CN100398470C - Infiltration method for treating garbage - Google Patents
Infiltration method for treating garbage Download PDFInfo
- Publication number
- CN100398470C CN100398470C CNB2006100345178A CN200610034517A CN100398470C CN 100398470 C CN100398470 C CN 100398470C CN B2006100345178 A CNB2006100345178 A CN B2006100345178A CN 200610034517 A CN200610034517 A CN 200610034517A CN 100398470 C CN100398470 C CN 100398470C
- Authority
- CN
- China
- Prior art keywords
- water
- pond
- hours
- percolate
- less
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The present invention discloses a sewage treating method for waste leachate, which comprises the following steps: step 1, preprocessing procedure, the preprocessing procedure comprises that the waste leachate is added in flocculating reagent to flocculate and pre-precipitate under the alkaline condition; step 2, the waste leachate is partly denitrified through a circulating blow-off tank and a stripping tower after alkalified; step 3, the waste leachate is in a UASB anaerobic reactor for anaerobic reaction; step 4, the waste leachate uses two-stage contact oxidation for aerobic treatment; step 5, the waste leachate makes an MBR film treatment in a film biological reacting tank; step 6, the leachate which is treated through the MBR film for nanofiltration. The water quality which is treated by the present invention has the advantages that COD is less than or equal to 10mg/L, SS is equal to 0, conductance is less than or equal to 1000 mus. cm, and reaches water quality standards for domestic service water.
Description
Technical field
The present invention relates to a kind of method of sewage disposal, particularly design a kind of sewage water treatment method of percolate.
Background technology
Along with the raising of expanding economy and living standards of the people and government need to improve to requirement on environmental protection, the sanitary landfill of municipal wastes, compost and waste incineration and generating electricity are the waste disposal methods that extensively adopts both at home and abroad at present.But the percolate sewage that rubbish produces in the process of landfill, compost and waste incineration and generating electricity is a kind of water quality and quantity to alter a great deal, microbial nutrition is out of proportion, ammonia-nitrogen content is high, the high concentration organic sewage of complicated component, be acknowledged as the most difficult sewage up to standard in the world today, not only very black smelly unpleasant, and its pollution concentration is 10-100 times of general municipal effluent, directly surrounding soil and underground water are caused severe contamination, the place of arrival, plant can't grow.COD reaches as high as up to ten thousand or several ten thousand mg/l in the percolate, ammonia nitrogen (NH
3-N) up to several thousand mg/l, and BOD/COD is very lower than again, and hardly degraded organic substance and ammonia nitrogen concentration are very high, and directly biodegradability is relatively poor, thereby undesirable with common direct biochemical treatment effect; And contain in the sewage the deleterious salt of microorganism, toxic compounds, heavy metal ion, the meeting microbiostatic activity influences the direct biochemical effect of microorganism, belongs to more unmanageable high concentrated organic wastewater.Therefore, the waste leachate purification of carrying out refuse landfill and burning electricity generation factory is dealt with the work quite urgent.
Summary of the invention
Purpose of the present invention is exactly in order to overcome the above problems, and a kind of advanced technology, convenient management are provided, operation efficient low-consume, the reliable rubbish leachate treatment method of decontamination effect improving.
For achieving the above object, the present invention has adopted following technical scheme:
The invention discloses a kind of garbage filter liquid processing method, described method comprises step:
(1) pre-treatment step, this pre-treatment step comprise percolate is added the flocculation agent preliminary precipitation of flocculating under alkaline conditions;
(2) alkalize after circulation blow-removing pond and stripping tower carry out the part denitrogenation,
(3) in the UASB anaerobic reactor, carry out anaerobic reaction;
(4) adopt the two-stage contact oxidation to carry out aerobic treatment;
(5) in the membrane biological reaction pond, handle;
(6) adopt nanofiltration technique to carry out advanced treatment for membrane biological reaction pond treat effluent.
The alkaline condition of described step (1) is meant the pH value between 9～11, adopts lime to make flocculation agent in step (1), and makes percolate preliminary precipitation be no less than 2 hours after adding flocculation agent.
Described step (2) is meant, adding alkali through in the pretreated percolate, make ammonium ion wherein be converted into free ammonia, and make percolate flow into the circulation blow-removing pond, pump to the stripping tower top with pump and spray water distribution, carry out air blast from bottom to top from the stripping tower bottom simultaneously, described stripping tower inside is equipped with polylith eddy flow plate scavenging tower, airflow from bottom to top on polylith eddy flow plate with the water counter current contact of spray, free ammonia is taken off inhale and overflows.
Circulation blow-removing pond recycle ratio is 100: 25～35, and preferred 100: 28, vapour-liquid ratio was 400～800: 1, and preferred 600: 1, the processing air quantity was 11000～18000m
3/ h.
Also comprise between described step (2) and the step (3), in the percolate inflow horizontal sedimentation tank of part deamination, carry out advection sedimentation, and before advection sedimentation, add flocculation agent; This flocculation agent preferably adopts aluminium iron polychloride, and the dosage of aluminium iron polychloride is 30～40mg/L, and the pH value is controlled at 7.5～9.
Described step (3) is carried out the residence time of anaerobic reaction for being no less than 50 hours in the UASB anaerobic reactor, water inlet adopts equally distributed perforated pipe water distributor to make waste water be incorporated into the bottom of UASB reactor equably, temperature of reactor is stabilized in 30 ℃～40 ℃, and the pH value stabilization is 7～8.
Preferably, in the described step (3), percolate flows into before the UASB anaerobic reactor, is introduced into the middle pond of anaerobism, and stop is no less than 12 days in the middle pond of anaerobism.
When described step (4) was carried out aerobic treatment in two-stage contact oxidation pond, the residence time was no less than 60 hours, and in the back in two-stage contact oxidation pond the intermediate sedimentation pond that a residence time is no less than 10 hours was set.
Described step (4) adopts the two-stage catalytic oxidation to carry out aerobic treatment and is meant, two-stage contact oxidation pond is divided into aerobic area, first step catalytic oxidation district, oxygen-starved area, four different zones in second stage catalytic oxidation district, each zone is equipped with different aeration rates, and sewage is purified the organism in the sewage, ammonia nitrogen and phosphorus degraded by the different microorganisms flora under being in anaerobism, anoxic, aerobic situation;
Described aerobic area is received carries out combination treatment with sewage and active sludge after the water outlet of UASB anaerobism, makes dissolved oxygen be controlled at 0.5-1.0mg/L, and hydraulic detention time is no less than 17 hours;
It is the microbial film contact medium that described first step catalytic oxidation district adopts the fiber soft-filler, and dissolved oxygen is controlled at 2.5-3.5mg/L, the gas-water ratio 10-15 of aeration: 1, and hydraulic detention time is no less than 17 hours;
Aeration is not carried out in described oxygen-starved area, allows double oxygen bacterium in the water remaining oxygen in the consume water in metabolic process, carries out denitrification denitrogenation, and hydraulic detention time is no less than 12 hours;
It is the microbial film contact medium that catalytic oxidation district, the described second stage adopts the fiber soft-filler, and dissolved oxygen is controlled at 2.0-2.5mg/L, and hydraulic detention time is no less than 14 hours.
The membrane biological reaction pond of described step (5) comprises anaerobic zone, catalytic oxidation district and film treatment zone three parts, percolate residence time of film treatment zone for being no less than 20 hours, membrane module adopts hollow fiber ultrafiltration membrane.
Because adopted above scheme, the beneficial effect that the present invention is possessed is:
Carry out the processing of percolate with method of the present invention, processing power is big, treatment effect is good, convenient management, the level of automation height, the operation efficient low-consume, water quality after the processing reaches (DB44/26-2001) the first period first discharge standard of Guangdong Province's provincial standard " water pollutant emission limit set ", reach 61250mg/L by COD (chemical oxygen demand (COD)) peak value before handling, SS (suspended substance) is up to 5000mg/L, changes the COD≤10mg/L after the processing into, SS=0, electricity is led≤1000 μ s.cm, reaches the reclaimed water standard, and effect is remarkable.
Description of drawings
Fig. 1 is the treatment scheme synoptic diagram of percolate of the present invention.
Embodiment
Below the present invention is described in further detail.
The specific embodiment of the present invention is the percolate sewage treatment process of Pinghu Town of Shenzhen Region garbage incinerating power plant, and this power station day treating refuse amount is 900 tons.Dumping produces certain percolate sewage, and every day, sewage quantity was about 120 tons, and this percolate is a kind of organic sewage of high density, contains the pollutents such as ammonia nitrogen, organism of high density.In this embodiment, percolate is when entering system, and COD (chemical oxygen demand (COD)) peak value reaches 61250mg/L, and SS (suspended substance) is up to 5000mg/L, and mean value is about 3000mg/L.
As Fig. 1, percolate is at first collected by water collecting basin, and the pump hole is established in the water collecting basin bottom, regularly takes the mud that is trapped in the water collecting basin bottom away.
The effusive sewage of water collecting basin enters grating tank, and grating tank is used the two-stage grid, and first road is positioned at the grating tank water inlet, adopts the drawer type aperture plate, and spacing is 2mm, and the second road grid places grating tank water outlet place, grid distance 1mm.
Enter the two poles of the earth flocculation basin again by the effusive sewage of grating tank, and add lime flocculation therein, PH is controlled between the 9-11, the lime dosing pump adopts Frequency Converter Control, the control of flocculation basin pH value adopts analog quantity output signals to give frequency transformer by setting the control bound of PH instrument, and frequency transformer is according to analog output signal, what of adding amount of lime are the operating frequency of adjusting the lime dosing pump determine, thus the pH value of control flocculation basin.
Sewage and then enter preliminary sedimentation tank, sedimentation time 2h.Preliminary sedimentation tank adopts rectangular sedimentation tank.After the preliminary sedimentation tank processing, the COD place to go rate of percolate is at 20%-30%, and the clearance of SS (suspended substance) is about 65%.
Through after the above-mentioned pre-treatment step, again waste water is imported the circulation blow-removing pond.The percolate ammonia-nitrogen content reaches more than the 2000mg/L, then be difficult to realize biological denitrificaion if allow it directly enter biochemical treatment apparatus, therefore utilize the alkalization stripping tower to carry out the part denitrogenation earlier, promptly at first adding alkali makes percolate be alkalescence (ph＞9), ammonium ion wherein is converted into free ammonia, sends into stripping tower then and removes free ammonia with spray and air blast stripping mode.But the ammonia that stripping comes out is qualified discharge after handle on the ammonia absorption tower.After waste water flows into the circulation blow-removing pond, pump to the stripping tower top with pump and to spray water distribution.Establish polylith eddy flow plate in the stripping tower, force flow through from bottom to top polylith eddy flow plate and contact with water adverse current thorough mixing of airflow is reached the purpose of stripping by two gas blowers installing at the stripping tower rear portion.Waste water is 24 hours in the residence time of this step, from the circulation blow-removing pond with pump draw water to the recycle ratio of stripping tower be 100: 28.Described recycle ratio is meant the cycle index of water between stripping tower and circulation blow-removing pond of unit volume, with 20: 1 be example, refer to 1m
3Former water between stripping tower and circulation blow-removing pond, circulate 20 times.The vapour-liquid ratio of gas blower blow air is 600: 1, and the processing air quantity is 14000m
3/ h.In order to improve ammonia stripping rate, the bottom in circulation blow-removing pond further is provided with aerating apparatus ammonia is carried out preliminary stripping, can further guarantee the high clearance of ammonia.In this step, to ammonia-N removal rate at 70%-80%.With traditional comparing with the filler stripping tower, adopt above-mentioned blow-removing system that following advantage is arranged: big (2) simple structure (3) running resistance little (4) energy consumption lower (5) of (1) gas flux need not to clean.
Go in the cycle set tank through the sewage collecting behind the circulation blow-removing, hydraulic detention time is 5h herein, enters next unit afterwards and continues to handle.
Next step enters coagulation reaction tank sewage, and adds flocculation agent, enters horizontal sedimentation tank then and precipitates.Sedimentation time 5h.Because follow-up UASB anaerobic reactor is to water inlet SS (suspended substance) requirement≤300mg/L, the hydraulic load that therefore designs this horizontal sedimentation tank is less.Flocculation agent adopts aluminium iron polychloride, dosage is 35mg/L, pH value is controlled at about 8, handle through this unit coagulating sedimentation, remove macromole suspended particulate matter, COD, also removed the part ammonia nitrogen simultaneously, greatly reduce the too high influence of organic compound and ammonia nitrogen of biochemical treatment bacterial classification, the COD clearance is about 15%, water outlet SS (suspended substance)≤300mg/L.
Next step flows into the waste water that horizontal sedimentation tank comes out in the middle pond of pulling flow type anaerobism, and stops about 15 days.In this step, utilize the residence time of overlength, make through pretreated percolate sewage and carry out abundant acidication.This handles the primary stage processing as the UASB anaerobic reactor.After the normal operation of UASB anaerobic reactor, can use the mud more than needed of its output that pond in the middle of the anaerobism is inoculated, further improve the treatment effect in the middle pond of anaerobism.The advantage of setting up the middle pond of this anaerobism is as follows: (1) realizes the equalizing tank function, regulate the influent load (3) of handling the water yield (2) buffering UASB anaerobic reactor and further reduce SS (suspended substance), guarantee that reactor water inlet safety (4) improves UASB anaerobic reactor water inlet biochemical.Through the COD clearance after this cell processing about 30%, SS (suspended substance)≤100mg/L.
Behind pond in the middle of the anaerobism, percolate enters the UASB anaerobic reactor, and sewage carries out anaerobic reaction at this, and larger molecular organics is decomposed into than the small molecules organism, improves the biodegradability of percolate.Sewage is 60 hours in effective residence time of UASB reactor.In operational process, the afterheat steam that utilizes refuse-burning plant makes it temperature of reaction and is stabilized in about 35 ℃ for the heating of UASB reactor.Water inlet adopts equally distributed perforated pipe water distributor to make waste water be incorporated into the bottom of UASB reactor equably, and sewage is upwards by comprising the Sludge Bed of granule sludge or floc sludge.Anaerobic reaction occurs in the contact process of sewage and mud granule, and the biogas that reaction produces has caused inner circulation.Adhere to or and rise to reactor head, hit triphase separator gaseous emission plate, cause the mud flco degassing of adhering to bubble attached to the biogas on the mud.Bubble discharges the surface that the back mud granule will be deposited to Sludge Bed, and gas is collected into the collection chamber of the triphase separator of reactor head.Some mud granules can enter the settling region through the separator slit.
10 meters of UASB anaerobic reactor diameters in the present embodiment, 8 meters of pond body overhead clearances, available depth is 7 meters, the reaction zone height is 5.5 meters, 60 hours residence time.
The startup of UASB anaerobic reactor:
Start and be divided into three phases: (1) sludge acclimatization incubation period (2) load (3) oepration at full load phase raising phase.
Fs sludge acclimatization incubation period: select for use through the mud of taming and inoculate, anaerobic sludge divides 5 days access 200m
3, the sludge concentration of reaction of inoculation device is 34mg/L, inserts 40m in every day
3Behind the anaerobic sludge, add the middle pond water outlet of the anaerobism of COD after the dilution about 3000mg/L, dosage is 40m
3, after 5 days vaccinizations and adding dilution waste water, be full of whole UASB anaerobic reactor.Because the temperature of seed sludge does not reach the design and operation temperature about 26 °, therefore, need to improve temperature of reactor.Adopt the little water yield intermittent water inflow every day, advanced 4 hours, stopped two hours, the water yield is controlled at 2m
3/ h, COD are about 3000mg/L, and volumetric loading is controlled at 0.15kgCOD/ (m
3.d), temperature raise 1 ° in per two days.When temperature was brought up to 36 °, amount of inlet water remained unchanged, and the pond water outlet directly enters without dilution in the middle of the anaerobism, and COD is between 16800mg/L-20000mg/L in water inlet, moves for 2 weeks continuously, and the clearance of later stage COD progressively improves, and clearance reaches about 80%.About 45 days consuming time of this stage.
Subordinate phase is the load raising phase: anaerobic reactor is through after the operation of fs, and beginning progressively improves the operating load of reactor, improves load by increasing amount of inlet water.Water inlet is continuously adopted in water inlet, and 1-15 days, the processing water yield was 2m
3/ h, COD is between 16800mg/L-20000mg/L in water inlet, and reactor load improves by 1.36kgCOD/ (m
3.d) bring up to 1.92kgCOD/ (m
3.d), the clearance of COD was stabilized in 80% water outlet SS (suspended substance)≤47mg/L in several days in the back.During 16-35 days, handle the water yield and rise to 3m
3/ h, intaking is pond water outlet in the middle of the anaerobism, reactor load is increased to 2.8kgCOD/ (m
3.d), in ensuing 2 months, amount of inlet water is brought up to designed water 7m gradually
3/ h, reactor load is increased to 4.07kgCOD/ (m
3.d) clearance of later stage water outlet COD is stabilized in more than 80%, water outlet SS (suspended substance)≤40mg/L.
Phase III is the oepration at full load phase: reach 7m in water inlet
3Behind/the h, reactor water outlet 100% refluxes, and organic loading reaches 4.5-5.3kgCOD/ (m
3.d), gas production rate also improves gradually, factor of created gase 2.7-3.9m
3/ (m
3.d).Microscopy reactor organisms kind branch is reasonable, and generating has granule sludge.Through after the processing of anaerobic reactor, the clearance of COD is more than 85%, SS (suspended substance)≤30mg/L.
Between the starting period of UASB anaerobic reactor, a PH instrument is installed on the reactor water inlet pipe, according to coming the regimen condition, an alkali volume pump is set, controlled by the PH instrument, the reactor pH value is stabilized in about 7.5, avoid because the water inlet acidifying makes reactor unbalance.
After the processing of UASB anaerobic reactor, organic pollutant in the percolate such as lipid acid, hydro carbons, phenols, heterocyclic arene class, polycyclic aromatic hydrocarbons etc. are all effectively removed, or be decomposed into the small molecules of easier degraded, obviously reduced the toxicity of percolate, heavy metals etc. have also obtained effective removal through behind a series of flocculation sediments.
UASB is on average intake COD about 20000mg/L, and reactor is after taming through inoculation, and processing power improves gradually, and the clearance of COD is stabilized between the 80-85%, and reactor water outlet COD＜4000mg/L, organic loading are 4.8kgCOD/m
3.d, simultaneously reactor effluent adopting 100% is refluxed.
The water outlet of UASB anaerobic reactor flows into two-stage contact oxidation pond and carries out aerobic reaction.This segment process principal feature is in same structures, by structures being divided into different zones, be equipped with different aeration rates, being under anaerobism, anoxic, the aerobic situation of sewage purified the organism in the sewage, ammonia nitrogen and phosphorus degraded by the different microorganisms flora, enter follow-up horizontal sedimentation tank at last, carry out mud-water separation, precipitating sludge enters the mud collecting tank, by mud backflow water pump it is reallocated, precipitated outlet water enters the MBR reaction tank and handles again.
The total useful volume of two-stage contact oxidation treatment system that this unit adopted is 487m
3, 4.6 meters of pond body available depths, total residence time is 70 hours.Be divided into aerobic area, first step catalytic oxidation district, oxygen-starved area, second stage catalytic oxidation district according to different functions.The aerobic area hydraulic detention time is 20 hours, is received the active sludge combination treatment of water outlet of UASB anaerobism and partial reflux, and dissolved oxygen D0 is controlled at 0.5-1.0mg/L; One-level catalytic oxidation district hydraulic detention time is 20 hours, and adopting the fiber soft-filler is the microbial film contact medium, and characteristics are that specific surface area is big, voidage is high, hydraulic resistance is little, steady chemical structure, low, the in light weight (2-3kg/m of cost
3) etc., this stage dissolved oxygen DO value is controlled at about 3mg/L, and gas-water ratio is at 10-15: 1; The oxygen-starved area hydraulic detention time is 14 hours, in this stage, water is not carried out aeration, allows double oxygen bacterium in the water remaining oxygen in the consume water in metabolic process, carries out denitrification denitrogenation; Catalytic oxidation district, second stage hydraulic detention time is 16 hours, and adopting the fiber soft-filler is the microbial film contact medium, and this stage dissolved oxygen DO value is controlled at 2.0-2.5mg/L.COD clearance through contact oxidation pond processing unit is stabilized in about 85%, and unit water outlet COD＜800mg/L, organic loading are 2.5kgCOD/m
3.d.
Next step enters the intermediate sedimentation pond waste water, precipitates.In the present embodiment, adopt rectangular sedimentation tank, long 4.6 meters of pond, wide 10 meters, the bucket height is 2.5 meters, and available depth is 2 meters, and the residence time is 13 hours, in order to reduce the pollution of ferro-aluminum ion for MBR film in the follow-up MBR film processing unit, this step can effectively precipitate the aging mud that the contact-oxidation pool water outlet is carried.Remove simultaneously further the COD in the waste water, the COD clearance of this element about 25%, unit water outlet COD＜600mg/L.
Next step enters waste water in the MBR reaction tank, and carries out the MBR film and handle.For guaranteeing that discharging water quality reaches primary standard, design immersion MBR membrane treatment appts in the MBR reaction tank.Waste water carries out the nitrification and denitrification reaction in the MBR reaction tank, can further remove pollutents such as COD, BOD, ammonia nitrogen.Membrane bioreactor (MBR) technology is the novel wastewater processing technology that membrane separation technique and biotechnology organically combine, and it utilizes membrane separation plant that active sludge in the biochemical reaction tank and larger molecular organics are held back, and saves second pond.Film-bioreactor technology has been strengthened the function of bio-reactor greatly by the isolation technique of film, through two-stage aerobic biochemical treatment before, biodegradability in the water is reduced to about 0.23 (BOD/COD), biochemical reduces, in conventional treatment process, the water in this stage is intractable, but in membrane bioreactor, by holding back to active sludge, bacterium, make the bacterium of some hardly degraded organic substances of degraded be kept propagation, cultivation, domestication through 2 months active sludge improve activated sludge concentration greatly, and bacterial species significantly increases.Membrane bioreactor can be controlled its hydraulic detention time (HRT) and sludge retention time (SRT) respectively simultaneously.
MBR reaction tank available depth is 3.5 meters.Reaction tank is divided into anaerobic zone, catalytic oxidation district and film treatment zone three parts.Membrane module adopts hollow fiber ultrafiltration membrane, and membrane material is polyvinylidene difluoride (PVDF) (PVDF), and membrane pore size is 0.2 μ m, monolithic membrane area 20m
2. water production rate is 3.8M
3/ sheet .d.The film treatment zone residence time is 24 hours, and sludge concentration is 4500mg/L, water outlet COD about 90mg/L, SS=0, SDI value≤3, turbidity≤0.46NTU meets nanofiltration water inlet requirement.
System is behind process two-stage aerobic biochemistry, COD biodegradability in the waste water also progressively reduces, adopt conventional aeration method can not effectively reduce COD in the water, and the employing membrane bioreactor, it can be in water outlet, do not take away active sludge, the microorganism of having handled difficult degradation COD for slower some of propagation since like this provides a good growing environment, and this is not accomplish in conventional aerobic activated sludge process.
Can further pass through nanofiltration (NF) through the water outlet of MBR reaction tank and the processing of MBR film and handle the back discharging.The aperture of nanofiltration mostly is nano level, and the boundary is between ultrafiltration and reverse osmosis filter.Nanofiltration promotes by external pressure, and the solvency in the water is held back.Because reverse osmosis membrane all has very high rejection to all ions in the water, and the nanofiltration membrane selectivity higher to holding back of water intermediate ion, nanofiltration membrane is that the organism of 200-1000 has very high rejection to divalent ion and molecular weight only.Therefore, select the technology of nanofiltration for use, and do not select reverse osmosis process for use, promptly can guarantee has higher removal to COD in the water, has avoided the dirty stifled problem in the long-time back of reverse osmosis membrane again, has prolonged the work-ing life of system, has reduced the running cost of system.
In the present embodiment, nanofiltration adopts 2+1 to arrange, and uses the antipollution nanofiltration membrane of 6 U.S. TFC series, water production rate 〉=7m
3/ h adopts constant pressure frequency conversion control, and pressure-controlling is at 0.35-0.4Mpa, produce water COD≤10mg/L, electricity is led≤1000 μ s.cm, reaches the reclaimed water standard, and meets (DB44/26-2001) first period first discharge standard requirement of Guangdong Province's provincial standard " water pollutant emission limit set ".
Claims (10)
1. a garbage filter liquid processing method is characterized in that, described method comprises step:
(1) pre-treatment step, this pre-treatment step comprise percolate is added the flocculation agent preliminary precipitation of flocculating under alkaline conditions;
(2) alkalize after circulation blow-removing pond and stripping tower carry out the part denitrogenation,
(3) in the UASB anaerobic reactor, carry out anaerobic reaction;
(4) adopt the two-stage catalytic oxidation to carry out aerobic treatment;
(5) in the membrane biological reaction pond, handle;
(6) will further handle through the percolate that handle in the membrane biological reaction pond with nanofiltration.
2. a kind of garbage filter liquid processing method according to claim 1, it is characterized in that: the alkaline condition of described step (1) is meant that the pH value is between 9～11, in step (1), adopt lime to make flocculation agent, and after adding flocculation agent, make percolate preliminary precipitation be no less than 2 hours.
3. a kind of garbage filter liquid processing method according to claim 1, it is characterized in that: described step (2) is meant, adding alkali through in the pretreated percolate, make ammonium ion wherein be converted into free ammonia, and make percolate flow into the circulation blow-removing pond, pump to the stripping tower top with pump again and spray water distribution, carry out air blast from bottom to top from the stripping tower bottom simultaneously, described stripping tower inside is equipped with polylith eddy flow plate, and airflow is from bottom to top through the water counter current contact of polylith eddy flow plate and top spray.
4. a kind of garbage filter liquid processing method according to claim 3 is characterized in that: circulation blow-removing pond recycle ratio is 100: 25～35, and the vapour-liquid ratio of air blast is 400～800: 1, and the processing air quantity is 11000～18000m
3/ h.
5. a kind of garbage filter liquid processing method according to claim 1, it is characterized in that: also comprise between described step (2) and the step (3), in the percolate inflow horizontal sedimentation tank of part deamination, carry out advection sedimentation, and before advection sedimentation, add flocculation agent; This flocculation agent preferably adopts aluminium iron polychloride, and the dosage of aluminium iron polychloride is 30～40mg/L, and the pH value is controlled at 7.5～9.
6. a kind of garbage filter liquid processing method according to claim 1, it is characterized in that: described step (3) is carried out the residence time of anaerobic reaction for being no less than 50 hours in the UASB anaerobic reactor, water inlet adopts equally distributed perforated pipe water distributor to make waste water be incorporated into the bottom of UASB reactor equably, temperature of reactor is stabilized in 30 ℃～40 ℃, and the pH value stabilization is 7～8.
7. a kind of garbage filter liquid processing method according to claim 6 is characterized in that: in the described step (3), percolate flows into before the UASB anaerobic reactor, is introduced into the middle pond of anaerobism, and stop is no less than 12 days in the middle pond of anaerobism.
8. a kind of garbage filter liquid processing method according to claim 1, it is characterized in that: when described step (4) is carried out aerobic treatment in two-stage contact oxidation pond, the residence time is no less than 60 hours, and in the back in two-stage contact oxidation pond the intermediate sedimentation pond that a residence time is no less than 10 hours is set.
9. a kind of garbage filter liquid processing method according to claim 8, it is characterized in that: described step (4) adopts the two-stage catalytic oxidation to carry out aerobic treatment and is meant, two-stage contact oxidation pond is divided into aerobic area, first step catalytic oxidation district, oxygen-starved area, four different zones in second stage catalytic oxidation district, each zone is equipped with different aeration rates, and sewage is purified the organism in the sewage, ammonia nitrogen and phosphorus degraded by the different microorganisms flora under being in anaerobism, anoxic, aerobic situation;
Described aerobic area is received carries out combination treatment with sewage and active sludge after the water outlet of UASB anaerobism, makes dissolved oxygen be controlled at 0.5-1.0mg/L, and hydraulic detention time is no less than 17 hours;
It is the microbial film contact medium that described first step catalytic oxidation district adopts the fiber soft-filler, and dissolved oxygen is controlled at 2.5-3.5mg/L, the gas-water ratio 10-15 of aeration: 1, and hydraulic detention time is no less than 17 hours;
Aeration is not carried out in described oxygen-starved area, allows double oxygen bacterium in the water remaining oxygen in the consume water in metabolic process, carries out denitrification denitrogenation, and hydraulic detention time is no less than 12 hours;
It is the microbial film contact medium that catalytic oxidation district, the described second stage adopts the fiber soft-filler, and dissolved oxygen is controlled at 2.0-2.5mg/L, and hydraulic detention time is no less than 14 hours.
10. a kind of garbage filter liquid processing method according to claim 1, it is characterized in that: the membrane biological reaction pond of described step (5) comprises anaerobic zone, catalytic oxidation district and film treatment zone three parts, percolate residence time of film treatment zone for being no less than 20 hours, membrane module adopts hollow fiber ultrafiltration membrane.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100345178A CN100398470C (en) | 2006-03-17 | 2006-03-17 | Infiltration method for treating garbage |
| HK07105482A HK1098121A1 (en) | 2006-03-17 | 2007-05-24 | A method for processing the garbage percolate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100345178A CN100398470C (en) | 2006-03-17 | 2006-03-17 | Infiltration method for treating garbage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1872745A CN1872745A (en) | 2006-12-06 |
| CN100398470C true CN100398470C (en) | 2008-07-02 |
Family
ID=37483373
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100345178A Expired - Fee Related CN100398470C (en) | 2006-03-17 | 2006-03-17 | Infiltration method for treating garbage |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN100398470C (en) |
| HK (1) | HK1098121A1 (en) |
Families Citing this family (28)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101445294B (en) * | 2009-01-04 | 2010-12-01 | 上海大学 | A marsh gas preparation method of landfill leachate resources |
| CN101508514B (en) * | 2009-03-20 | 2011-01-05 | 厦门凯瑞尔数字环保科技有限公司 | Zero discharge recycle treatment method for garbage leachate |
| CN101671090B (en) * | 2009-04-29 | 2011-05-04 | 四川宇阳环境工程有限公司 | Combined processing technique of garbage percolates |
| CN101585649B (en) * | 2009-05-05 | 2011-09-21 | 广东绿由环保科技股份有限公司 | Processing system and processing method for purifying sewerage sludge filtrate |
| CN101613163B (en) * | 2009-07-30 | 2012-08-29 | 唐绍明 | Rubbish percolate treatment process |
| CN101955295B (en) * | 2010-04-20 | 2012-02-08 | 南通泰禾化工有限公司 | Method for treating waste water from isophthalonitrile synthesis technology |
| CN101863598B (en) * | 2010-06-28 | 2012-05-23 | 深圳市龙澄高科技环保有限公司 | Method for treating city garbage leachate |
| CN101898855B (en) * | 2010-07-16 | 2012-02-29 | 华东理工大学 | Integrated ex-situ repair system for underground water polluted by volatile organic compound |
| CN101962249A (en) * | 2010-08-20 | 2011-02-02 | 北京清大国华环保科技有限公司 | Method and device for processing high-concentration undegradable waste water by using jet flow membrane bioreactor (MBR) |
| CN101948215B (en) * | 2010-08-31 | 2012-05-30 | 宇星科技发展(深圳)有限公司 | Garbage leachate treatment process |
| CN102531244B (en) * | 2010-12-07 | 2013-06-12 | 光大环保科技发展（北京）有限公司 | Pretreatment method of landfill leachate of waste incineration power plant |
| CN102107997B (en) * | 2011-01-12 | 2012-09-05 | 北京林业大学 | Method for treating leachate of domestic waste incineration plants |
| CN102167479B (en) * | 2011-03-22 | 2012-12-19 | 江苏久吾高科技股份有限公司 | Garbage percolate treatment technology |
| CN102503046B (en) * | 2011-11-18 | 2013-08-14 | 北京伊普国际水务有限公司 | Advanced treatment system and method for high-concentration percolate in comprehensive garbage disposal plant |
| CN102408168A (en) * | 2011-12-30 | 2012-04-11 | 深圳市能源环保有限公司 | Sewage pretreatment system and method |
| CN103992001B (en) * | 2014-03-13 | 2015-08-19 | 浙江海洋学院 | A kind for the treatment of process of refuse leachate |
| CN105836974B (en) * | 2016-05-24 | 2019-07-16 | 华南理工大学 | A kind of garbage leachate treatment device and method |
| CN106365376A (en) * | 2016-08-30 | 2017-02-01 | 宜兴市中发水处理环保设备有限公司 | Treating system applied to garbage leachate |
| CN106396294A (en) * | 2016-12-06 | 2017-02-15 | 大同新成新材料股份有限公司 | Treatment method of lithium battery electrolyte cask washing wastewater |
| CN107188368B (en) * | 2017-06-19 | 2020-03-20 | 浙江清华长三角研究院 | Advanced treatment process for kitchen waste fermentation waste liquid |
| CN107601781A (en) * | 2017-11-01 | 2018-01-19 | 成都恒力达科技有限公司 | A kind of sewage disposal system |
| CN109987780A (en) * | 2017-12-29 | 2019-07-09 | 南京理工大学 | Garbage percolation liquid treating system and its technique based on sewage source heat pump technology |
| CN109761441A (en) * | 2019-01-23 | 2019-05-17 | 广州故乡源水处理有限公司 | A kind of processing method and processing device of landfill leachate |
| CN109824204B (en) * | 2019-02-18 | 2021-08-24 | 江西盖亚环保科技有限公司 | Method and system for rapidly and efficiently starting and intensively treating landfill leachate |
| CN110668633A (en) * | 2019-07-31 | 2020-01-10 | 南京万德斯环保科技股份有限公司 | Kitchen waste sorting wastewater treatment system and process |
| CN111943427A (en) * | 2020-07-10 | 2020-11-17 | 山东东顺环保科技有限公司 | High salt wastewater treatment system that contains |
| CN112811738A (en) * | 2021-01-19 | 2021-05-18 | 江西楚杭环保科技有限公司 | Multi-stage purification treatment method for waste water of refuse landfill |
| CN114702196B (en) * | 2022-02-28 | 2022-12-20 | 广东君道环保科技有限公司 | Multistage AO treatment process for landfill leachate |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05228459A (en) * | 1992-02-18 | 1993-09-07 | Kurita Water Ind Ltd | Apparatus for recovering methane gas from landfill site |
| KR100294075B1 (en) * | 1998-04-08 | 2001-10-25 | 공영조 | System for treating landfill leachate |
| CN1456521A (en) * | 2003-03-28 | 2003-11-19 | 北京市肇麟环境技术开发公司 | Process and apparatus for urban refuse cite penetrating liquid by three stage plus one process |
| CN1544365A (en) * | 2003-11-27 | 2004-11-10 | 武汉安全环保研究院 | Urban refuse sanitary landfill leachate disposing process |
| CN1736908A (en) * | 2005-08-01 | 2006-02-22 | 陈昆柏 | Method and system for harnessing consumer waste landfill percolate |
-
2006
- 2006-03-17 CN CNB2006100345178A patent/CN100398470C/en not_active Expired - Fee Related
-
2007
- 2007-05-24 HK HK07105482A patent/HK1098121A1/en not_active IP Right Cessation
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05228459A (en) * | 1992-02-18 | 1993-09-07 | Kurita Water Ind Ltd | Apparatus for recovering methane gas from landfill site |
| KR100294075B1 (en) * | 1998-04-08 | 2001-10-25 | 공영조 | System for treating landfill leachate |
| CN1456521A (en) * | 2003-03-28 | 2003-11-19 | 北京市肇麟环境技术开发公司 | Process and apparatus for urban refuse cite penetrating liquid by three stage plus one process |
| CN1544365A (en) * | 2003-11-27 | 2004-11-10 | 武汉安全环保研究院 | Urban refuse sanitary landfill leachate disposing process |
| CN1736908A (en) * | 2005-08-01 | 2006-02-22 | 陈昆柏 | Method and system for harnessing consumer waste landfill percolate |
Non-Patent Citations (2)
| Title |
|---|
| 我国垃圾渗滤液的特点和处理技术探讨. 董春松等.中国给水排水，第21卷第12期. 2005 |
| 我国垃圾渗滤液的特点和处理技术探讨. 董春松等.中国给水排水，第21卷第12期. 2005 * |
Also Published As
| Publication number | Publication date |
|---|---|
| HK1098121A1 (en) | 2007-07-13 |
| CN1872745A (en) | 2006-12-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100398470C (en) | Infiltration method for treating garbage | |
| CN101357812B (en) | Processing method for domestic garbage leachate | |
| CN101357813B (en) | Processing method for domestic garbage leachate | |
| CN100402448C (en) | Paper-making effluent purifying treatment process | |
| CN101767914B (en) | Method for treating garbage leachate | |
| CN102775025B (en) | Municipal life wastewater treatment system with high efficiency and low energy consumption | |
| CN104961306B (en) | A kind of processing method of vaccary breeding wastewater | |
| CN206767868U (en) | A kind of garbage percolation liquid treating system | |
| CN106977059A (en) | A kind of new and effective sewage disposal system and method | |
| CN108383320B (en) | Integrated treatment method for livestock and poultry breeding wastewater | |
| CN110372096A (en) | The processing method of garbage leachate | |
| CN101659502B (en) | Method for treating waste leachate by utilizing high denitrification shared type Orbal oxidation ditch | |
| CN103342441A (en) | Erythromycin thiocyanate wastewater treatment method | |
| CN102557324B (en) | Method for treating garbage leachate | |
| CN204400777U (en) | A kind of village's field sanitary sewage disposal and reutilization system | |
| CN208071544U (en) | A kind of railway communication system production wastewater treatment system | |
| CN110294575A (en) | The processing unit of garbage leachate | |
| CN107522344A (en) | A kind of sewage water treatment method of percolate | |
| CN105819626A (en) | Combined customized sewage disposal system | |
| CN102515438B (en) | Landfill leachate treatment process | |
| CN114685014A (en) | Livestock and poultry breeding wastewater treatment circulating system | |
| CN207891216U (en) | A kind of processing system of high-concentration hardly-degradable pharmacy waste water | |
| CN208700837U (en) | A kind of recovery processing structure for sewage | |
| CN112499894A (en) | Integrated MBBR (moving bed biofilm reactor) process for treating high-organic high-ammonia nitrogen industrial wastewater | |
| CN114105394A (en) | High-efficiency percolate total nitrogen removal treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| REG | Reference to a national code |
Ref country code: HK Ref legal event code: DE Ref document number: 1098121 Country of ref document: HK |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| REG | Reference to a national code |
Ref country code: HK Ref legal event code: GR Ref document number: 1098121 Country of ref document: HK |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Garbage infiltration liquid treating method Effective date of registration: 20140519 Granted publication date: 20080702 Pledgee: Shenzhen high tech investment and financing Company limited by guarantee Pledgor: Baisite Environment Protection Engineering Co., Ltd., Shenzhen City Registration number: 2014990000374 |
|
| PLDC | Enforcement, change and cancellation of contracts on pledge of patent right or utility model | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080702 Termination date: 20180317 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |