CN106242163B - A kind of processing method of percolate embrane method concentrate - Google Patents
A kind of processing method of percolate embrane method concentrate Download PDFInfo
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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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- 238000000034 method Methods 0.000 title claims abstract description 63
- 239000012141 concentrate Substances 0.000 title claims abstract description 53
- 238000003672 processing method Methods 0.000 title claims abstract description 13
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 36
- 238000001728 nano-filtration Methods 0.000 claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 230000003647 oxidation Effects 0.000 claims abstract description 23
- 150000001875 compounds Chemical class 0.000 claims abstract description 21
- 238000001556 precipitation Methods 0.000 claims abstract description 18
- 230000001112 coagulating effect Effects 0.000 claims abstract description 17
- 238000012545 processing Methods 0.000 claims abstract description 15
- 230000003301 hydrolyzing effect Effects 0.000 claims abstract description 10
- 239000012466 permeate Substances 0.000 claims abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 239000012528 membrane Substances 0.000 claims description 25
- 239000002351 wastewater Substances 0.000 claims description 24
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000010813 municipal solid waste Substances 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 238000004062 sedimentation Methods 0.000 claims description 12
- 239000000701 coagulant Substances 0.000 claims description 10
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 239000004411 aluminium Substances 0.000 claims description 7
- 229910052782 aluminium Inorganic materials 0.000 claims description 7
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 7
- 229920002401 polyacrylamide Polymers 0.000 claims description 7
- 229920000642 polymer Polymers 0.000 claims description 7
- 229910052742 iron Inorganic materials 0.000 claims description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- 238000012856 packing Methods 0.000 claims description 5
- 238000001223 reverse osmosis Methods 0.000 claims description 5
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 4
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 4
- 229910001424 calcium ion Inorganic materials 0.000 claims description 4
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- 238000007667 floating Methods 0.000 claims description 3
- 239000003864 humus Substances 0.000 claims description 3
- 239000002075 main ingredient Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000005273 aeration Methods 0.000 claims description 2
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 2
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 2
- 239000003830 anthracite Substances 0.000 claims description 2
- 239000000571 coke Substances 0.000 claims description 2
- 238000011049 filling Methods 0.000 claims description 2
- 230000007062 hydrolysis Effects 0.000 claims description 2
- 238000006460 hydrolysis reaction Methods 0.000 claims description 2
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 claims description 2
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 2
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 25
- 239000000126 substance Substances 0.000 abstract description 8
- 230000008569 process Effects 0.000 description 18
- 230000000694 effects Effects 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 150000003839 salts Chemical class 0.000 description 7
- 239000005416 organic matter Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000005325 percolation Methods 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 230000035484 reaction time Effects 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- 238000001764 infiltration Methods 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 238000012805 post-processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000007348 radical reaction Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Classifications
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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
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
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
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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| CN107129107A (en) * | 2017-06-05 | 2017-09-05 | 安徽普朗膜技术有限公司 | A kind of recovery and processing system of percolate |
| 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 |
| 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 |
| CN110655269A (en) * | 2019-03-19 | 2020-01-07 | 深圳市深投环保科技有限公司 | Method for treating dangerous waste safe landfill leachate |
| 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 |
| 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 |
| CN113578919B (en) * | 2021-07-19 | 2022-09-09 | 上海大学 | A method for improving the dehydration performance of anaerobic digestion of food waste and biogas residue |
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| CN1066128C (en) * | 1997-10-09 | 2001-05-23 | 李维宁 | Deep purifying and reclaiming appts. and method for industrial organic sewage |
| KR100475451B1 (en) * | 2002-10-07 | 2005-03-10 | 주식회사 아이이아이 | The treatment system for purifying |
| CN101265003A (en) * | 2008-04-21 | 2008-09-17 | 北京水气蓝德环保科技有限公司 | Method for treating high-concentration organic sewage difficult to degrade |
| CN102086075B (en) * | 2009-12-08 | 2013-02-20 | 北京机电院高技术股份有限公司 | Deep treatment process of landfill leachate |
| CN101891336B (en) * | 2010-06-25 | 2012-07-04 | 北京伊普国际水务有限公司 | System and method for leachate treatment in sanitary landfill |
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