CN106242163A - A kind of processing method of percolate embrane method concentrated solution - Google Patents
A kind of processing method of percolate embrane method concentrated solution Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
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Abstract
The invention discloses the processing method of a kind of percolate embrane method concentrated solution, percolate embrane method concentrated solution sequentially passes through compound coagulative precipitation tank, ozone oxidation reaction device, hydrolytic tank and the anaerobism MBR pond of softening, anaerobism MBR pond water outlet entrance nanofiltration system；The permeate that nanofiltration system process obtains, after pressure contact oxidation reactor for treatment, directly discharges or discharges after more medium filter filters；Nanofiltration system processes the concentrated solution obtained and mixes with percolate, and the concentrated solution 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 process of percolate film-filter concentration liquid, is simultaneously applicable to other membrance concentration liquid containing higher hardly degraded organic substance concentration and processes.
Description
Technical field
The present invention relates to method for treating garbage percolation liquid, specifically, relate to one for percolate through reverse osmosis
Permeable membrane, NF membrane or other filtration embrane method process the method that produced concentrated solution carries out processing.
Background technology
Within 2008, country has promulgated " household refuse landfill sites Environmental capacity standard " (GB16889-2008), to garbage filter
The process of liquid is had higher requirement, and nowadays processes percolate many employings NF, RO membrane treatment process.Rubbish percolation liquid membrane
Filter concentration liquid is the residual liquid that percolate retains through NF film (or RO film) after biodegradation, and the most not having can be biochemical
Property, Main Ingredients and Appearance is Humus material, and in brownish black, COD is the highest, and containing substantial amounts of inorganic ions, TDS is 20000
～between 60000mg/L, COD is generally between 1000～5000mg/L, and ammonia nitrogen concentration is 100～1000mg/L, and electrical conductivity is
40000～50000us/cm.
The volume of film-filter concentration liquid accounts for the 20%～30% of percolate stock solution volume.Owing to concentrated solution contains various difficulty
Organic and the inorganic pollution of degraded, directly soil, surface water, ocean etc. may be produced and pollute by discharge；If entering municipal administration
Sewage disposal system, too high total dissolved solid is the most unfavorable to the growth of activated sludge.Therefore for reducing the product of concentrated solution
The research that amount, concentrated solution continue with is necessary.
Used main processing method to have at present: recharge, evaporate drying, solidify, burning etc..By embrane method Concentrated liquid recharge
To refuse landfill, garbage storing hole or percolate storage pool, long-term circulation can cause in percolate salt and organic tired
Long-pending, thus cause biochemical treatment system effect to be deteriorated, increase burden and expense that embrane method system is run.Evaporation drying is by embrane method
In concentrated solution, soluble solids is separated from water, and vaporizer corrosion resistance requires height, and energy consumption is big, and operating cost is higher.This
Outward, the partial organic substances in embrane method concentrated solution is volatile, and evaporation process is dealt with improperly and easily caused secondary pollution.Cured is profit
The mud produced with flying dust or sewage disposal carries out cured to embrane method concentrated solution, then transports the residue of mummification to rubbish
Landfill yard carries out innoxious landfill.Owing to the garbage disposal after solidification makes processing cost strengthen, embrane method concentrated solution is being processed
During need to combine soot practical situation and account for and economic analysis.High-level oxidation technology is to process garbage filter at present
The treatment technology that concentrated liquor is proper, the speed of high-level oxidation technology degradation of organic substances is very fast, such as O3/ UV system and O3/
H2O2System oxidation degradation process, and the intermediate product in oxidizing process all can continue same hydroxyl radical reaction, until finally
It is oxidized to carbon dioxide and water completely.
But, owing to rubbish percolation liquid membrane concentrated solution pollutant levels are too high, if using single chemical oxidization method, its
Operating cost is the highest.If using the biological treatment that operating cost is relatively low, the biodegradability of pollutant is the lowest.If adopted
With membrane treatment process, the problem of fouling membrane is difficult to again solve.Therefore, current percolate embrane method concentrated solution is badly in need of a kind of simple
The deep treatment method of the embrane method concentrated solution that effectively, energy consumption is low, operating cost is low.
Summary of the invention
In order to overcome the deficiency of above-mentioned percolate embrane method concentrated solution processing method, the present invention provides a kind of garbage filter
The processing method of liquid-film method concentrated solution, the treatment effect making embrane method concentrated solution is reliable and stable, has relatively low operating cost and relatively
High removal efficiency, water outlet is capable of qualified discharge.
The core thinking of the present invention is for high salt water quality, uses the biodegradability of kinds of processes lifting waste water, and passes through
Membrance separation realizes divalent salts, monovalent salt and organic separation, thus solves the accumulation problem of salt, and improves waste water greatly
Biodegradability, can make full use of percolate (not being concentrated solution) front road biochemistry processing procedure and is acted upon by biochemical waste water.
Utilize anaerobism MBR to solve Denitrogenation simultaneously.
For solving above-mentioned technical problem, the technical solution used in the present invention is as follows:
The processing method of a kind of percolate embrane method concentrated solution, percolate embrane method concentrated solution sequentially passes through compound soft
Changing coagulative precipitation tank, ozone oxidation reaction device, hydrolytic tank and anaerobism MBR pond, the water outlet of anaerobism MBR pond enters nanofiltration system；
The permeate that nanofiltration system process obtains is after pressure contact oxidation reactor for treatment, and directly discharge or warp are situated between more
Mass filter discharges after filtering；
Nanofiltration system processes the concentrated solution that obtains and mixes with percolate and return to pre-treatment biochemistry section, through biochemistry, MBR,
The concentrated solution obtained after embrane method concentration is re-circulated into compound softening coagulative precipitation tank and subsequent operation.
Wherein, described percolate embrane method concentrated solution be by percolate through reverse osmosis membrane or NF membrane
Or other filters produced concentrated solution after embrane method processes.
Wherein, described percolate embrane method concentrated solution, Main Ingredients and Appearance is Humus material, TDS be 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, it is made up of reaction of high order pond and sedimentation tank；Waste water first passes through many
Order reaction pond, then enters back into sedimentation tank precipitation, and reaction tank water outlet enters sedimentation tank precipitation, reduces useless hardness of water and removes
COD.Wherein, described reaction of high order pond is 3～4 grades, and reaction tanks at different levels are equipped with power agitating device or carry out hydraulic mixing；
Alkaline matter is added in the 1～2 order reaction ponds started；In first order reaction pond behind, reaction tank adds containing aluminum or iron content coagulation
Agent, final stage reaction tank adds polyacrylamide high polymer coagulant.Wherein, described alkaline matter is sodium carbonate, sodium hydroxide
With any one or a few the mixture in calcium hydroxide, the total mole number that adds of described alkaline matter is calcium and magnesium in waste water
0.5～3 times of ion total mole number；Described containing aluminum or iron content coagulant be aluminum sulfate, aluminum chloride, iron sulfate, iron chloride or
The polymer of any of the above-described material, the described dosage containing aluminum or iron content coagulant is 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 ozonator and reactor, ozonator is placed in reactor
In, ozonator is air source ozone generator or oxygen source ozone generator, ozone dosage and the COD of handled water
Ratio be 0.1～1:1.It is 0.3～2h that retention time of sewage in ozone oxidation reaction device controls.Ozone oxidation reaction device tank body
Can be metal or nonmetallic materials are made, it is possible to use civil engineering structure.
Wherein, described hydrolytic tank and anaerobism MBR pond are built jointly or are divided with anaerobism MBR pond and build.
Wherein, waste water total residence time in hydrolytic tank is 4～20h.
Wherein, described anaerobism MBR pond, including anaerobic pond and MBR module two parts；Anaerobic pond uses up-flow anaerobism anti-
Answer device；MBR module uses built-in hyperfiltration membrane assembly or external hyperfiltration membrane assembly.The waste water total stop in anaerobism MBR pond
Time is 10～60h.
Wherein, described pressure contact oxidation reactor is closed tank, and water inlet, by jet-flow aeration mode, carries dissolving
Oxygen enters tank body, and tank interior fills biologic packing material, and reactor inner air pressure is 0.2～0.8MPa；Wherein, described biology
Filler, including granular active carbon, coke, anthracite, haydite and soft, semi soft packing and floating stuffing any one or
Several mixture.
Wherein, the NF membrane element that described nanofiltration system uses has selectivity through performance, to bivalence or more high price
State metal ion has good rejection effect.
The inventive method is applicable not only to the process of percolate film-filter concentration liquid, is simultaneously applicable to other containing higher
The membrance concentration liquid of hardly degraded organic substance concentration processes.
Beneficial effect: the present invention compared with prior art has the advantage that
1) effectively advanced oxidation is processed and anaerobic bio-treated combines, reduce processing cost to greatest extent and carry
High treatment efficiency.Ozone oxidation is remarkably improved the biodegradability of waste water.Simultaneously as the existence of follow-up anaerobic treatment so that
One-level ozone oxidation concentrates the Recalcitrant chemicals in liquid without exhaustive oxidation percolate, and has only to destroy pollutant knot
Structure, improves pollutant biodegradability.Reduce ozone dosage the most to greatest extent.
2) biochemical processing process that the present invention selects is anaerobic membrane bioreactor.Anaerobic reactor is divided into hydrolysis section and detests
Oxygen section.Hardly degraded organic substance is processed by anaerobism and hydrolytic process the effect of uniqueness, is possible not only to directly reduce COD, also may be used
With by macromole hardly degraded organic substance open loop and chain rupture, become little molecule labile organic compound, thus improve treatment effect, and good
Oxygen processes technique and does not the most possess this function.Therefore, for comparing aerobic MBR, anaerobism MBR concentrates liquid for percolate
Treatment effeciency is higher.
3) organic nitrogen in percolate and ammonia-nitrogen content are the highest, containing substantial amounts of nitre in waste water after biochemical pretreatment
Hydrochlorate, denitrogenation is the most 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, and the small organic molecule that ozone oxidation can not only be utilized to produce is carried out as carbon source
Denitrogenation, also under anaerobic can react denitrogenation with residue ammonia nitrogen generation Anammox, it is possible to significantly reduce the total of concentrated solution
Nitrogen discharged.
4) pretreatment of the present invention uses complex coagulation depositing technology, can remove hardness and calcium ions and magnesium ions, in waste water
Organic substance also have significant removal effect.Can reduce the organic loading of anaerobic treatment greatly, prevention anaerobism MBR is produced simultaneously
Raw inorganic matter fouling membrane.
5) invention post processing uses nanofiltration and pressure contact oxidation combination of reactors technique.Nanofiltration technique can drop further
Organic substance in low waste water, it is ensured that stable water outlet is up to standard.Meanwhile, for the salinity in minimizing system, this project selects nanofiltration
As post processing secondary filter.Nanofiltration has preferable permeability to monovalent ion, uses nanofiltration technique to carry out secondary filter not
The salinity of concentrated solution can be significantly improved, so that the salinity of biochemical system keeps stable.
6) in order to promote the effect of water outlet further, the end processing technique is provided with pressure contact oxidation reactor, enters
One step improves effluent quality.Owing to the Organic substance in NF membrane permeate is little molecule, biodegradability is good.At pressure contact oxygen
Changing in reactor, form high pressure by intake pump, under high pressure the transport resistance of oxygen reduces, and in mixed liquor air, oxygen is to microorganism
The efficiency of transfer is greatly enhanced, and can improve the activated sludge concentration in reactor, and in making reactor, biomembrane character is fluffy, is difficult to
Conglomeration, activity is remarkably reinforced.Be conducive to the propagation of active sludge microorganism and organic degraded.Thus ensure that aqueous concentration is very
Low.Being provided with filter course inside pressure contact oxidation device, stable effluent quality is secure.
Accompanying drawing explanation
Fig. 1 is the process route chart that percolate embrane method concentrated solution obtains.
Fig. 2 is the flow chart that the present invention processes technique.
Detailed description of the invention
According to following embodiment, the present invention be may be better understood.But, as it will be easily appreciated by one skilled in the art that reality
Execute the content described by example and be merely to illustrate the present invention, and should be also without limitation on basis described in detail in claims
Invention.
Embodiment 1:
Typical percolate processes and nanofiltration, reverse osmosis concentrated liquid produce process and see Fig. 1.Percolate is through grid pretreatment system
System enters regulating reservoir, and subsequently into UBF anaerobic system, 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.Super
Cleaner liquid squeezes into nanofiltration system again after entering Clear liquid tank, produce nanofiltration concentrated solution and clear liquid, and nanofiltration clear liquid can directly discharge, or
After nanofiltration Clear liquid tank is collected, squeeze into counter-infiltration system again, produce reverse osmosis concentrated liquid and reverse osmosis clear liquid.
In the process, the membrance concentration that the dope that nanofiltration and reverse osmosis produce produces during being landfill leachate treatment
Liquid.
Embodiment 2:
Rubbish percolation liquid membrane concentrated solution embodiment 1 obtained first passes around the compound coagulative precipitation tank that softens, compound softening
Coagulative precipitation tank is made up of 3 order reaction ponds and sedimentation tank, and the 1st order reaction pond adds sodium carbonate, sodium carbonate add total mole number
For in waste water 1 times of calcium ions and magnesium ions total mole number, the 2nd order reaction pond adds 200mg/L aluminium polychlorid, and 3rd level reaction tank is thrown
Adding 2mg/L polyacrylamide high polymer coagulant PAM, total reaction time is 30min, precipitates subsequently into sedimentation tank, reduces useless
Hardness of water also removes COD, and waste water total residence time in compound softening coagulative precipitation tank is 3h.
Sedimentation tank water outlet enters ozone oxidation reaction device and processes, and described ozone oxidation reaction device is sent out including ozone
Raw device and reactor, ozonator is placed in reactor, and ozonator uses oxygen source ozone generator, ozone dosage
Being 0.5:1 with the ratio of the COD of handled water, the response time is 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 grades is anaerobism
MBR pond, waste water total residence time in hydrolytic tank is 12h.Described anaerobism MBR pond, 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 pond
Total residence time is 24h.
The water outlet of anaerobism MBR pond initially enters after intermediate pool collects, then squeezes into nanofiltration system by pump, nanofiltration permeate by
Pressure contact oxidation reactor delivered to by jet pump, and it is 0.45MPa that pressure contact oxidation reactor controls pressure, and built-in plastics suspend
Filler and ceramic grain filter, pressure contact oxidation reactor water outlet is directly discharged.Nanofiltration concentrated solution mixes with percolate and returns to
Pre-treatment biochemistry section, the concentrated solution obtained after biochemistry, MBR, embrane method concentration is re-circulated into compound softening coagulating sedimentation
Pond and subsequent operation.The clean-up effect of whole system such as table 1.
Table 1 embodiment 1 clean-up effect
Embodiment 3:
Rubbish percolation liquid membrane concentrated solution embodiment 1 obtained first passes around the compound coagulative precipitation tank that softens, compound softening
Coagulative precipitation tank is made up of 4 order reaction ponds and sedimentation tank, and the 1st～2 order reaction ponds add sodium hydroxide, and adding of 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 sulfate, 3rd level
Reaction tank adds 2mg/L polyacrylamide high polymer coagulant PAM, and total reaction time is 60min, sinks subsequently into sedimentation tank
Forming sediment, reduce useless hardness of water and remove COD, waste water total residence time in compound softening coagulative precipitation tank is 5h.
Sedimentation tank water outlet enters ozone oxidation reaction device and processes, and described ozone oxidation reaction device is sent out including ozone
Raw device and reactor, ozonator is placed in reactor, and ozonator uses oxygen source ozone generator, ozone dosage
Being 1:1 with the ratio of the COD of handled water, the response time is 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 grades is anaerobism
MBR pond, waste water total residence time in hydrolytic tank is 8h.Described anaerobism MBR pond, including anaerobic pond and MBR module two
Point；Anaerobic pond uses up-flow anaerobic reactor；MBR module uses built-in flat-plate ultrafiltration membrane assembly, and utilizes anaerobism to produce
Gas inner circulating aerating stirs, and blower fan uses rustless steel blower fan.Waste water total residence time in anaerobism MBR pond is 16h.
The water outlet of anaerobism MBR pond initially enters after intermediate pool collects, then squeezes into nanofiltration system by pump, nanofiltration permeate by
Jet pump is delivered to pressure contact oxidation reactor and is carried out biological cleaning, and it is 0.8MPa that pressure contact oxidation reactor controls pressure,
Built-in plastics floating stuffing and activated carbon, pressure contact oxidation reactor water outlet is discharged after more medium filter filters again.
Nanofiltration concentrated solution mixes with percolate and returns to pre-treatment biochemistry section, and obtain after biochemistry, MBR, embrane method concentration is 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.
Table 2 embodiment 2 clean-up effect
Claims (10)
1. the processing method of a percolate embrane method concentrated solution, it is characterised in that percolate embrane method concentrated solution is successively
Softening coagulative precipitation tank, ozone oxidation reaction device, hydrolytic tank and anaerobism MBR pond through compound, the water outlet of anaerobism MBR pond enters nanofiltration
System；
The permeate that nanofiltration system process obtains, after pressure contact oxidation reactor for treatment, directly discharges or through multimedium mistake
Filter discharges after filtering；
Nanofiltration system processes the concentrated solution obtained and mixes with percolate, obtains after biochemistry, MBR, embrane method concentration
Concentrated solution is re-circulated into compound softening coagulative precipitation tank and subsequent operation.
The processing method of percolate embrane method concentrated solution the most according to claim 1, it is characterised in that described rubbish
Percolate embrane method concentrated solution is will to be produced percolate after reverse osmosis membrane or NF membrane or other filtration embrane method process
Raw concentrated solution.
The processing method of percolate embrane method concentrated solution the most according to claim 1 and 2, it is characterised in that described
Percolate embrane method concentrated solution, Main Ingredients and Appearance is Humus material, and TDS is 20000～60000mg/L, COD be 1000～
5000mg/L, ammonia nitrogen concentration is 100～1000mg/L, and TN concentration is 500～2500, and electrical conductivity is 40000～50000us/cm.
The processing method of percolate embrane method concentrated solution the most according to claim 1 and 2, it is characterised in that described
Compound softening coagulative precipitation tank, is made up of reaction of high order pond and sedimentation tank；Waste water first passes through reaction of high order pond, then enters back into
Sedimentation tank precipitates.
The processing method of percolate embrane method concentrated solution the most according to claim 4, it is characterised in that described is multistage
Reaction tank is 3～4 grades, and reaction tanks at different levels are equipped with power agitating device or carry out hydraulic mixing；At 1～2 order reactions started
Pond adds alkaline matter；In first order reaction pond behind, reaction tank adds containing aluminum or iron content coagulant, and final stage reaction tank adds
Polyacrylamide high polymer coagulant.
The processing method of percolate embrane method concentrated solution the most according to claim 5, it is characterised in that described alkalescence
Material is any one or a few the mixture in sodium carbonate, sodium hydroxide and calcium hydroxide, the throwing of described alkaline matter
Add that total mole number is calcium ions and magnesium ions total mole number in waste water 0.5～3 times；Described containing aluminum or iron content coagulant be aluminum sulfate,
Aluminum chloride, iron sulfate, iron chloride or the polymer of any of the above-described material, the described dosage containing aluminum or iron content coagulant is
40～2000mg/L；The dosage of described polyacrylamide high polymer coagulant is 1～10mg/L.
The processing method of percolate embrane method concentrated solution the most according to claim 1, it is characterised in that described ozone
Oxidation reactor, including ozonator and reactor, ozonator is placed in reactor, and ozonator is that air source is smelly
Oxygen Generator or oxygen source ozone generator, ozone dosage is 0.1～1:1 with the ratio of the COD of handled water.
The processing method of percolate embrane method concentrated solution the most according to claim 1, it is characterised in that described hydrolysis
Pond and anaerobism MBR pond are built jointly or are divided with anaerobism MBR pond and build.
The processing method of percolate embrane method concentrated solution the most according to claim 1, it is characterised in that described anaerobism
MBR pond, including anaerobic pond and MBR module two parts；Anaerobic pond uses up-flow anaerobic reactor；MBR module uses built-in
Hyperfiltration membrane assembly or external hyperfiltration membrane assembly.
The processing method of percolate embrane method concentrated solution the most according to claim 1, it is characterised in that described pressure
Power contact oxidation reactor is closed tank, and water inlet, by jet-flow aeration mode, is carried dissolved oxygen and entered tank body, and tank interior is filled out
Filling biologic packing material, reactor inner air pressure is 0.2～0.8MPa；Wherein, described biologic packing material, including granular active carbon,
Any one or a few mixture of coke, anthracite, haydite and soft, semi soft packing and floating stuffing.
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| CN107500441A (en) * | 2017-10-13 | 2017-12-22 | 中联环股份有限公司 | A kind of landfill leachate thick water processing system and processing method |
| CN108341560A (en) * | 2018-04-27 | 2018-07-31 | 江苏环集团有限公司 | A kind of Small Town Wastewater treatment process based on anaerobism MBR technology |
| CN108675565A (en) * | 2018-06-20 | 2018-10-19 | 启迪桑德环境资源股份有限公司 | A kind of system and method for advanced treatment of landfill leachate |
| CN108715491A (en) * | 2018-06-21 | 2018-10-30 | 江苏天楹环保能源成套设备有限公司 | A kind of processing method of nanofiltration concentrate to landfill leachate |
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| CN113578919A (en) * | 2021-07-19 | 2021-11-02 | 上海大学 | Method for improving dehydration performance of kitchen waste anaerobic digestion biogas residues |
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| CN108341560A (en) * | 2018-04-27 | 2018-07-31 | 江苏环集团有限公司 | A kind of Small Town Wastewater treatment process based on anaerobism MBR technology |
| CN108675565A (en) * | 2018-06-20 | 2018-10-19 | 启迪桑德环境资源股份有限公司 | A kind of system and method for advanced treatment of landfill leachate |
| CN108715491A (en) * | 2018-06-21 | 2018-10-30 | 江苏天楹环保能源成套设备有限公司 | A kind of processing method of nanofiltration concentrate to landfill leachate |
| CN109553185A (en) * | 2018-12-29 | 2019-04-02 | 肇庆市鹏凯环保装备有限公司 | A kind of film advanced treating integrated module device for landfill leachate |
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| CN109928476A (en) * | 2019-04-26 | 2019-06-25 | 中创水务科技环保(广东)有限公司 | A kind of landfill leachate pretreatment system and its technique |
| CN110304789A (en) * | 2019-06-12 | 2019-10-08 | 北京洁绿环境科技股份有限公司 | A kind of processing system and its processing method of the nanofiltration concentrate that landfill leachate treatment generates |
| CN110316905A (en) * | 2019-06-18 | 2019-10-11 | 中国电建集团河南工程有限公司 | Processing system for landfill leachate zero-emission in garbage incineration power plant |
| CN110372096A (en) * | 2019-07-26 | 2019-10-25 | 中国恩菲工程技术有限公司 | The processing method of garbage leachate |
| CN110563265A (en) * | 2019-09-10 | 2019-12-13 | 贵州欧瑞欣合环保股份有限公司 | Landfill leachate treatment process |
| CN113443735A (en) * | 2020-03-26 | 2021-09-28 | 深圳市长隆科技有限公司 | Method for resource utilization of landfill leachate concentrated solution |
| CN112441689A (en) * | 2020-09-29 | 2021-03-05 | 武汉天源环保股份有限公司 | Membrane concentrate harmless treatment system and method |
| CN112441689B (en) * | 2020-09-29 | 2022-12-13 | 武汉天源环保股份有限公司 | Membrane concentrate harmless treatment system and method |
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| CN113578919B (en) * | 2021-07-19 | 2022-09-09 | 上海大学 | Method for improving dehydration performance of kitchen waste anaerobic digestion biogas residues |
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