very fast, such as O3/ UV systems and O3/ H2O2System oxidation degradation process, and the intermediate product in oxidizing process can continue same hydroxyl radical reaction, until last Carbon dioxide and water are oxidized to completely.
But because rubbish percolation liquid membrane concentrate pollutant concentration is too high, if using single chemical oxidization method, its Operating cost is too high.If using the relatively low biological treatment of operating cost, the biodegradability of pollutant is again very low.If adopt It is difficult to solve again with membrane treatment process, the problem of fouling membrane.Therefore, percolate embrane method concentrate is badly in need of one kind simply at present Effectively, the deep treatment method for the embrane method concentrate that energy consumption is low, operating cost is low.
The content of the invention
In order to overcome the shortcomings of above-mentioned percolate embrane method concentrate processing method, the present invention provides a kind of garbage filter The processing method of liquid-film method concentrate, make the treatment effect of embrane method concentrate reliable and stable, have relatively low operating cost and compared with High removal efficiency, water outlet can realize qualified discharge.
The core thinking of the present invention is to be directed to high salt water quality, using the biodegradability of kinds of processes lifting waste water, and is passed through UF membrane realizes the separation of divalent salts, monovalent salt and organic matter, so as to solve the problems, such as the accumulation of salt, and greatly improves waste water Biodegradability, percolate (not being concentrate) preceding road biochemical treatment process is made full use of to be acted upon biochemical waste water. Solves Denitrogenation using anaerobism MBR simultaneously.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows:
A kind of processing method of percolate embrane method concentrate, percolate embrane method concentrate is successively by compound soft Change coagulative precipitation tank, ozone oxidation reaction device, hydrolytic tank and anaerobism MBR ponds, anaerobism MBR pond water outlets and enter nanofiltration system;
Be situated between directly is discharged or passed through to the permeate that nanofiltration system handles to obtain more after pressure contact oxidation reactor for treatment Discharged after mass filter filtering;
The concentrate that nanofiltration system handles to obtain mixes with percolate returns to pre-treatment biochemistry section, through biochemistry, MBR, The concentrate obtained after embrane method concentration is re-circulated into compound softening coagulative precipitation tank and subsequent operation.
Wherein, described percolate embrane method concentrate is will to pass through reverse osmosis membrane or NF membrane to percolate Or caused concentrate after other filtering embrane method processing.
Wherein, described percolate embrane method concentrate, Main Ingredients and Appearance are humus material, TDS is 20000~ 60000mg/L, COD are 1000~5000mg/L, and ammonia nitrogen concentration is 100~1000mg/L, and TN concentration is 500~2500, conductance Rate is 40000~50000us/cm.
Wherein, described compound softening coagulative precipitation tank, is made up of reaction of high order pond and sedimentation basin;Waste water is first by more Order reaction pond, sedimentation basin precipitation is then entered back into, reaction tank water outlet precipitates into sedimentation basin, reduces hardness and the removal of waste water COD.Wherein, described reaction of high order pond is 3~4 grades, and reaction tanks at different levels are all provided with dynamic agitating device or carry out hydraulic mixing; Alkaline matter is added in 1~2 order reaction pond of beginning;Reaction tank is added containing aluminium or iron content coagulation in first order reaction pond behind Agent, final stage reaction tank add polyacrylamide high polymer coagulant.Wherein, described alkaline matter is sodium carbonate, sodium hydroxide With any one or a few the mixture in calcium hydroxide, described alkaline matter adds total mole number as calcium and magnesium in waste water 0.5~3 times of ion total mole number;It is described containing aluminium or iron content coagulant be aluminum sulfate, aluminium chloride, ferric sulfate, iron chloride or The polymer of any of the above-described material, the dosage containing aluminium or iron content coagulant are 40~2000mg/L;Described poly- third The dosage of acrylamide high polymer coagulant is calculated as 1~10mg/L in mass ratio.Waste water is in compound softening coagulative precipitation tank Total residence time is 2~10h.
Wherein, described ozone oxidation reaction device, including ozone generator and reactor, ozone generator are placed in reactor Interior, ozone generator is the COD of air source ozone generator or oxygen source ozone generator, ozone dosage and handled water The ratio between be 0.1~1:1.Retention time of sewage control in ozone oxidation reaction device is 0.3~2h.Ozone oxidation reaction device tank body It can be made up of metal or nonmetallic materials, can also use civil engineering structure.
Wherein, described hydrolytic tank and anaerobism MBR ponds are built jointly or built with anaerobism MBR ponds point.
Wherein, total residence time of the waste water in hydrolytic tank is 4~20h.
Wherein, described anaerobism MBR ponds, including anaerobic pond and MBR module two parts;Anaerobic pond is anti-using up-flow anaerobism Answer device;MBR module uses built-in hyperfiltration membrane assembly or external hyperfiltration membrane assembly.Total stop of the waste water in anaerobism MBR ponds Time is 10~60h.
Wherein, described pressure contact oxidation reactor is closed tank, intakes by jet-flow aeration mode, carries dissolving Oxygen enters tank body, and tank interior filling biologic packing material, reactor inner air pressure is 0.2~0.8MPa;Wherein, described biology Filler, including granular activated carbon, coke, anthracite, haydite and soft, semi soft packing and floating stuffing any one or Several mixtures.
Wherein, the nanofiltration membrane component that described nanofiltration system uses has selective through performance, to divalence or more at high price State metal ion has good rejection effect.
The inventive method is applicable not only to the processing of percolate film-filter concentration liquid, while is also applied for other containing higher The film concentrate processing of hardly degraded organic substance concentration.
Beneficial effect:The present invention has advantages below compared with prior art:
1) effectively advanced oxidation processing and anaerobic bio-treated are combined, reduce processing cost to greatest extent and carry High treatment efficiency.Ozone oxidation is remarkably improved the biodegradability of waste water.Simultaneously as the presence of follow-up Anaerobic Treatment so that One-level ozone oxidation concentrates the Recalcitrant chemicals in liquid without exhaustive oxidation percolate, and only needs to destroy pollutant knot Structure, improve pollutant biodegradability.Therefore ozone dosage is reduced to greatest extent.
2) biochemical processing process that the present invention selects is anaerobic membrane bioreactor.Anaerobic reactor is divided into hydrolysis section and detested Oxygen section.Anaerobism and hydrolytic process play the role of uniqueness to hardly degraded organic substance processing, not only can directly reduce COD, may be used also By the open loop of macromolecular hardly degraded organic substance and chain rupture, to become small molecule labile organic compound, so as to improve treatment effect, and it is good Oxygen handling process does not possess this function then.Therefore, for compared to aerobic MBR, anaerobism MBR concentrates liquid for percolate Treatment effeciency is higher.
3) organic nitrogen in percolate and ammonia-nitrogen content are very high, contain substantial amounts of nitre in waste water after biochemistry pre-processes Hydrochlorate, denitrogenation are very difficult, it is difficult to reach discharge standard.Aerobic MBR is low to the removal efficiency of nitrate nitrogen, and this project uses Anaerobism MBR has fabulous denitrification efficiency, can not only be carried out using small organic molecule caused by ozone oxidation as carbon source Denitrogenation, Anammox reaction denitrogenation can also occur with remaining ammonia nitrogen under anaerobic, the total of concentrate can be significantly reduced It is nitrogen discharged.
4) present invention pretreatment uses complex coagulation depositing technology, hardness and calcium ions and magnesium ions can be being removed, in waste water Organic matter also have significant removal effect.The organic loading of Anaerobic Treatment can be greatly reduced, while prevent anaerobism MBR productions Raw inorganic matter fouling membrane.
5) invention post processing uses nanofiltration and pressure contact oxidation combination of reactors technique.Nanofiltration technique can further drop Organic matter in low waste water, it is ensured that stable water outlet is up to standard.Meanwhile in order to which the salt content in reduction system, this project select nanofiltration As post processing secondary filter.Nanofiltration has preferable permeability to monovalent ion, and secondary filter is carried out not using nanofiltration technique The salt content of concentrate can be significantly improved, so that the salinity of biochemical system keeps stable.
6) in order to further lift the effect of water outlet, the end of handling process is provided with pressure contact oxidation reactor, entered One step improves effluent quality.Because the organic matter in NF membrane permeate is small molecule, biodegradability is good.In pressure contact oxygen Change in reactor, high pressure is formed by intake pump, the transport resistance of oxygen reduces under high pressure, and oxygen is to microorganism in mixed liquor air The efficiency of transfer greatly enhances, and can improve the activated sludge concentration in reactor, makes in reactor that biomembrane character is fluffy, is not easy Conglomeration, activity are remarkably reinforced.Be advantageous to the propagation of active sludge microorganism and the degraded of organic matter.So as to ensure aqueous concentration very It is low.Filter layer is provided with inside pressure contact oxidation device, stable effluent quality is secure.
Brief description of the drawings
Fig. 1 is the process route chart that percolate embrane method concentrate obtains.
Fig. 2 is the flow chart of handling process of the present invention.
Embodiment
According to following embodiments, the present invention may be better understood.It is however, as it will be easily appreciated by one skilled in the art that real Apply the content described by example and be merely to illustrate the present invention, without should be also without limitation on sheet described in detail in claims Invention.
Embodiment 1:
Typical percolate processing and nanofiltration, reverse osmosis concentrated liquid produce process and see Fig. 1.Percolate pre-processes through grid System enters regulating reservoir, and subsequently into UBF anaerobic systems, anaerobic effluent enters intermediate pool, and intermediate pool water outlet sequentially enters instead Nitrification tank and two sections of aerobic nitrification ponds.Nitrification tank water outlet enters tubular ultra-filtration membrane system.Ultrafiltration dope is back to denitrification pond.It is super Cleaner liquid squeezes into nanofiltration system again after entering Clear liquid tank, and producing nanofiltration concentrate and clear liquid, nanofiltration clear liquid can directly discharge, or Counter-infiltration system is squeezed into again after the collection of nanofiltration Clear liquid tank, produces reverse osmosis concentrated liquid and counter-infiltration clear liquid.
In the process, dope caused by nanofiltration and counter-infiltration is caused film concentration during landfill leachate treatment Liquid.
Embodiment 2:
The rubbish percolation liquid membrane concentrate that embodiment 1 obtains is first passed around into compound softening coagulative precipitation tank, compound softening Coagulative precipitation tank is made up of 3 order reaction ponds and sedimentation basin, and the 1st order reaction pond adds sodium carbonate, and sodium carbonate adds total mole number For 1 times of calcium ions and magnesium ions total mole number in waste water, the 2nd order reaction pond adds 200mg/L aluminium polychlorides, and 3rd level reaction tank is thrown Add 2mg/L polyacrylamides high polymer coagulant PAM, total reaction time 30min, precipitated subsequently into sedimentation basin, reduced useless The hardness of water simultaneously removes COD, and total residence time of the waste water in compound softening coagulative precipitation tank is 3h.
Sedimentation basin water outlet is handled into ozone oxidation reaction device, described ozone oxidation reaction device, including ozone hair Raw device and reactor, ozone generator are placed in reactor, and ozone generator uses oxygen source ozone generator, ozone dosage It is 0.5 with the ratio between the handled COD of water:1, reaction time 1.5h.
Ozone oxidation reaction device water outlet enters back into compound pond, and compound pond is divided into 2 grades, and one-level is hydrolytic tank, and two level is anaerobism MBR ponds, total residence time of the waste water in hydrolytic tank are 12h.Described anaerobism MBR ponds, including anaerobic pond and MBR module two Point;Anaerobic pond uses up-flow anaerobic reactor;MBR module uses external hyperfiltration membrane assembly.Waste water is in anaerobism MBR ponds Total residence time is 24h.
Anaerobism MBR pond water outlets initially enter after intermediate pool collects, then squeeze into nanofiltration system by pump, nanofiltration permeate liquid by Jet is pumped to pressure contact oxidation reactor, and pressure contact oxidation reactor control pressure is 0.45MPa, and built-in plastics suspend Filler and ceramic grain filter, pressure contact oxidation reactor water outlet are directly discharged.Nanofiltration concentrate is mixed with percolate and returned to Pre-treatment biochemistry section, the concentrate obtained after biochemistry, MBR, embrane method concentration are re-circulated into compound softening coagulating sedimentation Pond and subsequent operation.The clean-up effect of whole system such as table 1.
The clean-up effect of 1 embodiment of table 1
Embodiment 3:
The rubbish percolation liquid membrane concentrate that embodiment 1 obtains is first passed around into compound softening coagulative precipitation tank, compound softening Coagulative precipitation tank is made up of 4 order reaction ponds and sedimentation basin, and the 1st~2 order reaction pond adds sodium hydroxide, and adding for sodium hydroxide is total Molal quantity is 0.8 times of calcium ions and magnesium ions total mole number in waste water, and the 2nd order reaction pond adds 500mg/L bodied ferric sulfates, 3rd level Reaction tank adds 2mg/L polyacrylamide high polymer coagulant PAM, total reaction time 60min, is sunk subsequently into sedimentation basin Form sediment, reduce the hardness of waste water and remove COD, total residence time of the waste water in compound softening coagulative precipitation tank is 5h.
Sedimentation basin water outlet is handled into ozone oxidation reaction device, described ozone oxidation reaction device, including ozone hair Raw device and reactor, ozone generator are placed in reactor, and ozone generator uses oxygen source ozone generator, ozone dosage It is 1 with the ratio between the handled COD of water:1, reaction time 1h.
Ozone oxidation reaction device water outlet enters back into compound pond, and compound pond is divided into 2 grades, and one-level is hydrolytic tank, and two level is anaerobism MBR ponds, total residence time of the waste water in hydrolytic tank are 8h.Described anaerobism MBR ponds, including anaerobic pond and MBR module two Point;Anaerobic pond uses up-flow anaerobic reactor;MBR module uses built-in flat-plate ultrafiltration membrane component, and is produced using anaerobism Gas inner circulating aerating stirs, and blower fan uses stainless steel blower fan.Total residence time of the waste water in anaerobism MBR ponds is 16h.
Anaerobism MBR pond water outlets initially enter after intermediate pool collects, then squeeze into nanofiltration system by pump, nanofiltration permeate liquid by Jet is pumped to pressure contact oxidation reactor and carries out biological cleaning, and pressure contact oxidation reactor control pressure is 0.8MPa, Built-in plastics floating stuffing and activated carbon, the water outlet of pressure contact oxidation reactor are discharged after more medium filter filters again. Nanofiltration concentrate mixes with percolate returns to pre-treatment biochemistry section, is obtained after biochemistry, MBR, embrane method concentration dense Contracting liquid is re-circulated into compound softening coagulative precipitation tank and subsequent operation.The clean-up effect of whole system such as table 2.
The clean-up effect of 2 embodiment of table 2

Claims (6)

1. a kind of processing method of percolate embrane method concentrate, it is characterised in that percolate embrane method concentrate is successively Enter nanofiltration by compound softening coagulative precipitation tank, ozone oxidation reaction device, hydrolytic tank and anaerobism MBR ponds, anaerobism MBR pond water outlets System;
The permeate that nanofiltration system handles to obtain directly is discharged or through multimedium mistake after pressure contact oxidation reactor for treatment Discharged after filter filtering;
The concentrate that nanofiltration system handles to obtain mixes with percolate, is obtained after biochemistry, MBR, embrane method concentration Concentrate is re-circulated into compound softening coagulative precipitation tank and subsequent operation;
Described pressure contact oxidation reactor is closed tank, is intake by jet-flow aeration mode, carries dissolved oxygen and enters tank Body, tank interior filling biologic packing material, reactor inner air pressure is 0.2~0.8MPa;Wherein, described biologic packing material, bag Include granular activated carbon, coke, anthracite, haydite and any one or a few of soft, semi soft packing and floating stuffing Mixture;
Described compound softening coagulative precipitation tank, is made up of reaction of high order pond and sedimentation basin;Waste water first by reaction of high order pond, Then sedimentation basin precipitation is entered back into;
Described reaction of high order pond is 3~4 grades, and reaction tanks at different levels are all provided with dynamic agitating device or carry out hydraulic mixing;Opening 1~2 order reaction pond begun adds alkaline matter;Reaction tank is added containing aluminium or iron content coagulant in first order reaction pond behind, Final stage reaction tank adds polyacrylamide high polymer coagulant;
Described alkaline matter is sodium carbonate, and described alkaline matter adds total mole number as calcium ions and magnesium ions total moles in waste water Several 0.5~3 times;Described is aluminum sulfate, aluminium chloride, ferric sulfate, iron chloride or any of the above-described thing containing aluminium or iron content coagulant The polymer of matter, the dosage containing aluminium or iron content coagulant are 40~2000mg/L;Described polyacrylamide high score The dosage of sub- flocculant is 1~10mg/L.
2. the processing method of percolate embrane method concentrate according to claim 1, it is characterised in that described rubbish Percolate embrane method concentrate is that percolate will be produced after reverse osmosis membrane or NF membrane or other filtering embrane method processing Raw concentrate.
3. the processing method of percolate embrane method concentrate according to claim 1 or 2, it is characterised in that described Percolate embrane method concentrate, Main Ingredients and Appearance are humus material, and TDS is 20000~60000mg/L, COD is 1000~ 5000mg/L, ammonia nitrogen concentration are 100~1000mg/L, and TN concentration is 500~2500, and electrical conductivity is 40000~50000us/cm.
4. the processing method of percolate embrane method concentrate according to claim 1, it is characterised in that described ozone Oxidation reactor, including ozone generator and reactor, ozone generator are placed in reactor, and ozone generator is that air-source is smelly Oxygen Generator or oxygen source ozone generator, the ratio between ozone dosage and the handled COD of water are 0.1~1: 1.
5. the processing method of percolate embrane method concentrate according to claim 1, it is characterised in that described hydrolysis Pond and anaerobism MBR ponds are built jointly or built with anaerobism MBR ponds point.
6. the processing method of percolate embrane method concentrate according to claim 1, it is characterised in that described anaerobism MBR ponds, including anaerobic pond and MBR module two parts;Anaerobic pond uses up-flow anaerobic reactor;MBR module is using built-in Hyperfiltration membrane assembly or external hyperfiltration membrane assembly.
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CN105645662B (en) * 2014-11-14 2018-12-25 中国石油天然气股份有限公司 The removing means and removal methods of hardly degraded organic substance in film-filter concentration liquid

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