CN107365027A - The processing system and method for percolate - Google Patents
The processing system and method for percolate Download PDFInfo
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- CN107365027A CN107365027A CN201710697620.9A CN201710697620A CN107365027A CN 107365027 A CN107365027 A CN 107365027A CN 201710697620 A CN201710697620 A CN 201710697620A CN 107365027 A CN107365027 A CN 107365027A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- 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
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- 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
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- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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Abstract
The invention discloses a kind of processing system of percolate and method, the system includes the pretreatment unit for cleaning, the pretreatment unit includes first order reaction sedimentation basin, one stage catalyzing oxidizing tower and the second order reaction sedimentation basin being sequentially connected, the system also includes biochemical treatment apparatus, two level catalysis oxidizing tower, removing heavy metals tower and the clear water reserviors being sequentially connected, and the second order reaction sedimentation basin is connected with biochemical treatment apparatus.The present invention using biological synergetic biochemical technology, deep oxidation process part in biological treatment part by using catalytic ozonation technology and heavy metal adsorption technology, further reduce COD and ammonia nitrogen, and heavy metal, concentrate, non-secondary pollution are not produced after advanced treating.
Description
Technical field
The invention belongs to environmental technology field, and in particular to the processing system and method for a kind of percolate.
Background technology
The conventional processing method of percolate has：Bioanalysis, chemical oxidization method, flocculent precipitation, recharge method, Manual moist
Ground method etc., these methods have preferable treatment effect, but the processing effect of centering mature landfill leachate to early stage percolate
Fruit is then very poor, and middle mature landfill leachate has following features compared with early stage percolate：(1) yield of percolate
The influence of climate and seasonal variations is extremely obvious, and especially rainy season amount is bigger；(2) complicated component, difficult for biological degradation have
Machine thing accounts for more than 70% of total organic component in percolate；(3) biodegradability is poor, BOD5/CODcrValue is generally less than 0.15；
(4) ammonia nitrogen concentration is high, produces toxic action to microorganism, causes nutrient in percolate out of proportion；(5) nutrient ratio
Example imbalance；(6) total dissolved solid is high；(7) heavy metal ion content is high；(8) with the extension of Closure of landfill site time, diafiltration
Further accumulation and increase, intractability further increase hardly degraded organic substance in liquid.
Domestic conventional method for treating garbage percolation liquid has ammonia aeration+anaerobism+aerobic or membrane technology at present.Ammonia aeration
The ammonia nitrogen in waste water can be effectively removed, reduces influence of the ammonia nitrogen to biochemical section microorganism, but traditional stripping technology can cause
Stripping tower blocks, and stripping goes out gas, these gases such as a large amount of volatile ammonia, phenol and hydrogen sulfide very big stink and poison
Property, can cause secondary pollution to environment, and due to there is a large amount of bio-refractory materials in percolate, it is biochemical after water outlet very
Difficulty reaches emission request.Membrane technology is to be retained the pollutant in waste water by membrane modules such as micro-filtration, nanofiltration, ultrafiltration, counter-infiltrations,
So as to reach the purpose to purify water.But membrane module maintenance, change frequently, cleaning is difficult, easily block, treating capacity fluctuation is larger,
Operating cost is high, while concentrated water caused by film process is difficult to handle, and easily produces secondary pollution.Research and probe is efficient, economical, full
The problem of garbage leachate treatment process of sufficient New emission standard is urgent need to resolve in garbage loading embeading processing procedure.
The content of the invention
It is contemplated that at least solves one of technical problem present in prior art.Therefore, the present invention provides a kind of rubbish
The processing system and method for rubbish percolate, it is therefore an objective to the treatment effeciency of biological treatment part is improved, reduces sludge reflux technique,
Concentrate, no secondary pollution are not produced after advanced treating, and makes the reduction of landfill leachate treatment expense.
To achieve these goals, the technical scheme taken of the present invention is：
A kind of processing system of percolate, including the pretreatment unit for removal of impurities, the pretreatment unit include
First order reaction sedimentation basin, one stage catalyzing oxidizing tower and the second order reaction sedimentation basin being sequentially connected, the system also include connecting successively
At biochemical treatment apparatus, two level catalysis oxidizing tower, removing heavy metals tower and the clear water reserviors connect, the second order reaction sedimentation basin and biochemistry
Manage device connection.
The biochemical treatment apparatus includes anaerobic reactor, A/O ponds and the UF membrane pond being sequentially connected, the second order reaction
Sedimentation basin is connected with anaerobic reactor.
The processing system also includes pre-acidified pond, the delivery port of the second order reaction sedimentation basin and the water inlet in pre-acidified pond
Mouth connection, the delivery port in institute's pre-acidified pond are connected with anaerobic reactor.
The processing system also includes being used for the accident for collecting sludge in first order reaction sedimentation basin and second order reaction sedimentation basin
Blow-down pit.
The processing system also includes being used for the sludge for concentrating sludge derived from accident blow-down pit and UF membrane pond
Concentration basin.
Preferably, the processing system also includes the collecting methane tank being connected with anaerobic reactor exhaust outlet.
The present invention also provides a kind of processing method of percolate, and the processing method is to first pass through percolate waste water
Particle suspensions clean and the pre-treatment step of one stage catalyzing oxidation, afterwards successively by biochemical treatment, two level catalysis oxidation at
After reason and heavy metal adsorption processing, then discharged after standing.
Methods described specifically comprises the following steps：
Step A, the particle suspensions of percolate waste water are removed by first order reaction sedimentation basin；
Step B, the water outlet of first order reaction sedimentation basin is imported into one stage catalyzing oxidizing tower and carries out catalytic oxidation；
Step C, the reacted water outlet of one stage catalyzing oxidizing tower is imported into second order reaction sedimentation basin and removes oil removal；
Step D, the reacted water outlet of second order reaction sedimentation basin is imported into anaerobic reactor and carries out Anaerobic Treatment, carried out afterwards
A/O ponds carry out biochemical degradation processing, then enter water-filling and activated sludge separating treatment by UF membrane pond；
Step E, the water outlet after the separating treatment of UF membrane pond is imported into two level catalysis oxidizing tower and carries out catalytic oxidation treatment；
Step F, the water outlet after two level catalytic oxidation treatment is imported in removing heavy metals tower and removes removing heavy metals, it is quiet through clear water reserviors
Postpone discharge.
Preferably, percolate is first collected to regulating reservoir with balanced water quality and quantity, is pumped to first order reaction sedimentation basin.
First order reaction sedimentation basin is coagulative precipitation tank in the step A, and the flocculant used is aluminium polychloride, polymerised sulphur
The one or more of sour iron, iron chloride, aluminum sulfate, ferrous sulfate etc., first order reaction sedimentation basin surface loading are 0.5~1m3/
m2H, hydraulic detention time are 3.5~4.5h.The purpose of adding flocculant is effectively to remove the colloidal suspended substance in waste water, is subtracted
Few suppression to subsequent biochemical system, flocculant dosage is PAC (aluminium polychloride) 100~350mg/L, PAM (polyacrylamide
Amine) 2~5mg/L.
One stage catalyzing oxidizing tower is catalytic ozonation tower in the step B, and the catalyst used is catalyzed for iron-based, manganese base
Agent, preferably manganese-based catalyst, the hydraulic detention time in one stage catalyzing oxidizing tower is 1~2h, and ozone concentration is 50~150mg/
m3, catalyst bed volume is 0.8~1.5 times of unit amount of inlet water.Advanced oxidation (one stage catalyzing oxidation) main function is
The biodegradability of water is improved, reduces the suppression to microorganism.
Second order reaction sedimentation basin is coagulating sedimentation in the step C, and second order reaction sedimentation basin surface loading is 0.5~1m3/
m2H, hydraulic detention time are 5.5~6.5h.It is organic that flocculant removal part difficult degradation is added by second order reaction sedimentation basin
Thing, flocculant dosage are PAC (aluminium polychloride) 50~100mg/L, PAM (polyacrylamide) 2~3mg/L.Sludge in pond
Collected through rectangular sedimentation tank to accident blow-down pit.
Methods described also includes being used to import the leading of anaerobic reactor to the reacted water outlet of second order reaction sedimentation basin
Enter the step of pre-acidified pond carries out pre-acidified processing, the pre-acidified tank waterpower residence time is 4h, and pH value of waste water is adjusted in pond into
Property.Larger molecular organicses in water are converted into by small organic molecule by acidification in pre-acidified pond, in order to anaerobic bacteria
Degraded is absorbed, the water outlet of pre-acidified pond is pumped to anaerobic reactor.
The anaerobic reactor is up flow type multistep treatment anaerobic reactor (UASB), and the COD in waste water is effectively removed,
Anaerobic reactor volumetric loading is 5~18kg COD/m3D or so, upflow velocity are 2~6m/h.Anaerobic reactor water outlet is certainly
A/O ponds (anoxic/aerobic) are flow to, by the further ammonia nitrogen and organic matter removed in waste water in A/O ponds；O ponds part mixed liquor
It is back to A ponds and ensures that nitrification, denitrification are smoothed out, the A tank waterpower residence times is 1.5d, and the O tank waterpower residence times are 2.5d.
The water outlet of A/O ponds flows automatically to medium sediment pool, further removes oil removal, medium sediment pool sludge reflux to A ponds, is arranged outside excess sludge, in sink
Pond water outlet is pumped into UF membrane pond, and UF membrane pond can use MBR Flat Membranes or hollow-fibre membrane.It is preferred that MBR Flat Membranes are used,
By the COD in aerobic removal waste water.
The MBR pool volumes load is 0.3~0.5kgBOD/m3D, dissolved oxygen be 2~3.5mg/L, sludge concentration be
4000~8000mg/L.The water outlet of MBR ponds is promoted to two level catalysis oxidizing tower.
Due to the organic matter and heavy metal of bio-refractory in percolate be present, therefore the water outlet after biochemical treatment needs
Further advanced treating.The two level catalysis oxidizing tower is preferably catalytic ozonation tower, and the catalyst used is iron-based, manganese base
Catalyst, preferably manganese-based catalyst, the hydraulic detention time in two level catalysis oxidizing tower are 1~2h, ozone concentration is 50~
150mg/L, catalyst bed volume are 1.2~1.8 times of unit amount of inlet water.The water outlet in MBR ponds is pumped into advanced oxidation tower, high
Level is oxidized to catalytic ozonation tower, can use up flow type multi-phase waste-water processing oxidation tower.
Water outlet is pumped into removing heavy metals adsorption tower after catalytic ozonation, except weight in removing heavy metals tower in the step F
Metal material is activated carbon, ceramic filter material, the one or more of natural minerals.It is preferred that use renewable ceramic material, adsorbent bed
Layer voidage is 40~65%, and bulk density is in 0.6~1.2g/cm3, hydraulic detention time is 1~2h, is passed through through adsorption tower water outlet
After clear water reserviors stand 1~2h, standard water discharge discharge.
The percolate is especially suitable for middle age caused by household refuse landfill sites or aging percolate.
Processing method of the present invention is mainly the group technology using pretreatment+biochemical treatment+advanced treating, below to each section
The effect of handling process, is described：
(1) pre-process.Pretreatment makes waste water using the method for coagulating sedimentation and catalytic ozonation by adding flocculant
In organic matter, ammonia nitrogen, metallics concentration reduce, reduce to subsequent biochemical processing inhibitory action, to improve waste water
Biodegradability.
(2) biochemical treatment.Biochemical treatment uses A2/ O (anaerobic/anoxic/aerobic)+MBR (membrane bioreactor) are to waste water
Carry out biochemical degradation.Anaerobism workshop section utilizes most of organic matter in anaerobe degradation water, and caused biogas can be used as biology
Matter using energy source, so as to reduce operating cost.Organic concentration is also higher in anaerobic effluent, need to further carry out biodegradation,
Simultaneously for ammonia nitrogen in waste water it is higher the characteristics of using A/O+MBR using nitrification, denitrifying bacterium by the mineralized nitrogen in waste water into nitrogen
Gas removes from water, and the ammonia nitrogen of MBR water outlets can ensure to reach discharge standard.
(3) advanced treating.Advanced treating uses catalytic ozonation+absorption.It is more difficult raw due to having in percolate
Change the material and heavy metal of degraded, be difficult to effectively remove these materials by pretreatment+biochemical treatment merely, it is therefore necessary to right
Bio-chemical effluent carries out advanced treating and can be only achieved discharge standard.The cardinal principle of catalytic ozonation technology is in oxidation system
Add transition metal ions, obvious catalytic effect can be produced to ozone oxidation, can with selfdecomposition of the catalysis ozone in water,
Increase caused OH concentration in water, so as to reduce the COD of difficult degradation in waste water.Advanced treating can be according to above bio-chemical effluent
Water quality survey ozone speculates amount, ensures that water outlet reaches emission request.
Beneficial effects of the present invention：The present invention in biological treatment part by using biological synergetic biochemical technology, depth oxygen
Change process part and use catalytic ozonation technology and heavy metal adsorption technology, further reduce COD and ammonia nitrogen, and a huge sum of money
Belong to, concentrate, no secondary pollution are not produced after advanced treating.This method investment operating cost is low, for the landfill of landfill age length
Field percolate integrated operation cost is in 15~35 yuan/t.
Brief description of the drawings
This specification includes the following drawings, and shown content is respectively：
Fig. 1 is the process chart of the present invention.
Embodiment
Below against accompanying drawing, by the description to embodiment, embodiment of the invention is made further details of
Explanation, it is therefore an objective to help those skilled in the art to have more complete, accurate and deep reason to design of the invention, technical scheme
Solution, and contribute to its implementation.
A kind of processing system of percolate, including the pretreatment unit for removal of impurities, pretreatment unit are included successively
First order reaction sedimentation basin, one stage catalyzing oxidizing tower and the second order reaction sedimentation basin of connection, the processing system also include being sequentially connected
Biochemical treatment apparatus, two level catalysis oxidizing tower, removing heavy metals tower and clear water reserviors, second order reaction sedimentation basin and biochemical treatment apparatus
Connection.Biochemical treatment apparatus includes anaerobic reactor, A/O ponds and the UF membrane pond being sequentially connected, and second order reaction sedimentation basin is with detesting
Oxygen reactor connects.
Absorb and degrade for the ease of anaerobic bacteria, processing system also includes pre-acidified pond, the delivery port of second order reaction sedimentation basin
It is connected with the water inlet in pre-acidified pond, the delivery port of acidification pool is connected with anaerobic reactor.
For the ease of being recycled to caused sludge in system, above-mentioned processing system also includes being used to collect one-level
The accident blow-down pit of sludge in reaction settling basin and second order reaction sedimentation basin.In addition, above-mentioned processing system also includes being used for thing
Therefore the sludge concentration tank that sludge derived from blow-down pit and UF membrane pond is concentrated.Sludge is after concentration basin is handled, Zhi Houzai
After sludge treating system is handled, sludge is transported outward into back landfill yard and handled.Preferably, above-mentioned processing system also include with
The collecting methane tank of anaerobic reactor exhaust outlet connection.It is easy to collect biogas, carries out follow-up utilization.
As shown in figure 1, the present invention also provides a kind of processing method of percolate, the processing method is that percolate gives up
Water first passes through particle suspensions removal of impurities and the pre-treatment step of one stage catalyzing oxidation, is given birth to successively using anaerobism, A/O and MBR
Change is handled, and is finally catalyzed advanced oxidation using two level and absorption carries out advanced treating, the water quality after processing meets discharge standard.
Above-mentioned processing method specifically comprises the following steps：
Step A, the particle suspensions of percolate waste water are removed by first order reaction sedimentation basin；
Step B, the water outlet of first order reaction sedimentation basin is imported into one stage catalyzing oxidizing tower and carries out catalytic oxidation, raising can give birth to
The property changed；
Step C, the reacted water outlet of one stage catalyzing oxidizing tower is imported into second order reaction sedimentation basin and removes remaining levitation thing；
Step D, the reacted water outlet of second order reaction sedimentation basin is imported into anaerobic reactor and carries out Anaerobic Treatment, carried out afterwards
A/O ponds carry out biochemical degradation processing, then enter water-filling and activated sludge separating treatment by UF membrane pond, improve living in aerobic section
Property sludge concentration；
Step E, the water outlet after the separating treatment of UF membrane pond is imported into two level catalysis oxidizing tower and carries out catalytic oxidation treatment, entered
One step reduces COD；
Step F, the water outlet after two level catalytic oxidation treatment is imported in removing heavy metals tower and removes removing heavy metals, it is quiet through clear water reserviors
Postpone, qualified discharge.
This method investment operating cost is low, for landfill age length Landfill Leachate integrated operation cost 15~
35 yuan/t.
It is described in detail below by specific preferred embodiment：
Embodiment 1
Pilot scale, raw water COD are carried out to Pingxiang Jiangxi's refuse landfill percolatecrFor 4000mg/L or so, add wadding
Solidifying agent PAC is 150mg/L, PAM 2mg/L, first order reaction sedimentation basin surface loading 0.5m3/m2H, hydraulic detention time are
4h, one-level advanced oxidation tower (catalytic ozonation tower), ozone dosage 75mg/m are imported afterwards3, hydraulic detention time is
1h, it is then introduced into second order reaction sedimentation basin, second order reaction sedimentation basin surface loading 0.5m3/m2H, hydraulic detention time 6h,
Pre-acidified pond is pumped into afterwards, pre-acidified time 4h, adjusts pH value of waste water to be pumped into anaerobic reactor, the present embodiment is used to 7 or so
Anaerobic reactor be UASB (up flow type multistage anaerobic reactor), anaerobic reactor volumetric loading 8kgCOD/m3D, rise
Flow velocity is 3m/h, and the A tank waterpower residence times are 1.5d, and the O tank waterpower residence times are 2.5d, MBR pool volume loads 0.3kgBOD/
m3D, dissolved oxygen 2.2mg/L, sludge concentration 6000mg/L or so, MBR ponds water outlet COD are 180mg/L or so, the water outlet of MBR ponds
Secondary ozone catalysis oxidizing tower is pumped into, catalytic ozonation tower aoxidizes for up flow type multiphase wastewater treatment used by the present embodiment
Tower, hydraulic detention time 1h, oxygen dosage are 150mg/m3, catalyst bed layer height 2.5m, secondary ozone catalysis oxidizing tower
(advanced oxidation) water outlet enters removing heavy metals adsorption tower, and adsorbent is renewable ceramic material, adsorption bed voidage 40%,
Bulk density is in 0.6g/cm3, hydraulic detention time 1.5h, clear water reserviors water outlet CODcr85mg/L or so, ammonia nitrogen 12mg/L or so,
Indices reach discharge standard GB16889-2008.
Embodiment 2
Pilot scale research, raw water CODcr 7000mg/L or so is carried out to Pingxiang Jiangxi's refuse landfill percolate,
It is 350mg/L, PAM 5mg/L, first order reaction sedimentation basin surface loading 1m to add flocculant PAC3/m2H, hydraulic detention time are
4h, it is 150mg/m to import one-level advanced oxidation tower ozone dosage afterwards3, hydraulic detention time 1h, it is anti-to be then introduced into two level
Answer sedimentation basin, second order reaction sedimentation basin surface loading 1m3/m2H, hydraulic detention time 6h, pre-acidified pond is pumped into afterwards, in advance
Acidificatoin time 4h, tune pH value of waste water to 7 or so are pumped into anaerobic reactor, and anaerobic reactor is UASB used by the present embodiment
(up flow type multistage anaerobic reactor), anaerobic reactor volumetric loading 15kgCOD/m3D, upflow velocity 6m/h, A tank waterpower
Residence time is 1.5d, and the O tank waterpower residence times are 2.5d, MBR pool volume loads 0.4kgBOD/m3D, dissolved oxygen 2.8mg/
L, sludge concentration 8000mg/L or so, MBR water outlet COD are 380mg/L or so, and MBR water outlets are pumped into secondary ozone catalysis oxidizing tower,
Catalytic ozonation tower is up flow type multi-phase waste-water processing oxidation tower used by the present embodiment, hydraulic detention time 1h, oxygen
Dosage is 250mg/m3, catalyst bed layer height 2.5m, secondary ozone catalysis oxidizing tower (advanced oxidation) water outlet, which enters, removes weight
Metal adsorption tower, adsorbent are renewable ceramic material, and adsorption bed voidage is 60%, and bulk density is in 1.2g/cm3, water
Power residence time 1.5h, clear water reserviors water outlet CODcr95mg/L or so, ammonia nitrogen 12mg/L or so, indices reach discharge standard
GB16889-2008。
The present invention is exemplarily described above in association with accompanying drawing.Obviously, present invention specific implementation is not by above-mentioned side
The limitation of formula.As long as employ the improvement of the various unsubstantialities of inventive concept and technical scheme of the present invention progress；Or not
It is improved, the above-mentioned design of the present invention and technical scheme are directly applied into other occasions, in protection scope of the present invention
Within.
Claims (10)
1. a kind of processing system of percolate, including the pretreatment unit for removal of impurities, it is characterised in that the pretreatment
Device includes first order reaction sedimentation basin, one stage catalyzing oxidizing tower and the second order reaction sedimentation basin being sequentially connected, and the system is also wrapped
Include the biochemical treatment apparatus being sequentially connected, two level catalysis oxidizing tower, removing heavy metals tower and clear water reserviors, the second order reaction sedimentation basin
It is connected with biochemical treatment apparatus.
2. the processing system of percolate according to claim 1, it is characterised in that the biochemical treatment apparatus include according to
Anaerobic reactor, A/O ponds and the UF membrane pond of secondary connection, the second order reaction sedimentation basin are connected with anaerobic reactor.
3. the processing system of percolate according to claim 2, it is characterised in that the processing system also includes pre-sour
Change pond, the delivery port of the second order reaction sedimentation basin is connected with the water inlet in pre-acidified pond, and the delivery port in institute's pre-acidified pond is with detesting
Oxygen reactor connects.
4. according to the processing system of any one of the claim 1-3 percolates, it is characterised in that the processing system is also
Including the accident blow-down pit for collecting sludge in first order reaction sedimentation basin and second order reaction sedimentation basin.
5. the processing system of percolate according to claim 4, it is characterised in that the processing system also includes being used for
The sludge concentration tank concentrated to sludge derived from accident blow-down pit and UF membrane pond.
6. a kind of processing method of percolate, it is characterised in that the processing method is to first pass through percolate waste water
The pre-treatment step of the removal of impurities of grain suspension and one stage catalyzing oxidation, afterwards successively by biochemical treatment, two level catalytic oxidation treatment
After heavy metal adsorption processing, then discharged after standing.
7. the processing method of percolate according to claim 6, it is characterised in that methods described specifically includes following step
Suddenly：
Step A, the particle suspensions of percolate waste water are removed by first order reaction sedimentation basin；
Step B, the water outlet of first order reaction sedimentation basin is imported into one stage catalyzing oxidizing tower and carries out catalytic oxidation；
Step C, the reacted water outlet of one stage catalyzing oxidizing tower is imported into second order reaction sedimentation basin and removes oil removal；
Step D, the reacted water outlet of second order reaction sedimentation basin is imported into anaerobic reactor and carries out Anaerobic Treatment, carry out A/O afterwards
Pond carries out biochemical degradation processing, then enters water-filling and activated sludge separating treatment by UF membrane pond；
Step E, the water outlet after the separating treatment of UF membrane pond is imported into two level catalysis oxidizing tower and carries out catalytic oxidation treatment；
Step F, the water outlet after two level catalytic oxidation treatment is imported in removing heavy metals tower and removes removing heavy metals, after clear water reserviors are stood
Discharge.
8. the processing method of percolate according to claim 7, it is characterised in that first order reaction is sunk in the step A
Shallow lake pond is coagulative precipitation tank, and the flocculant used is aluminium polychloride, bodied ferric sulfate, iron chloride, aluminum sulfate, ferrous sulfate etc.
One or more, first order reaction sedimentation basin surface loading is 0.5~1m3/m2H, hydraulic detention time are 3.5~4.5h.
9. the processing method of percolate according to claim 8, it is characterised in that methods described also includes being used for two
The reacted water outlet of order reaction sedimentation basin imports the step of pre-acidified pond carries out pre-acidified processing before anaerobic reactor is imported,
The pre-acidified tank waterpower residence time is 4h, and pH value of waste water is adjusted in pond to neutrality.
10. the processing method of percolate according to claim 7, it is characterised in that the MBR pool volumes load is
0.3~0.5kgBOD/m3D, dissolved oxygen be 2~3.5mg/L, sludge concentration be 4000~8000mg/L.
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| CN111285554A (en) * | 2020-03-21 | 2020-06-16 | 杭州师范大学钱江学院 | Method for deep purification treatment of landfill leachate |
| CN112939361A (en) * | 2021-02-05 | 2021-06-11 | 四川国润和洁环境科技有限公司 | Method for treating landfill leachate |
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