CN105060607A - Landfill leachate treatment method - Google Patents
Landfill leachate treatment method Download PDFInfo
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- CN105060607A CN105060607A CN201510416277.7A CN201510416277A CN105060607A CN 105060607 A CN105060607 A CN 105060607A CN 201510416277 A CN201510416277 A CN 201510416277A CN 105060607 A CN105060607 A CN 105060607A
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- 238000000034 method Methods 0.000 title claims abstract description 110
- 239000000149 chemical water pollutant Substances 0.000 title abstract 5
- 230000008569 process Effects 0.000 claims abstract description 68
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 40
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 23
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 18
- 239000000126 substance Substances 0.000 claims abstract description 18
- 238000004062 sedimentation Methods 0.000 claims abstract description 16
- 230000003647 oxidation Effects 0.000 claims abstract description 13
- 238000004659 sterilization and disinfection Methods 0.000 claims abstract description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 239000010802 sludge Substances 0.000 claims description 27
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 26
- 229910052757 nitrogen Inorganic materials 0.000 claims description 19
- 239000012028 Fenton's reagent Substances 0.000 claims description 17
- 239000006228 supernatant Substances 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000010865 sewage Substances 0.000 claims description 10
- 238000001556 precipitation Methods 0.000 claims description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 230000000813 microbial effect Effects 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 238000002203 pretreatment Methods 0.000 claims description 5
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 238000005189 flocculation Methods 0.000 claims description 4
- 230000016615 flocculation Effects 0.000 claims description 4
- 150000002978 peroxides Chemical class 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- 239000011150 reinforced concrete Substances 0.000 claims description 3
- 239000007800 oxidant agent Substances 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 239000010813 municipal solid waste Substances 0.000 abstract description 12
- 230000001105 regulatory effect Effects 0.000 abstract description 2
- 230000003311 flocculating effect Effects 0.000 abstract 1
- 238000001179 sorption measurement Methods 0.000 abstract 1
- 239000012528 membrane Substances 0.000 description 19
- 238000001223 reverse osmosis Methods 0.000 description 16
- 238000001728 nano-filtration Methods 0.000 description 15
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 14
- 239000007788 liquid Substances 0.000 description 12
- 230000000630 rising effect Effects 0.000 description 11
- 230000000694 effects Effects 0.000 description 8
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- 239000004571 lime Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
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- 238000012546 transfer Methods 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
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- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
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- 239000012153 distilled water Substances 0.000 description 2
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to a landfill leachate treatment method. The landfill leachate treatment method comprises following steps in sequence: pretreatment comprising steps of flocculating sedimentation, ammonia stripping, ammonia adsorption and processes of regulating pH and adjusting the temperature of the leachate to be not lower than 15 DEG C, primary anoxic-aerobic biological treatment, primary sedimentation treatment, chemical oxidation treatment, secondary sedimentation treatment, secondary anoxic-aerobic biological treatment, tertiary sedimentation treatment and disinfection treatment. According to the landfill leachate treatment method, a physicochemical and biochemical combined treatment system is adopted based on the characteristics of the municipal solid waste landfill site leachate, so that stable and efficient operation of the whole system is guaranteed, and the landfill leachate reaches the emission standard of Standard for Pollution Control on the Landfill Site Of Municipal Solid Waste (GB16889-2008) finally.
Description
Technical field
The present invention relates to a kind for the treatment of process of application of city life garbage sanitary filling field percolate, belong to environmental engineering technical field of sewage.
Background technology
Percolate refers to and derives from the moisture that in refuse landfill, rubbish itself contains, the sleet water entering landfill yard and other moisture, the saturation moisture capacity of deduction rubbish, overburden layer, and a kind of high-concentration waste water experiencing waste layer and overburden layer and formed.The ammonia nitrogen of high density is one of water quality characteristic of Leachate site, and Leachate site ammonia nitrogen concentration is generally from tens to thousands of milligrams per liter.According to the Leachate site Regular of Water Quality Variation that domestic refuse landfill produces, along with the prolongation of landfill time, the ammonia nitrogen concentration of Leachate site has the trend of rising, and biodegradability can decline.
Word is high should the main technique of first class be had several as follows between 3.5 millimeters to 4.5 millimeters:
1. membrane bioreactor (MBR)+nanofiltration (NF)+reverse osmosis (RO) technique, adopts the utility model patent of this technique number to be: ZL200810056984.X;
2. membrane bioreactor (MBR)+nanofiltration (NF) technique, adopts the Authorization Notice No. of the patent of this technique to be: CN101244880B;
3. ammonia aeration+membrane bioreactor (MBR)+nanofiltration (NF) technique, adopts the patent of invention of this technique number to be: ZL200610034517.8;
The main technique of second largest class is as follows:
Disc tube reverse osmosis (dt-ro) film (DTRO) technique, adopts the patent of invention of this technique number to be: ZL200510102945.5;
The main technique of the third-largest class is as follows:
Evaporation+ion exchange process, adopts the patent of invention of this technique number to be: ZL200710031584.9;
The fourth-largest class main technique is as follows:
Biological nitration/denitrification+Fenton oxidation (Fenton)+BAF (BAF) technique, adopts the patent of invention of this technique number to be: ZL200510035132.9.
First class treatment process is the technique be most widely used at present, and the nanofiltration used in such technique (NF) and reverse osmosis (RO) they are a kind of physical sepn technique, and reverse osmosis membrane aperture is little of nano level, under pressure, and H
2o molecule can pass through RO film, and the impurity such as inorganic salt, heavy metal ion, organism, colloid, bacterium, virus in percolate cannot pass through RO film, the material permeance that nanofiltration membrane allows relative molecular weight to be less than 200, ultra-filtration membrane allows the larger material of relative molecular weight to pass through.In first class treatment process, nanofiltration membrane and ultra-filtration membrane are to the NO in water
3 -, NO
2 -, NH
3, NH
4 +retain efficiency extremely low; Only have reverse osmosis membrane to retain and live in state four kinds of ions.Therefore, do not use in the existing membrane process craft of reverse osmosis, the important task of the removal of total nitrogen is all entrusted give in MBR nitrated/denitrification process, if the not enough or biological nitration/denitrification of carbon source occurs abnormal in waste water, then there will be the situation that total nitrogen exceeds standard.Therefore, all add reverse osmosis membrane assembly in current membrane treatment process, up to standard to guarantee water outlet total nitrogen.Membranous system all produces concentrated solution, and nanofiltration system produces the concentrated solution of about 15%, and reverse osmosis system produces about 15% concentrated solution.
Second largest class treatment process is the side that the pollution substances such as the organism in waste water, ammonia nitrogen are trapped in film by application butterfly tubular type reverse osmosis membrane (DTRO) assembly, H
2o molecule arrives the opposite side of film through reverse osmosis membrane, thus obtains clean water outlet.This technique is pure physical separating process, and the concentrated solution adopting this kind of technique to produce is greater than 25% for the treatment of capacity usually.
The third-largest class technique: evaporation+ion exchange process, percolate heating is evaporated by this technique, produce the distilled water of about 90% and the evaporation concentration liquid of 10%, the pollution substances such as the organism in percolate, heavy metal are concentrated in the concentrated solution of 10%.The distilled water collected is removed after ammonia nitrogen can reach emission standard through storng-acid cation exchange resin again.
The maximum feature of the fourth-largest class treatment process does not use the membrane modules such as ultra-filtration membrane (UF), nanofiltration membrane (NF), reverse osmosis membrane (RO), therefore, do not have concentrated solution to produce.Such technique adopts the total nitrogen in traditional biological nitration, denitrification removal percolate, adopts (Fenton) to be oxidized coordinate subsequent biochemical technique to be removed to the organic pollutant of difficult degradation in percolate.
Common four large class Technology Economic contrast are in table 1:
The large class treatment process technology and economy comparison of table 1 four
The difficult point of percolate process has two aspects: one is remove total nitrogen, and another reduces ton water treatment running cost.
As can be seen from the above table, although first, second, third large class treatment process treatment effect is stablized, effluent quality is excellent, but total investment of engineering and ton cost of water treatment high, high investment and working cost bring very heavy economical load to the operation of landfill yard.The fourth-largest class technique has that total investment of engineering is low, the advantage of ton water running low cost, but the operation for the treatment of facility affected by environment large, operational administrative is more complicated.When ambient temperature sharply changes, the fourth-largest class treatment process can fluctuate larger in total nitrogen removal efficiency.
Summary of the invention
The technical problem to be solved in the present invention overcomes the deficiencies in the prior art, provides that a kind of construction investment is low, running cost is low, treatment effect is good, applied range, easily is automated and controls and the garbage percolation liquid treating system of operation.
For solving the problems of the technologies described above, the technical scheme that the present invention proposes is a kind for the treatment of process of percolate, see Fig. 1, comprise pre-treatment, an Anoxybiotic-aerobic biologic process, primary sedimentation process, chemical oxidation treatment, secondary sedimentation process, the process of secondary Anoxybiotic-aerobic biologic, three precipitation process successively and disinfect technique, each treatment process detailed step is as follows:
(1) pre-treatment
Pre-treatment comprises the following steps successively:
(1) flocculation sediment:
In percolate, add Ferric Salt Flocculants, carry out precipitation process, sedimentation time is 1 ~ 3 hour; When precipitating, NaOH can be added as required in right amount and regulate percolate pH to be 7 ~ 9.
(2) one times pH value regulates:
Percolate supernatant liquor after precipitation process flows into PH equalizing tank, adds NaOH or lime, regulates its pH value to be 10.5 ~ 11.5, and while adjust ph, the temperature of adjustment percolate is not less than 10 DEG C; When envrionment temperature is lower, by passing into appropriate high temperature saturated vapor in percolate, temperature requirement is reached to percolate heating.
(3) stripping ammonia nitrogen:
To the percolate pump delivery after processing be regulated to Ammonia blowing-out tower through pH value, percolate flows from the top of stripping tower to tower bottom, and air flows from tower bottom to top of tower, the ammonia nitrogen in stripping percolate, and the vapour-liquid ratio in stripping tower is 2000 ~ 3500; Flow out from Ammonia blowing-out tower top containing ammonia-nitrogen desorption tail gas, percolate flows out bottom Ammonia blowing-out tower.
(4) ammonia nitrogen is absorbed:
Enter bottom ammonia absorber containing ammonia-nitrogen desorption tail gas, tail gas absorbs high-altitude qualified discharge after ammonia nitrogen through acid.
(5) secondary pH value regulates:
Percolate after stripping process flows into PH equalizing tank, and add sulfuric acid, adjust ph is 7 ~ 8.5, and adjustment percolate temperature is not less than 15 DEG C; When envrionment temperature is lower, appropriate high temperature saturated vapor can be passed into temperature requirement is reached to percolate heating.
(2) Anoxybiotic-aerobic biologic process
Enter anaerobic-aerobic pond through pretreated percolate, load elastic filler in pond, microorganic adhesion forms microbial film in elastic filler;
Control dissolved oxygen content in anoxic pond and be not more than 0.4mg/L, anoxic pond hydraulic detention time 2.4 ~ 7 hours;
In Aerobic Pond, dissolved oxygen content is at 2 ~ 5mg/L, hydraulic detention time 70 ~ 140 hours; Nitrobacteria is utilized by nitride converted for nitrate under aerobic condition;
Reflux pump is set, by the mixed-liquor return containing nitric nitrogen in Aerobic Pond to anoxic pond, control of reflux ratio is 4 ~ 10, and phegma carries out denitrification process in denitrification pond, utilize denitrifying bacterium that nitrate reduction is become gaseous nitrogen under anoxic conditions, remove the total nitrogen in waste water and BOD.
(3) primary sedimentation process
Percolate after anaerobic-aerobic process precipitates through settling tank, and supernatant liquor enters chemical oxidation advanced treatment.
(4) chemical oxidation advanced treatment
The supernatant liquor added after the process of sulfuric acid adjustment primary sedimentation makes its pH=3, carries out chemical oxidation advanced treatment.
The chemical oxidizing agent that chemical oxidation treatment adopts is Fenton reagent, Fe in described Fenton reagent
2+with H
2o
2mass ratio be 0.75: 1 ~ 1.2: 1, the add-on of described Fenton reagent is that in Fenton reagent, in hydrogen peroxide and pending water, COD mass ratio is 0.5: 1 ~ 2.4: 1, and the reaction times is 0.5 ~ 1.5 hour.
(5) secondary sedimentation process
Water outlet through Fenton reagent process adds NaOH and regulates its pH value to 6 ~ 8; Add coagulating agent, percolate is flocculation sediment in settling tank, hydraulic detention time 1 ~ 2 hour; Water after precipitation enters the process of secondary anaerobic-aerobic workshop section, and coagulating agent can be PAC (polymerize aluminum chloride).
(6) secondary Anoxybiotic-aerobic biologic process
Anoxybiotic-aerobic biologic process is carried out in reinforced concrete sewage pond or in Steel Vessel, and load elastic filler in sewage lagoon or Steel Vessel, microorganic adhesion forms microbial film in elastic filler.
The dissolved oxygen content controlling anoxic operation is not more than 0.4mg/L, anoxic pond hydraulic detention time 1.5 ~ 3 hours;
Aerobic in-process dissolved oxygen content at 2 ~ 5mg/L, hydraulic detention time 30 ~ 60 hours;
By the mixed-liquor return of aerobic in-process to anoxic operation, control of reflux ratio is 3 ~ 6, and phegma carries out denitrification process in denitrification pond, utilizes denitrifying bacterium that nitrate reduction is become gaseous nitrogen under anoxic conditions, removes the total nitrogen in waste water and BOD.
(7) three precipitation process
Percolate after the process of secondary Anoxybiotic-aerobic biologic precipitates in settling tank, and supernatant liquor enters disinfects.
(8) disinfect
Supernatant liquor after three precipitations enters sterilization pool, uses disinfection by chlorine dioxide process.
Can also have sludge treatment technique, mud is backfilled to landfill yard after being dewatered by pressure filter, and pressing filtering liquid is back to water inlet place of percolate former water and processes.
As further improvement, a part of mud in sludge sump is back to two anoxic pond respectively, according to nitrogen dynamics formula determination return sludge ratio, effectively can control activated sludge concentration, reduces mud handling capacity.
Getting Changsha Mark Reserved percolate from garbage filling field is that pilot plant test is carried out in water inlet, and treatment capacity is 300L/d, influent quality BOD
5(3500mg/L), CODCr (10000mg/L), SS (500mg/L), NH
3-N (1500mg/L), TN (1800mg/L), pH (6.0-8.5) and colourity concentration (1100 times), adopt the process test that technical solution of the present invention is carried out 12 months by a definite date, effluent quality mean value is BOD after treatment
5(25mg/L), CODCr (90mg/L), SS (25mg/L), NH
3-N (20mg/L), TN (35mg/L), pH (6.0-8.5) and colourity concentration (35 times), as shown in table 2.
Table 2 garbage leachate treatment station influent quality
| Sequence number | Pollutent title | Unit | Influent quality | Effluent quality | Clearance (%) |
| 1 | BOD 5 | mg/L | 3500 | 25 | 99.29 |
| 2 | COD Cr | mg/L | 10000 | 90 | 99.10 |
| 3 | SS | mg/L | 500 | 25 | 95.00 |
| 4 | NH 3-N | mg/L | 1500 | 20 | 98.67 |
| 5 | TN | mg/L | 1800 | 35 | 98.06 |
| 6 | pH | - | 6.0-8.5 | 6.0-8.5 | |
| 7 | Colourity | Extension rate | 1100 | 35 | 96.8 |
Adopt the clearance of technical solution of the present invention to above typical pollution factor high as can be seen from Table 2, wherein for the typical high density BOD of percolate from garbage filling field
5, COD, NH
3the clearance of-N and TN is respectively up to 99.29%, 99.10%, 98.67% and 98.06.Therefore the application of this technique can reach the pollutant emission mass concentration limit value of " household refuse landfill sites Environmental capacity standard " (GB16889-2008).Compared with existing treatment process, the present invention has following beneficial effect:
1, adopt molysite to carry out coagulation pretreatment, can significantly reduce subsequent technique processing cost;
2, owing to have employed heating temperature adjustment, biological treatment is made to be subject to such environmental effects less, stable;
3, total investment of engineering, maintenance cost and ton cost of water treatment are lower than nanofiltration (NF) and reverse osmosis (RO) technique, butterfly tubular type reverse osmosis membrane (DTRO) technique and evaporation+ion exchange process;
4, operation stability is better than traditional biological nitration, denitrification process, simple to operate, administrative convenience.
Construction costs of the present invention is low, Operation and Maintenance is simple, follow-up expense is few, and ton cost of water treatment is low; After sewage disposal, discharge meets national standard, and treatment effect is good; Go out water treatment up to standard.Whole Sewage treatment systems simple and convenient management, the present invention can be widely used in percolate from garbage filling field, sanitary sewage disposal.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention
Fig. 2 is specific embodiment of the invention schematic diagram
In Fig. 2:
A---settling tank; The former water water inlet pipe of 1-percolate, 2-molysite adds pipeline, and 3-alkali adds pipeline; 4-settling tank rising pipe; 5-sludge from sedimentation tank pipe;
B---pH adjusts pond; 6-steam-heated pipe line, 7-alkali adds pipeline;
C---Ammonia blowing-out tower; Topping-up pump, 9-percolate transfer lime, 10-ammonia-containing exhaust transfer lime, 11-percolate delivery pipe, 43-inlet mouth;
D---ammonia absorber; 12-cleaning of off-gas delivery pipe;
E---pH adjusts pond; 13-H2SO4 adds pipe; 14-steam-heated pipe line;
F-_ anoxic pond; 15-percolate water inlet pipe;
G---Aerobic Pond; 16-air line; 17-mixed-liquor return pipe;
H---settling tank; 18-supernatant liquor rising pipe, 19-precipitating sludge shore pipe;
I---Fenton chemical oxidation reaction device; 20-H2SO4 adds pipe, and 21-Fenton reagent adds pipe, 22-reflux pump, 23-reflux line, 24-Fenton oxidation reactor rising pipe;
J---settling tank; 25-NaOH adds pipe, and 26-PAC adds pipe, 27-supernatant liquor rising pipe, 28-precipitating sludge shore pipe;
K---anoxic pond; 30-nitrification tank internal reflux pipe;
L---Aerobic Pond; 29-air line;
M---settling tank; 31-supernatant liquor rising pipe, 32-mud discharging pipe, 33-sludge pump, 34-sludge pipe;
N---sterilization pool; 35-dioxide peroxide adds pipe, 36-delivery pipe;
O---mud storage pool; 37-reflux sludge tube, 38-reflux sludge tube;
P---sludge filter press; 39-sludge pump enters mud pipe; 40-sludge pump; 41-pressure filter enters mud pipe, 42-pressing filtering liquid delivery pipe.
Embodiment
The embodiment of method for treating garbage percolation liquid of the present invention is described below in conjunction with Fig. 2:
Percolate enters settling tank A by the former water water inlet pipe 1 of percolate, add pipe 2 through molysite and in the percolate in the former water water inlet pipe 1 of percolate, add Ferric Salt Flocculants by line mixer, simultaneously add pipeline 3 by alkali as required and add NaOH in right amount to the former water water inlet pipe 1 of percolate and regulate percolate pH to be 7 ~ 9.The sedimentation time of percolate in settling tank A is 1 ~ 3 hour.The mud of settling tank A enters mud storage pool O through sludge from sedimentation tank pipe 5, the water outlet of settling tank A enters pH by settling tank rising pipe 4 and adjusts pond B, in this pond, add pipeline 7 by alkali add NaOH and regulate percolate pH to be 10.5 ~ 11.5, while adjustment pH, in pH adjustment pond B, pass into appropriate high temperature saturated vapor by steam-heated pipe line 6 according to the temperature of the percolate measured to heat percolate, the temperature of the percolate before making to enter stripping tower is not less than 10 DEG C.The percolate that pH adjusts in the B of pond is delivered to Ammonia blowing-out tower C by topping-up pump 8 through percolate transfer lime 9, percolate flows from the top of Ammonia blowing-out tower C to tower bottom, air flows from tower bottom to top of tower, ammonia nitrogen in stripping percolate, vapour-liquid ratio in Ammonia blowing-out tower C is 2000 ~ 3500, stripping tail gas containing ammonia enters bottom ammonia absorber D from Ammonia blowing-out tower C tower top by ammonia-containing exhaust transfer lime 10, air enters the bottom, bottom of Ammonia blowing-out tower C from inlet mouth 43, percolate enters pH by percolate delivery pipe 11 and adjusts pond E bottom Ammonia blowing-out tower C, H is passed through in this pond
2sO
4add pipe 13 and add H
2sO
4regulate the pH of percolate between 7 ~ 8.5, pass into appropriate high temperature saturated steam according to the temperature of percolate in pond through steam-heated pipe line 14 simultaneously and percolate is heated, make the temperature of the percolate entering anoxic pond F be not less than 15 DEG C.
The percolate that pH adjusts in the E of pond enters anoxic pond F through percolate water inlet pipe 15.Load elastic filler in anoxic pond F, microorganic adhesion forms microbial film in elastic filler; Control dissolved oxygen content in anoxic pond and be not more than 0.4mg/L.Arrange aerating apparatus in Aerobic Pond G, gas enters from air line 16, and in Aerobic Pond G, dissolved oxygen content controls at 2 ~ 5mg/L.Nitric nitrogen is oxidized under the effect of the nitrobacteria of the ammonia nitrogen in percolate in Aerobic Pond G and nitrite bacteria.Nitric nitrogen in Aerobic Pond G is back to anoxic pond F by mixed-liquor return pipe 17, under the effect of the denitrifying bacterium in anoxic pond F, denitrification process occurs, and removes the total nitrogen in percolate and BOD.
Percolate is after the reaction of first step anaerobic-aerobic, enter settling tank H from Aerobic Pond G and carry out solid-liquid separation, the supernatant liquor of settling tank H enters Fenton chemical oxidation reaction device I by No. 18, supernatant liquor rising pipe, and the mud of settling tank H enters mud storage pool O by precipitating sludge shore pipe 19.
The oxygenant that Fenton chemical oxidation reaction device I adopts is Fenton reagent, and Fenton reagent is hydrogen peroxide and catalyst Fe
2+the oxidation system formed, Fe in Fenton reagent
2+with H
2o
2mass ratio be 0.75: 1 ~ 1.2: 1, in Fenton reagent, in hydrogen peroxide and pending water, COD mass ratio is 0.5: 1 ~ 2.4: 1, and Fenton reagent adds pipe 21 by Fenton reagent and adds in pending percolate by line mixer, H
2sO
4by H
2sO
4adding pipe 20 adds in pending percolate by line mixer, regulates the pH=3 of percolate.For enhancement process effect, reflux pump 22 is set Fenton chemical oxidation reaction device I upper flow is led back bottom.
The water outlet of Fenton chemical oxidation reaction device I enters settling tank J through Fenton oxidation reactor rising pipe 24, add pipe 25 by NaOH and add pH to 7 ~ 8.5 in NaOH equalizing tank, add pipe 26 by PAC and add PAC (polymerize aluminum chloride) coagulating agent, percolate is flocculation sediment in settling tank J, supernatants after precipitation enters anoxic pond K by supernatant liquor rising pipe 27, and the mud of settling tank J enters mud storage pool O by No. 28 pipelines.
Load elastic filler in anoxic pond K, microorganic adhesion forms microbial film in elastic filler; Control dissolved oxygen content in anoxic pond K and be not more than 0.4mg/L.Arrange aerating apparatus in Aerobic Pond L, gas enters from air line 29, and in Aerobic Pond, dissolved oxygen content controls at 2 ~ 5mg/L.Nitric nitrogen is oxidized under the effect of the nitrobacteria of the ammonia nitrogen in percolate in Aerobic Pond L and nitrite bacteria.Nitric nitrogen in Aerobic Pond L flow to anoxic pond K by No. 30 back of pipelines, in anoxic pond K denitrifying bacterium effect under there is denitrification process, remove the total nitrogen in percolate and BOD.
Percolate is after the reaction of second stage anaerobic-aerobic, enter settling tank M from the top water outlet of Aerobic Pond L and carry out solid-liquid separation, the supernatant liquor of settling tank M enters sterilization pool N by supernatant liquor rising pipe 31, and the mud of settling tank M enters mud storage pool O via sludge pump 33 by sludge pipe 34 by mud discharging pipe 32.
Sterilization pool N adds pipe 35 through dioxide peroxide and adds dioxide peroxide and carry out disinfection, and sterile-processed water is by delivery pipe 36 qualified discharge.
A mud part in mud storage pool O is back to anoxic pond F, anoxic pond K respectively by reflux sludge tube 37, reflux sludge tube 38, excess sludge enters mud pipe 39 through sludge pump, sludge pump 40, pressure filter enter mud pipe 41, dewatered by pressure filter P, mud after dehydration is backfilled to landfill yard, and the pressing filtering liquid that sludge dewatering produces is back to the former water water inlet pipe 1 of percolate by pressing filtering liquid delivery pipe 42 and processes.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (9)
1. a treatment process for percolate, is characterized in that: comprise pre-treatment, an Anoxybiotic-aerobic biologic process, primary sedimentation process, chemical oxidation treatment, secondary sedimentation process, the process of secondary Anoxybiotic-aerobic biologic, three precipitation process successively and disinfect technique.
2., by the treatment process of a kind of percolate according to claim 1, it is characterized in that:
Described pre-treatment comprises the following steps successively:
Molysite is added, flocculation, precipitation process in percolate;
In percolate supernatant liquor after treatment, add NaOH regulates pH to be 10.5 ~ 11.5, while adjustment pH, heat percolate by passing into appropriate high temperature saturated vapor in percolate, the temperature of the percolate before making to enter stripping tower is not less than 10 DEG C;
Percolate pump delivery is after treatment gone out ammonia to Ammonia blowing-out tower stripping;
Ammonia-containing exhaust enters ammonia absorber, and tail gas is high altitude discharge after acid absorbs;
In the percolate after stripping process, add sulfuric acid, regulate pH to be 7 ~ 8.5, pass into appropriate high temperature saturated vapor according to the temperature of percolate and it is heated, make percolate temperature be not less than 15 DEG C.
3., by the treatment process of a kind of percolate according to claim 1, it is characterized in that:
A described Anoxybiotic-aerobic biologic process is carried out in reinforced concrete sewage pond, and install elastic filler in sewage lagoon, microorganic adhesion forms microbial film in elastic filler;
Control dissolved oxygen content in anoxic pond and be not more than 0.4mg/L, anoxic pond hydraulic detention time 12 ~ 24 hours;
Controlling dissolved oxygen content in Aerobic Pond is 2 ~ 5mg/L, hydraulic detention time 70 ~ 140 hours;
By the mixed-liquor return in Aerobic Pond to anoxic pond, control of reflux ratio is 4 ~ 10.
4., by the treatment process of a kind of percolate according to claim 1, it is characterized in that:
Described chemical oxidation advanced treatment comprises:
Add sulfuric acid and regulate pH=3;
The chemical oxidizing agent that chemical oxidation treatment adopts is Fenton reagent, Fe in described Fenton reagent
2+with H
2o
2mass ratio be 0.75: 1 ~ 1.2: 1, the add-on of described Fenton reagent is that in Fenton reagent, in hydrogen peroxide and pending water, COD mass ratio is 0.5: 1 ~ 2.4: 1;
Reaction times is 0.5 ~ 1.5 hour;
Through water outlet adjust ph to 6 ~ 8 of Fenton reagent process.
5. by the treatment process of a kind of percolate according to claim 1, it is characterized in that: the hydraulic detention time of described secondary sedimentation process is 1 ~ 2 hour.
6., by the treatment process of a kind of percolate according to claim 1, it is characterized in that:
The process of described secondary Anoxybiotic-aerobic biologic is carried out in reinforced concrete sewage pond or in Steel Vessel, and load elastic filler in sewage lagoon or Steel Vessel, microorganic adhesion forms microbial film in elastic filler;
The dissolved oxygen content controlling anoxic operation is not more than 0.4mg/L, anoxic pond hydraulic detention time 1.5 ~ 3 hours;
Control aerobic in-process dissolved oxygen content at 2 ~ 5mg/L, hydraulic detention time 30 ~ 60 hours;
By the mixed-liquor return of aerobic in-process to anoxic operation, control of reflux ratio is 3 ~ 6.
7. by the treatment process of a kind of percolate according to claim 1, it is characterized in that: use dioxide peroxide disinfection.
8. by the treatment process of a kind of percolate according to claim 1, it is characterized in that: also comprise sludge treatment technique, mud is backfilled to landfill yard after being dewatered by pressure filter.
9. by the treatment process of the arbitrary described a kind of percolate of claim 1 ~ 8, it is characterized in that: biological treatment adopts activated sludge process, according to nitrogen dynamics formula determination return sludge ratio.
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| CN109851182A (en) * | 2019-04-12 | 2019-06-07 | 湖南湘奈环保科技有限责任公司 | A kind of processing method of landfill leachate |
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Application publication date: 20151118 |