CN108751550A - A kind of processing method and processing system of landfill leachate tail water - Google Patents
A kind of processing method and processing system of landfill leachate tail water Download PDFInfo
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- CN108751550A CN108751550A CN201810514598.4A CN201810514598A CN108751550A CN 108751550 A CN108751550 A CN 108751550A CN 201810514598 A CN201810514598 A CN 201810514598A CN 108751550 A CN108751550 A CN 108751550A
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- water
- unit
- landfill leachate
- membrane distillation
- catalytic oxidation
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 130
- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 36
- 238000003672 processing method Methods 0.000 title claims abstract description 17
- 238000012545 processing Methods 0.000 title claims abstract description 16
- 239000012528 membrane Substances 0.000 claims abstract description 79
- 238000004821 distillation Methods 0.000 claims abstract description 61
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 54
- 230000003197 catalytic effect Effects 0.000 claims abstract description 54
- 239000002131 composite material Substances 0.000 claims abstract description 53
- 230000003647 oxidation Effects 0.000 claims abstract description 51
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 51
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000005345 coagulation Methods 0.000 claims abstract description 28
- 230000015271 coagulation Effects 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 239000000701 coagulant Substances 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000006228 supernatant Substances 0.000 claims abstract description 9
- 239000003054 catalyst Substances 0.000 claims abstract description 6
- 230000002195 synergetic effect Effects 0.000 claims abstract description 5
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 4
- 239000007800 oxidant agent Substances 0.000 claims abstract description 3
- 239000010813 municipal solid waste Substances 0.000 claims description 13
- 229920002401 polyacrylamide Polymers 0.000 claims description 12
- 238000001556 precipitation Methods 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 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 8
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 8
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 7
- 229910001882 dioxygen Inorganic materials 0.000 claims description 7
- 239000000945 filler Substances 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000010802 sludge Substances 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 5
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 4
- 239000000498 cooling water Substances 0.000 claims description 4
- 230000004907 flux Effects 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 239000003344 environmental pollutant Substances 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 229910052759 nickel Inorganic materials 0.000 claims description 3
- 231100000719 pollutant Toxicity 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 229920001661 Chitosan Polymers 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims description 2
- 239000004411 aluminium Substances 0.000 claims description 2
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 230000008859 change Effects 0.000 claims description 2
- 238000002386 leaching Methods 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 150000002739 metals Chemical class 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 229910021420 polycrystalline silicon Inorganic materials 0.000 claims description 2
- 229920005591 polysilicon Polymers 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 1
- 238000006116 polymerization reaction Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 23
- 239000012141 concentrate Substances 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 239000000126 substance Substances 0.000 abstract description 7
- 239000005416 organic matter Substances 0.000 abstract description 5
- 238000010612 desalination reaction Methods 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 230000008569 process Effects 0.000 description 11
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 238000003860 storage Methods 0.000 description 6
- -1 hydroxyl radical free radical Chemical class 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 238000000108 ultra-filtration Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 241001122767 Theaceae Species 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 235000003891 ferrous sulphate Nutrition 0.000 description 2
- 239000011790 ferrous sulphate Substances 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 239000008235 industrial water Substances 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000001728 nano-filtration Methods 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 125000002573 ethenylidene group Chemical group [*]=C=C([H])[H] 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 238000006385 ozonation reaction Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
-
- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F1/5263—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using natural chemical compounds
-
- 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- 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)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention provides a kind of processing method and processing system of landfill leachate tail water, including：(1) dosing coagulant into landfill leachate tail water is realized by coagulation unit and is separated by solid-liquid separation；(2) supernatant of coagulation unit adds hydrogen peroxide, so that ozone is generated the hardly degraded organic substance in strong oxidizer decomposition percolate under the catalytic action of catalyst using the synergistic effect of ozone and hydrogen peroxide into composite catalytic oxidation unit；(3) water outlet of composite catalytic oxidation unit carries out advanced treating by membrane distillation unit, and wherein membrane distillation unit distills form using submerged membrane.The present invention method energy depth removal tail water in COD and organic matter difficult to degrade, and to water outlet carry out desalination, make its can direct reuse in production process.The parallel-adder settle-out time of membrane distillation unit can effectively be extended simultaneously, reduce equipment maintenance cost, the yield of concentrate is down to reduced levels or realize zero-emission.
Description
Technical field
The invention belongs to field of waste water treatment, and in particular to a kind of processing method and processing dress of landfill leachate tail water
It sets.
Background technology
Two kinds of China townm refuse treatment measures：Sanitary landfills and burning can all lead to the problem of landfill leachate.Rubbish oozes
Filtrate component is complicated, and pollutant concentration is high, is usually expressed as high COD, high ammonia nitrogen and with high salt.If can be led without processing direct emission
The serious pollution for causing water body and soil endangers the health of resident and destroys town ecological and living environment.Mainstream at present
Garbage leachate treatment process be " pretreatment+biochemical treatment (including anaerobism, AO, MBR etc.)+film process group technology (ultrafiltration,
It is nanofiltration, reverse osmosis) ".The technique can by landfill leachate original sub-block to receiving pipe standards, but face simultaneously processing time compared with
It is long, many problems such as concentrate is difficult to handle after film, operating cost is higher.
Chinese patent CN107098531A is related to a kind of high-efficiency refuse percolate treating process, mainly by ozone oxidation+mixed
Solidifying+membrane distillation unit is constituted.This set technique can effectively reduce COD, BOD in landfill leachate water outlet5And ammonia nitrogen concentration.But
It is that its ozone oxidation unit uses ozone regulating reservoir as reaction vessel, ozone directly blasts in pond, in fact it could happen that ozone stops
Time is too short, and mass transfer effect is bad, generates the problems such as hydroxyl radical free radical is few and the utilization rate of ozone is relatively low, cannot fully will be in water
COD and BOD5Removal.Lack filter device between coagulation unit and membrane distillation unit, suspends present in coagulation water outlet
Object may block fenestra, influence the stable operation of membrane distillation unit.
Chinese patent CN104211245A discloses a kind of processing method of landfill leachate embrane method concentrate.Embrane method concentrates
Liquid after pretreatment, is concentrated into multiple-effect membrane distillation unit, water outlet can qualified discharge or reuse, obtained concentrated phase liquid passes through
After condensing crystallizing isolates solid, directly filled.This method is handled for embrane method concentrated phase liquid, reduces concentrated phase liquid
Yield, but will appear multiple concentration process (including reverse osmosis, nanofiltration etc.) on integrated artistic, technological process is long, is
It unites more complex.
It is existing insufficient in view of the above technology, this application involves a kind of processing method and system of landfill leachate tail water,
Suspended matter, calcium ions and magnesium ions and part COD remaining in tail water are removed by coagulation first, utilizes tower composite catalytic oxidation later
Unit improves ozone utilization rate based on the synergistic effect between hydrogen peroxide and ozone, to the COD and organic matter progress depth in water
Degree removal.The filler in tower can also remove the partial suspended thing in the water outlet of coagulation unit simultaneously, will significantly improve membrane distillation list
The influent quality of member.The water outlet of composite catalytic oxidation tower finally enters membrane distillation unit and is concentrated, and production water can be with direct emission
Or reuse, concentrate can be burned directly or be separated by solid-liquid separation by crystallization.
Invention content
The purpose of the present invention is the garbage leachate treatment process " pretreatments+biochemical treatment+film process for current main-stream
Concentrated phase liquid yield is larger after the film that group technology " faces and intractable problem, provides a kind of place of landfill leachate tail water
Method and system is managed, percolate treatment is subjected to depth concentration using film distillation technology, substitutes traditional later stage membrane treatment process,
Make processing of the percolate treatment Jing Guo " coagulation+tower composite catalytic oxidation+membrane distillation " technique, promotes effluent quality, and can
Qualified discharge is back to production process.
Realize that the technical solution of the object of the invention is：
A kind of processing method of landfill leachate tail water, includes the following steps：
(1) dosing coagulant into landfill leachate tail water, is separated by solid-liquid separation in coagulation unit；The coagulant is
Bodied ferric sulfate, polyacrylamide, polyaluminum ferric chloride, aluminium polychloride, poly-ferric chloride, polysilicon acid flocculant, chitosan
It is one or more in flocculant；
(2) supernatant that coagulation unit generates adds hydrogen peroxide, into composite catalytic oxidation unit, utilizes ozone and dioxygen
The synergistic effect of water makes ozone generate strong oxidizer decomposition under the catalytic action of catalyst and remove difficult to degrade in percolate
Organic matter；
(3) water outlet of composite catalytic oxidation unit carries out advanced treating by membrane distillation unit, and wherein membrane distillation unit is adopted
Form is distilled with submerged membrane.
Wherein, in step (1), the addition of the coagulant is with the pollutant load in the landfill leachate tail water
Increase and increase, when COD is 400~600mg/L in the landfill leachate tail water, then the addition of coagulant is 0.2~1g/
L, when COD is 1000~1400mg/L in the landfill leachate tail water, then the addition of coagulant is 1~3g/L.
Preferably, in step (1), the coagulant is bodied ferric sulfate and polyacrylamide, and the mass ratio of the two is
1000：(1~4)；After first adding 5~15min of bodied ferric sulfate stirring, polyacrylamide is added.
Wherein, in step (2), added based on 30% hydrogen peroxide, in supernatant hydrogen peroxide volume fraction be 0.5~
2.0%；Ozone dosage is 0.5~5.0g/L；Water is 0.5~4 hour in the residence time of the composite catalytic oxidation unit.
Wherein, in step (3), the water outlet of composite catalytic oxidation unit is heated up to entering membrane distillation after 50~70 DEG C
The heat source of unit, heating includes the water vapour that membrane distillation unit generates and the Low Temperature Steam that garbage burning factory provides, the low temperature
The temperature of steam is 100~130 DEG C, pressure 0.1-0.3MPa.
Wherein, in step (3), the cooling water side temperature of membrane distillation unit maintains 10~20 DEG C, membrane distillation cell-average
Membrane flux is 20~28L m-2·h-1。
Wherein, when the water outlet conductivity of membrane distillation unit is higher than 500 μ Scm-1When, then use hydrochloric acid solution, sodium hydroxide molten
Liquid and water clean the membrane module in membrane distillation unit.
A kind of processing system of landfill leachate tail water, including coagulation unit, composite catalytic oxidation tower and membrane distillation unit,
The coagulation unit includes the stirred tank and precipitation tank being linked in sequence, the stirred tank be provided with percolate treatment into
The mouth of a river and dosing mouth, the precipitation tank are provided with water outlet, and precipitation trench bottom is provided with sludge outlet；
The water outlet connects the composite catalytic oxidation tower bottom, and water is delivered to composite catalytic oxidation by metering pump
Tower, the composite catalytic oxidation tower are provided with dioxygen water inlet and ozone import；The composite catalytic oxidation top of tower is by going out
Waterpipe connects the membrane distillation unit；Metering pump, First Heat Exchanger and the second heat exchanger are provided on the outlet conduit,
The heating agent pipeline of First Heat Exchanger connects the steam outlet of the membrane distillation unit, and the heating agent pipeline of the second heat exchanger connects rubbish
The Low Temperature Steam pipeline of rubbish power generation by waste combustion factory.
By the suction of vacuum pump, the water vapour that membrane distillation unit generates is carried over, and is exchanged heat and condensed in First Heat Exchanger
It is condensation of water (final outflow water after processing) from First Heat Exchanger discharge for liquid.After being concentrated by membrane distillation unit
Concentrate is discharged from the water outlet of the unit.
Air enters ozone generator by air pump, after certain density ozone is generated in ozone generator, into again
Close catalysis oxidizing tower.If containing ozone in the tail gas of composite catalytic oxidation tower discharge, absorbing off-gas ozone should be added behind and filled
It sets.
Preferably, the composite catalytic oxidation tower is packed tower, and the filler in tower is active carbon particle, is loaded on activated carbon
There are one or more metals in Mn, Co, Ni, Fe；
The ozone import of the composite catalytic oxidation tower is connected with ozone generator, and the ozone generator is connected with air
Pipeline and air pump；
Absorbing off-gas ozone device is provided on the exhaust pipe of composite catalytic oxidation tower.
It is highly preferred that the membrane distillation unit includes plate type membrane assembly, the membrane material that membrane module uses is poly- for hydrophobicity
Vinylidene.
The present invention has the following advantages in contrast to existing garbage leachate treatment process：
(1) can depth go water removal in COD and organic matter difficult to degrade, promoted effluent quality.
(2) generation of concentrated phase liquid after film is substantially reduced, and can further concentrate concentrated phase liquid, concentrated phase liquid is made to be directly entered burning
Stove burns or carries out brine separation, realizes near-zero release or zero-emission.
(3) advanced desalination being discharged to percolate can be achieved, by water outlet direct reuse in production process.
(4) influent quality for ensureing membrane distillation unit, extends the parallel-adder settle-out time of membrane distillation unit.
(5) ozone utilization ratio is significantly improved, the treatment effect of tower composite catalytic oxidation unit is improved.
COD and organic matter difficult to degrade in the method energy depth removal tail water of the present invention, and desalination is carried out to water outlet, make it
Can direct reuse in production process.The parallel-adder settle-out time of membrane distillation unit can effectively be extended simultaneously, reduce plant maintenance expense
With, by the yield of concentrate be down to reduced levels or realize zero-emission.
Description of the drawings
Fig. 1 is the process flow chart of landfill leachate tail water processing method of the present invention.
Fig. 2 is the schematic diagram of landfill leachate tail water treatment system.
The correspondence of equipment and number is in figure：
Stirred tank 1, polymeric ferrous sulphate solution storage tank 101, polyacrylamide solution storage tank 102, composite catalytic oxidation tower 2,
Dioxygen water storage tank 201, ozone generator 202, membrane distillation unit 3, First Heat Exchanger 301, the second heat exchanger 302, Low Temperature Steam
Pipeline 303, vacuum pump 304, condensation of water pipeline 305, concentrate pipeline 306, sludge outlet 4, precipitation tank 5.
Specific implementation mode
What Fig. 1 was presented is the process flow chart of landfill leachate tail water processing method.In figure, landfill leachate tail water enters
Coagulation unit removes suspended particulate substance, calcium ions and magnesium ions and part COD remaining in tail water by coagulation first.Coagulation unit produces
Raw sludge is focused on, and water outlet enters tower composite catalytic oxidation unit.Coagulation unit water outlet (add hydrogen peroxide it
Afterwards), it reacts with the hydroxyl radical free radical being decomposed to form through catalysis ozone in tower composite catalytic oxidation unit, in water
Hardly degraded organic substance carries out depth removal.Later, the water outlet of composite catalytic oxidation tower enters membrane distillation unit and is concentrated, and produces water
Industrial water reuse is can be used as, concentrated phase liquid can be burned directly or is separated by solid-liquid separation into subsequent evaporation crystalline element.
A kind of processing method of landfill leachate tail water, specifically comprises the following steps：
(1) a certain amount of coagulant is added into landfill leachate tail water, is realized and is separated by solid-liquid separation in coagulation unit.It is described
Coagulant is bodied ferric sulfate and polyacrylamide, and dosage is 0.2~3g/L.
(2) supernatant of coagulation unit is after adding hydrogen peroxide, into tower composite catalytic oxidation unit, using ozone with
The synergistic effect of hydrogen peroxide makes ozone form the difficulty that hydroxyl radical free radical OH is destroyed in percolate under the catalytic action of catalyst
Degradation of organic substances.Tower composite catalytic oxidation unit can extend the residence time of ozone molecule in water so that ozone can
It is come into full contact with catalyst, decomposition releases more hydroxyl radical free radicals, improves the utilization ratio of ozone, improves in water
COD removal effects.Filler (catalyst) is filled in composite catalytic oxidation tower, filler is to have loaded the one kind or more such as Mn, Co, Ni
The granular activated carbon of kind metallic element.The filler can also adsorb and filter the water outlet of coagulation unit other than with catalytic action
In suspended matter that may be present, the influent quality of subsequent film distillation unit can be significantly improved.Hydrogen peroxide dosage is 0.5~2%,
Ozone dosage is 0.1~5g/L, and residence time of the water in composite catalytic oxidation tower is 0.5~4h.
(3) sludge (precipitation) that the bottom of coagulation unit generates is handled after collecting and being dehydrated.
(4) water outlet of tower composite catalytic oxidation unit enters membrane distillation unit progress advanced treating.Film distillation technology profit
Two kinds of different liquid of temperature are separated into (film both sides are respectively raw water side and production water side), only vapor point with microporous hydrophobic membrane
Under son vapor partial pressure difference effect caused by the temperature different solutions of film both sides, hydrophobic membrane is passed through from raw water side, and in production water
Side is collected.Therefore film distillation technology has the spies such as salt rejection rate and water rate of recovery higher, producing water water quality more preferable (comparison is reverse osmosis)
Point.The membrane module that membrane distillation unit uses is plate type membrane assembly, and membrane material is hydrophobicity Kynoar, and operation format is leaching
It is mainly the Low Temperature Steam that garbage incinerating power plant generates to no formula, heat source.The production water of membrane distillation unit since water quality is preferable,
It can be used as the industrial water or cooling water of factory；The concentrated phase liquid of generation can directly be fired since volume greatly reduces into incinerator
It burns or enters the evaporative crystallizations units such as multiple-effect evaporation, MVR and be separated by solid-liquid separation.
Below in conjunction with concrete operations parameter, technical solution is further illustrated the present invention by embodiment.Art technology
Personnel are not used in and are limited the scope of the invention it is to be understood that embodiment is merely to illustrate the present invention.
In embodiment, unless otherwise instructed, technological means used is this field conventional technology.
Embodiment 1：
Referring to Fig. 2, the processing system for the landfill leachate tail water that the present embodiment uses, including coagulation unit, composite catalyzing
Oxidizing tower and membrane distillation unit,
The coagulation unit includes the stirred tank 1 being linked in sequence and precipitation tank 5, and the stirred tank 1 is provided with percolate tail
Water water inlet and dosing mouth, dosing mouth connect polymeric ferrous sulphate solution storage tank 101 and polyacrylamide solution storage tank 102, institute
It states precipitation tank 5 and is provided with water outlet, 5 bottom of precipitation tank is provided with sludge outlet 4；
The water outlet connects 2 bottom of composite catalytic oxidation tower, and water is delivered to composite catalyzing oxygen by metering pump
Change tower, the composite catalytic oxidation tower is provided with dioxygen water inlet and ozone import；Dioxygen water inlet is connected with dioxygen water storage tank
201, the composite catalytic oxidation top of tower connects the membrane distillation unit 3 by outlet conduit；It is set on the outlet conduit
It is equipped with metering pump and the water outlet of composite catalytic oxidation tower is delivered to First Heat Exchanger 301 and the second heat exchanger 302.First Heat Exchanger
Heating agent pipeline connect the steam outlet of the membrane distillation unit 3, the heating agent pipeline of the second heat exchanger 302 connects waste incineration
The Low Temperature Steam pipeline 303 in power plant, water are elevated the water inlet that temperature enters membrane distillation unit later.The Low Temperature Steam
Temperature is 100~130 DEG C, and pressure is 0.1~0.3MPa.
By the suction of vacuum pump 304, the vapor that membrane distillation unit generates is carried over, and is exchanged heat in First Heat Exchanger
It is condensed into liquid, the water in condensation of water pipeline 305 is final outflow water after processing.It is dense after being concentrated by membrane distillation unit
The concentrated liquid pipe road 306 of contracting liquid is discharged from the water outlet of the unit.
Air enters ozone generator by air pump, will be smelly after certain density ozone is generated in ozone generator 202
Oxygen and air blast composite catalytic oxidation tower together.It, should be behind if containing ozone in the tail gas of composite catalytic oxidation tower discharge
In addition absorbing off-gas ozone device.
The membrane distillation unit 3 includes plate type membrane assembly, and the membrane material that membrane module uses is hydrophobicity Kynoar.
The composite catalytic oxidation tower is packed tower, and the filler that the present embodiment uses is the activated carbon that load has Mn and Co
Grain.The higher ozone of concentration is equipped with exhaust gas processing device (routine purchased in market to human health, composite catalytic oxidation top of tower
Equipment), remaining ozone in decomposed tail gas.
Using the percolate ultra-filtration water of Jiangsu garbage incinerating power plant as the water inlet of coagulation unit, the water of ultra-filtration water
Matter situation approximately as：PH is 6.2 or so；A concentration of 500~600mg/L of COD；Ammonia nitrogen concentration is 20~40mg/L；Total nitrogen is dense
Degree is about 100~200mg/L；Conductance is about 15000 μ s/cm；Color is tea yellow, basic odorless.
Successively add Polyferric Sulfate Flocculants and polyacrylamide into ultra-filtration water, dosage be respectively 0.5g/L and
1.5mg/L.It is sufficiently stirred 10min after first adding bodied ferric sulfate in coagulation unit, polyacrylamide is added later and continues to stir
20min is mixed, mixing water is staticly settled by about 30min, is layered as supernatant liquor and lower sediment.Lower sediment after separation,
Dehydration is collected to be focused on.
Supernatant is after adding 30% hydrogen peroxide of 1% (volume ratio), into composite catalytic oxidation tower.Composite catalyzing
The ozone source of oxidizing tower is ozone generator, and the air source that ozone generator uses is air or industrial oxygen.The present embodiment makes
It uses air as the air source of ozone generator, and is equipped with air compressor and air separation unit, remove the moisture in air and incite somebody to action
Oxygen concentration in air is increased to 90% or more.Adjusting ozone dosage is 0.8g/L, and water is in catalytic ozonation tower
Residence time is 2h.
The water outlet of tower composite catalytic oxidation unit is heated before entering membrane distillation unit, and heat source is rubbish
The Low Temperature Steam of power generation by waste combustion factory, vapor (steam) temperature are about 100~130 DEG C.Membrane distillation raw water side temperature maintains 60~70 DEG C, cold
But water side temperature maintains 10~20 DEG C, and membrane distillation cell-average membrane flux is 25L m-2·h-1。
The water quality situation being discharged after this method advanced treating is：PH is 6.8 or so；A concentration of 53mg/L of COD；Ammonia nitrogen is dense
Degree is 5mg/L；Total nitrogen concentration is about 2mg/L；Conductivity is 37us/cm；The color of water becomes clear, colorless, COD from tea yellow
Removal rate is more than 90%, and ammonia nitrogen removal frank is more than 75%, and nitrogen removal rate is more than 99%, and salt rejection rate is about 99.7%.In water outlet
COD, ammonia nitrogen and total nitrogen concentration be satisfied by《Household refuse landfill sites control standard》Discharge in (GB 16889-2008) table 3
Standard limit.
Membrane module, pipeline, sink in membrane distillation unit etc. are kept the temperature, and to reduce heat losses, are reduced processed
Journey energy consumption.After distillation device runs a period of time, when production water conductivity is higher than 500 μ Scm-1When, need to membrane module into
Row cleaning.The hydrochloric acid solution that pH is 2.5 and the NaOH solution that pH is 11.5 are prepared, is respectively washed membrane module 30 minutes.Later, make
It is rinsed with clear water, until the pH value of cleaning water outlet is returned to 7 or so.
Embodiment 2：
Using the percolate bio-chemical effluent of Jiangsu garbage burning factory as the water inlet of coagulation unit, the water quality of bio-chemical effluent
Situation approximately as：PH is 6.7~6.9；A concentration of 1200mg/L of COD or so；Ammonia nitrogen concentration is 10~20mg/L；Total nitrogen concentration
About 40~50mg/L；Conductance is about 20000 μ s/cm.
The percolate bio-chemical effluent is handled using the method in embodiment 1, during test run, polyaluminum sulfate
The dosage of iron and polyacrylamide is respectively 1.2g/L and 2mg/L, and it is 1.5% that supernatant liquor, which adds hydrogen peroxide ratio,；It adjusts
Ozone dosage is 1.5g/L, and residence time of the water in composite catalytic oxidation tower is 2.5h；Membrane distillation raw water side temperature maintains
At 70 DEG C, cooling water side temperature maintains 15 DEG C, and average flux is 20.1L m-2·h-1。
The water quality situation being discharged after processing is：PH is 7.1 or so；A concentration of 54mg/L of COD；Ammonia nitrogen concentration is 4.1mg/
L；Total nitrogen concentration is about 3.1mg/L；Conductivity is 69us/cm.COD totality removal rates are more than 95.5%；Ammonia nitrogen removal frank is more than
60%；Nitrogen removal rate is more than 92%；Salt rejection rate is about 99.6%.COD, ammonia nitrogen and total nitrogen concentration in water outlet are satisfied by《It is raw
Refuse landfill living controls standard》Emission limit standard in (GB 16889-2008) table 3.
Above embodiment be only to the present invention specific implementation mode be described, not to the scope of the present invention into
Row limits, and those skilled in the art can also do numerous modifications and variations, be set not departing from the present invention on the basis of existing technology
Under the premise of meter spirit, all variations and modifications that this field ordinary engineering and technical personnel makes technical scheme of the present invention,
It should all fall into the protection domain of claims of the present invention determination.
Claims (10)
1. a kind of processing method of landfill leachate tail water, which is characterized in that include the following steps：
(1) dosing coagulant into landfill leachate tail water is realized in coagulation unit and is separated by solid-liquid separation；The coagulant is polymerization
Ferric sulfate, polyacrylamide, polyaluminum ferric chloride, aluminium polychloride, poly-ferric chloride, polysilicon acid flocculant, flocculate with chitosan
It is one or more in agent；
(2) supernatant that coagulation unit generates adds hydrogen peroxide, into composite catalytic oxidation unit, utilizes ozone and hydrogen peroxide
Synergistic effect makes ozone generate strong oxidizer decomposition under the catalytic action of catalyst and remove difficult to degrade organic in percolate
Object；
(3) water outlet of composite catalytic oxidation unit carries out advanced treating by membrane distillation unit, and wherein membrane distillation unit is using leaching
Do not have formula membrane distillation form.
2. the processing method of landfill leachate tail water according to claim 1, which is characterized in that described mixed in step (1)
The addition of solidifying agent increases as the pollutant load in the landfill leachate tail water increases, when the landfill leachate tail
COD is 400~600mg/L in water, then the addition of coagulant is 0.2~1g/L, when COD is in the landfill leachate tail water
1000~1400mg/L, then the addition of coagulant is 1~3g/L.
3. the processing method of landfill leachate tail water according to claim 1, which is characterized in that described mixed in step (1)
Solidifying agent is bodied ferric sulfate and polyacrylamide, and the mass ratio of the two is 1000：(1~4)；First add bodied ferric sulfate stirring
After 5~15min, polyacrylamide is added.
4. the processing method of landfill leachate tail water according to claim 1, which is characterized in that in step (2), by 30%
Hydrogen peroxide meter, the volume fraction that hydrogen peroxide is added in supernatant are 0.5~2.0%；Ozone dosage is 0.5~5.0g/L；Water
It it is 0.5~4 hour in the residence time of the composite catalytic oxidation unit.
5. the processing method of landfill leachate tail water according to claim 1, which is characterized in that compound to urge in step (3)
The water outlet for changing oxidation unit is heated up to membrane distillation unit is entered after 50~70 DEG C, and the heat source of heating includes membrane distillation unit
The temperature of the Low Temperature Steam that the water vapour and garbage incinerating power plant of generation provide, the Low Temperature Steam is 100~130 DEG C, pressure
Power is 0.1~0.3MPa.
6. the processing method of landfill leachate tail water according to claim 1, which is characterized in that in step (3), membrane distillation
The cooling water side temperature of unit maintains 10~20 DEG C, and membrane distillation cell-average membrane flux is 20~28Lm-2·h-1。
7. according to the processing method of claim 1~6 any one of them landfill leachate tail water, which is characterized in that when film steams
The water outlet conductivity for evaporating unit is higher than 500 μ Scm-1When, then use hydrochloric acid solution, sodium hydroxide solution and water to membrane distillation unit
In membrane module cleaned.
8. a kind of processing system of landfill leachate tail water, which is characterized in that including coagulation unit, composite catalytic oxidation tower and film
Distillation unit,
The coagulation unit includes the stirred tank and precipitation tank being linked in sequence, and the stirred tank is provided with percolate treatment water inlet
And dosing mouth, the precipitation tank are provided with water outlet, and precipitation trench bottom is provided with sludge outlet；
The water outlet connects the composite catalytic oxidation tower bottom, and water is delivered to composite catalytic oxidation tower by metering pump,
The composite catalytic oxidation tower is provided with dioxygen water inlet and ozone import；The composite catalytic oxidation top of tower passes through outlet pipe
Road connects the membrane distillation unit；It is provided with metering pump, First Heat Exchanger and the second heat exchanger on the outlet conduit, first
The heating agent pipeline of heat exchanger connects the steam outlet of the membrane distillation unit, and the heating agent pipeline connection rubbish of the second heat exchanger is burnt
Burn the Low Temperature Steam pipeline in power plant.
9. processing system according to claim 8, which is characterized in that the composite catalytic oxidation tower is packed tower, in tower
Filler be active carbon particle, on activated carbon load have one or more metals in Mn, Co, Ni, Fe；The composite catalyzing oxygen
The ozone import for changing tower is connected with ozone generator, and the ozone generator is connected with air pipeline and air pump；Composite catalyzing oxygen
Change and is provided with absorbing off-gas ozone device on the exhaust pipe of tower.
10. processing system according to claim 8 or claim 9, which is characterized in that the membrane distillation unit includes flat film group
Part, the membrane material that membrane module uses are hydrophobicity Kynoar.
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| CN110328218A (en) * | 2019-07-30 | 2019-10-15 | 湖南中森环境科技有限公司 | A kind of resource utilization method of organic pollution salt slag |
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| CN111977776A (en) * | 2020-08-28 | 2020-11-24 | 吉林大学 | Catalytic ozonation-based pretreatment method for acidic wastewater containing difficultly-degradable water-soluble polymers |
| CN112517604A (en) * | 2020-11-16 | 2021-03-19 | 新中天环保股份有限公司 | Harmless treatment process for industrial waste salt |
| CN113698015A (en) * | 2020-05-21 | 2021-11-26 | 河海大学 | Electro-catalysis and membrane distillation-based landfill leachate concentrated solution treatment system and method |
| WO2022062552A1 (en) * | 2020-09-27 | 2022-03-31 | 山东理工大学 | Medium-to-high-temperature mvr wastewater treatment method and system capable of degrading organic matter |
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