CN107522344A - A kind of sewage water treatment method of percolate - Google Patents

A kind of sewage water treatment method of percolate Download PDF

Info

Publication number
CN107522344A
CN107522344A CN201610438930.4A CN201610438930A CN107522344A CN 107522344 A CN107522344 A CN 107522344A CN 201610438930 A CN201610438930 A CN 201610438930A CN 107522344 A CN107522344 A CN 107522344A
Authority
CN
China
Prior art keywords
percolate
water
pond
sewage
hours
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.)
Pending
Application number
CN201610438930.4A
Other languages
Chinese (zh)
Inventor
王立兵
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to CN201610438930.4A priority Critical patent/CN107522344A/en
Publication of CN107522344A publication Critical patent/CN107522344A/en
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

The present invention discloses a kind of sewage water treatment method of percolate sewage, including step：（1）Pre-treatment step, the pre-treatment step carry out flocculation preformed precipitate including percolate is added into flocculant in the basic conditions；（2）After alkalization part denitrogenation is carried out through circulation blow-removing pond and stripping tower；（3）Anaerobic reaction is carried out in UASB anaerobic reactors；（4）Aerobic Process for Treatment is carried out using two-stage catalytic oxidation；（5）MBR film process is carried out in membrane biological reaction pond；（6）Percolate Jing Guo MBR film process is further handled with nanofiltration.With water-quality COD≤10mg/L after the method processing of the present invention, SS=0, the μ s.cm of conductance≤1000, reach reclaimed water standard.

Description

A kind of sewage water treatment method of percolate
Technical field
The present invention relates to a kind of method of sewage disposal, particularly designs a kind of sewage water treatment method of percolate.
Background technology
As the requirement of expanding economy and the raising of living standards of the people and government to environmental protection needs to improve, sanitary landfills, compost and the waste incineration and generating electricity of municipal refuse are current domestic and international widely used waste disposal methods.But rubbish caused percolate sewage during landfill, compost and waste incineration and generating electricity be a kind of water quality and quantity change very greatly, microbial nutrition is out of proportion, ammonia-nitrogen content is high, the high concentration organic sewage of complicated component, the world today is acknowledged as to be most difficult to handle sewage up to standard, it is not only extremely black smelly unpleasant, and its pollution concentration is 10-100 times of general municipal sewage, directly surrounding soil and underground water are caused seriously to pollute, place of arrival, plant can not grow.COD reaches as high as up to ten thousand or tens of thousands of mg/l, ammonia nitrogen (NH in percolate3- N) thousands of mg/l are up to, and BOD/COD ratios are again very low, hardly degraded organic substance and ammonia nitrogen concentration are very high, and direct biodegradability is poor, thus undesirable with common directly Biochemical Treatment；And heavy metal ion, microbial activity can be suppressed containing salt, the toxic compounds to harmful microorganism in sewage, influence the direct biochemical effects of microorganism, belong to high concentrated organic wastewater difficult to deal with.Therefore, the waste leachate purification processing work for carrying out refuse landfill and burning electricity generation factory is quite urgent.
The content of the invention
The purpose of the present invention is exactly to solve problem above, there is provided a kind of advanced technology, management are convenient, run efficient low-consume, the processing method of the reliable percolate of clean-up effect.
To achieve the above object, present invention employs following technical scheme：
The invention discloses a kind of sewage water treatment method of percolate, methods described includes step：
(1) pre-treatment step, the pre-treatment step carry out flocculation preformed precipitate including percolate is added into flocculant in the basic conditions；
(2) part denitrogenation is carried out through circulation blow-removing pond and stripping tower after alkalizing,
(3) anaerobic reaction is carried out in UASB anaerobic reactors；
(4) Aerobic Process for Treatment is carried out using two-stage contact oxidation；
(5) handled in membrane biological reaction pond；
(6) advanced treating is carried out using nanofiltration technique for the processing water outlet of membrane biological reaction pond.
The alkalescence condition of the step (1) refers to pH value between 9~11, and flocculant is made using lime in step (1), and percolate preformed precipitate is no less than 2 hours after flocculant is added.
The step (2) refers to, add alkali in the percolate by pretreatment, ammonium ion therein is set to be converted into free ammonia, and percolate is set to flow into circulation blow-removing pond, delivered to again with pumping at the top of stripping tower and carry out spray water distribution, while air blast is carried out from bottom to top from stripping tower bottom, polylith spiral board purifying column is installed inside the stripping tower, the air stream water counter current contacting on polylith spiral board with spray from bottom to top, escape free ammonia desorption in water.
Circulation blow-removing pond recycle ratio is 100: 25~35, preferably 100: 28, and gas liquid ratio is 400~800: 1, preferably 600: 1, and processing air quantity is 11000~18000m3/h。
Also include between the step (2) and step (3), the percolate through part deamination is flowed into horizontal sedimentation tank and carries out advection sedimentation, and flocculant is added before advection sedimentation；The flocculant preferably uses PAFC, and the dosage of PAFC is 30~40mg/L, and pH value control is 7.5~9.
The residence time that the step (3) carries out anaerobic reaction in UASB anaerobic reactors is no less than 50 hours, water inlet uses the bottom that equally distributed perforated pipe water-locator makes waste water be uniformly introduced UASB reactors, temperature of reactor is stable at 30 DEG C~40 DEG C, and pH stable is 7~8.
Preferably, in the step (3), percolate is flowed into before UASB anaerobic reactors, is introduced into anaerobism intermediate pool, and stop and be no less than 12 days in anaerobism intermediate pool.
When the step (4) carries out Aerobic Process for Treatment in two-stage contact oxidation pond, the residence time is no less than 60 hours, and intermediate sedimentation pond of the residence time no less than 10 hours is set behind two-stage contact oxidation pond.
The step (4) carries out Aerobic Process for Treatment using two-stage catalytic oxidation and referred to, two-stage contact oxidation pond is divided into aerobic area, first order catalytic oxidation area, anoxic zone, four, second level catalytic oxidation area different zones, each region is equipped with different aeration quantity, sewage is being purified the degraded of the organic matter in sewage, ammonia nitrogen and phosphorus by different microorganisms flora under anaerobism, anoxic, aerobic situation；
Sewage and activated sludge are subjected to mixed processing after the aerobic area receiving UASB anaerobic effluents, dissolved oxygen control is no less than 17 hours in 0.5-1.0mg/L, hydraulic detention time；
The first order catalytic oxidation area uses fiber soft-filler as biomembrane contact medium, and dissolved oxygen control is no less than 17 hours in 2.5-3.5mg/L, gas-water ratio 10-15: 1 of aeration, hydraulic detention time；
The anoxic zone is without aeration, and the simultaneous oxygen bacterium allowed in water consumes remaining oxygen in water in metabolic process, carries out denitrification denitrogenation, and hydraulic detention time is no less than 12 hours；
The second level catalytic oxidation area uses fiber soft-filler as biomembrane contact medium, and dissolved oxygen control is no less than 14 hours in 2.0-2.5mg/L, hydraulic detention time.
The membrane biological reaction pond of the step (5) includes anaerobic zone, catalytic oxidation area and film process area three parts, and residence time of the percolate in film process area is that membrane module used hollow fiber ultrafiltration membrane no less than 20 hours.
Scheme as a result of more than, it is the beneficial effect that the present invention possesses：
The processing of percolate is carried out with the method for the present invention, disposal ability is big, and treatment effect is excellent, and management is convenient, and automaticity is high, runs efficient low-consume, and the water quality after processing reaches Guangdong Province's provincial standard《Sewage Water Emissions limit》(DB44/26-2001) the first period first discharge standard, 61250mg/L is reached by COD (COD) peak value of before processing, SS (suspension) is up to 5000mg/L, COD≤the 10mg/L being changed into after processing, SS=0, the μ s.cm of conductance≤1000, reach reclaimed water standard, significant effect.
Embodiment
The present invention is described in further detail below.
The embodiment of the present invention is the percolate sewage disposal process of garbage incinerating power plant, and power plant day processing quantity of refuse is 900 tons.Dumping produces certain percolate sewage, and daily sewage quantity is about 120 tons, and this percolate is a kind of pollutant such as organic sewage of high concentration, ammonia nitrogen, organic matter containing high concentration.In this embodiment, for percolate when entering system, COD (COD) peak value reaches 61250mg/L, and SS (suspension) is up to 5000mg/L, and average value is in 3000mg/L or so.
Percolate is collected by collecting-tank first, and collecting-tank bottom sets pump hole, periodically takes the sludge for being trapped in collecting-tank bottom away.
The sewage of collecting-tank outflow enters grid pond, and grid pond uses two-stage grid, is located at grid pond water inlet first, and using drawer type aperture plate, spacing 2mm, second grid is placed in grid pond water outlet, grid distance 1mm.
The sewage flowed out by grid pond enters back into the two poles of the earth flocculation basin, and feeding lime flocculates wherein, PH is controlled between 9-11, lime dosing pump uses Frequency Converter Control, the control of flocculation basin pH value is by setting the control bound of PH instrument, and using analog quantity output signals to frequency converter, frequency converter is according to analog output signal, adjust lime dosing pump working frequency come determine add amount of lime number, so as to control the pH value of flocculation basin.
Then sewage enters back into preliminary sedimentation tank, sedimentation time 2h.Preliminary sedimentation tank uses rectangular sedimentation tank.After preliminary sedimentation tank is handled, the COD places to go rate of percolate is in 20%-30%, and SS (suspension) clearance is 65% or so.
Circulation blow-removing pond is imported after above-mentioned pre-treatment step, then by waste water.Percolate ammonia-nitrogen content reaches more than 2000mg/L, biological denitrificaion is difficult to realize if allowing it to be directly entered biochemical treatment apparatus, therefore part denitrogenation is carried out first with ammonia stripper, alkali is added to make percolate be in alkaline (ph ＞ 9) first, ammonium ion therein is converted into free ammonia, be then fed into stripping tower by spray with air blast stripping in a manner of remove free ammonia.The ammonia that stripping comes out can qualified discharge after ammonia absorption tower is handled.After waste water flows into circulation blow-removing pond, delivered to pumping at the top of stripping tower and carry out spray water distribution.Polylith spiral board is set in stripping tower, forces that air stream is flowed through to polylith spiral board from bottom to top and is sufficiently mixed with water adverse current to contact by two air blowers installed at stripping tower rear portion, reaches the purpose of stripping.Waste water is 24 hours in the residence time of the step, is 100: 28 from circulation blow-removing pond pumping water to the recycle ratio of stripping tower.The recycle ratio refers to cycle-index of the water of unit volume between stripping tower and circulation blow-removing pond, exemplified by 20: 1, refers to 1m3Raw water circulated 20 times between stripping tower and circulation blow-removing pond.The gas liquid ratio that air blower blows air is 600: 1, and processing air quantity is 14000m3/h.In order to improve ammonia aeration rate, the bottom in circulation blow-removing pond further sets aerator to carry out preliminary stripping to ammonia, can be further assured that the high clearance of ammonia.In this step, to the clearance of ammonia nitrogen in 70%-80%.With traditional compared with filler stripping tower, had the advantage that using above-mentioned blow-removing system：(1) big small (4) energy consumption of (2) simple structure (3) running resistance lower (5) of gas flux is without cleaning.
Sewage collecting after circulation blow-removing enters to circulate in water leg, and hydraulic detention time is 5h here, is continued with afterwards into next unit.
Sewage enters coagulation reaction tank in next step, and adds flocculant, is precipitated subsequently into horizontal sedimentation tank.Sedimentation time 5h.Because follow-up UASB anaerobic reactors are to SS (suspension) requirement≤300mg/L of intaking, therefore the hydraulic load for designing this horizontal sedimentation tank is smaller.Flocculant uses PAFC, dosage is 35mg/L, pH value is controlled 8 or so, through this unit coagulating kinetics, macromolecular suspended particulate matter, COD are removed, while also been removed part ammonia nitrogen, greatly reduces organic composite and the too high influence to strain of ammonia nitrogen of biochemical treatment, COD clearances about 15%, water outlet SS (suspension)≤300mg/L.
The waste water that horizontal sedimentation tank comes out is flowed into pulling flow type anaerobism intermediate pool in next step, and is stopped 15 days or so.In this step, using the residence time of overlength, make to carry out being fully hydrolyzed acidifying by pretreated percolate sewage.This processing is handled as the primary stage of UASB anaerobic reactors.It after UASB anaerobic reactor normal operations, the sludge more than needed of its output can be used to be inoculated with anaerobism intermediate pool, further improve the treatment effect of anaerobism intermediate pool.The advantages of setting up this anaerobism intermediate pool is as follows：(1) regulating reservoir function is realized, regulation processing water, (2) influent load of UASB anaerobic reactors is buffered, (3) SS (suspension) is further reduced, ensure that reactor enters water security, (4) improve UASB anaerobic reactors water inlet biochemical.COD clearances after this cell processing are in 30% or so, SS (suspension)≤100mg/L.
After anaerobism intermediate pool, percolate enters UASB anaerobic reactors, and sewage carries out anaerobic reaction, larger molecular organicses are decomposed into compared with small organic molecule herein, improves the biodegradability of percolate.Sewage is 60 hours in effective residence time of UASB reactors.In the process of running, heated using the afterheat steam of refuse-burning plant for UASB reactors, it is stable at 35 DEG C or so to be allowed to reaction temperature.Water inlet makes waste water be uniformly introduced the bottom of UASB reactors using equally distributed perforated pipe water-locator, and sewage is upwardly through the Sludge Bed for including granule sludge or floc sludge.Anaerobic reaction occurs in the contact process of sewage and mud granule, and biogas caused by reaction causes the circulation of inside.The biogas for adhering to or being not adhered on sludge rises to reactor head, hits three phase separator gas expelling plate, causes the sludge flco of bubbles attached to deaerate.Mud granule will be deposited to the surface of Sludge Bed after bubble release, and gas is collected into the collection chamber of the three phase separator of reactor head.Some mud granules can enter settling zone by separator gap.
10 meters of UASB anaerobic reactors diameter in present embodiment, 8 meters of pond body head room, available depth are 7 meters, and reaction zone is highly 5.5 meters, 60 hours residence times.
The startup of UASB anaerobic reactors：
Startup is divided into three phases：(1) sludge acclimatization culture period (2) load improves phase (3) the oepration at full load phase.
First stage sludge acclimatization culture period：It is inoculated with from the sludge through taming, 5 days access 200m of anaerobic sludge point3, the sludge concentration of reaction of inoculation device is 34mg/L, in access 40m daily3After anaerobic sludge, anaerobism intermediate pool water outlets of the COD after 3000mg/L or so dilution, dosage 40m are added3, after the vaccinizations of 5 days and adding dilution waste water, full of whole UASB anaerobic reactors.Because the temperature of seed sludge is at 26 ° or so, not up to design and operation temperature, therefore, it is necessary to improve temperature of reactor.Small water intermittent water inflow is used daily, is entered 4 hours, is stopped two hours, water rate control is in 2 m3/ h, COD are controlled in 0.15kgCOD/ (m in 3000mg/L or so, volumetric loading3.d), temperature raises 1 ° in every two days.When temperature brings up to 36 °, amount of inlet water keeps constant, and anaerobism intermediate pool water outlet is directly entered without dilution, and influent COD is between 16800mg/L-20000mg/L, and continuous operation 2 weeks, later stage COD clearance steps up, and clearance reaches 80% or so.This stage is time-consuming 45 days or so.
Second stage is that load improves the phase：Anaerobic reactor starts to step up the operating load of reactor, load is improved by increasing amount of inlet water after the operation of first stage.Water inlet uses continuum micromeehanics, and 1-15 days, processing water was 2m3/ h, between 16800mg/L-20000mg/L, reactor load improves by 1.36kgCOD/ (m influent COD3.d 1.92kgCOD/ (m) are brought up to3.d), COD clearance is stable in 80% water outlet SS (suspension)≤47mg/L at latter several days.During 16-35 days, processing water rises to 3m3/ h, intake and improved for anaerobism intermediate pool water outlet, reactor load to 2.8 kgCOD/ (m3.d), in ensuing 2 months, amount of inlet water is gradually increased to design the m of water 73/ h, reactor load are improved to 4.07kgCOD/ (m3.d) later stage water outlet COD clearance is stable more than 80%, water outlet SS (suspension)≤40mg/L.
Phase III is the oepration at full load phase：Reach 7m in water inlet3After/h, reactor water outlet 100% flows back, and organic loading reaches 4.5-5.3kgCOD/ (m3.d), gas production also gradually steps up, factor of created gase 2.7-3.9m3/(m3.d).Microscopy reactor organisms species branch is reasonable, and generation has granule sludge.After the processing of anaerobic reactor, COD clearance is more than 85%, SS (suspension)≤30mg/L.
During the startup of UASB anaerobic reactors, a PH instrument is installed on reactor water inlet pipe, according to water situation, an alkali measuring pump is set, controlled by PH instrument, makes reactor pH value stable 7.5 or so, avoids because water inlet acidifying makes reactor unbalance.
After the processing of UASB anaerobic reactors, the organic pollution in percolate such as aliphatic acid, hydro carbons, phenols, heterocyclic arene class, multiring aromatic hydrocarbon etc. is set all effectively to be removed, or it is decomposed into more degradable small molecule, significantly reduce the toxicity of percolate, heavy metal etc. has also obtained effective removal after a series of flocculation sediments.
The average influent CODs of UASB are in 20000mg/L or so, and after being tamed by inoculation, disposal ability gradually steps up reactor, and COD clearance is stable between 80-85%, reactor water outlet COD ＜ 4000mg/L, organic loading 4.8kgCOD/m3.d, while to reactor water outlet using 100% backflow.
The water outlet of UASB anaerobic reactors flows into two-stage contact oxidation pond and carries out aerobic reaction.This segment process is mainly characterized by same structures, by structures being divided into different regions, it is equipped with different aeration quantity, purify sewage the organic matter in sewage, ammonia nitrogen and phosphorus are degraded by different microorganisms flora under anaerobism, anoxic, aerobic situation, follow-up horizontal sedimentation tank is finally entered, carries out mud-water separation, precipitating sludge is discharged into sludge collecting pit, it is reallocated by sludge reflux water pump again, precipitation water outlet is reprocessed into MBR reaction tanks.
The total dischargeable capacity of two-stage contact oxidation processing system is 500m used by this unit3, 4.6 meters of pond body available depth, total residence time is 70 hours.Aerobic area, first order catalytic oxidation area, anoxic zone, second level catalytic oxidation area are divided into according to different functions.Aerobic area hydraulic detention time is 20 hours, receiving UASB anaerobic effluents, and the activated sludge mixed processing of partial reflux, and dissolved oxygen D0 is controlled in 0.5-1.0mg/L；One-level catalytic oxidation area hydraulic detention time is 20 hours, uses fiber soft-filler as biomembrane contact medium, feature is that specific surface area is big, voidage is high, hydraulic resistance is small, steady chemical structure, low cost, (2-3kg/m in light weight3) etc., this stage dissolved oxygen DO values are controlled in 3mg/L or so, and gas-water ratio is 10-15: 1；Anoxic zone hydraulic detention time is 14 hours, in this stage, water is not aerated, and the simultaneous oxygen bacterium allowed in water consumes remaining oxygen in water in metabolic process, carries out denitrification denitrogenation；Second level catalytic oxidation area hydraulic detention time is 16 hours, uses fiber soft-filler as biomembrane contact medium, and this stage dissolved oxygen DO values are controlled in 2.0-2.5mg/L.Stable 85% or so, unit water outlet COD ＜ 800mg/L, organic loading 2.5kgCOD/m by the COD clearances of contact oxidation pond processing unit3.d。
Waste water enters intermediate sedimentation pond in next step, is precipitated.
In present embodiment, using rectangular sedimentation tank, grow 4.6 meters in pond, it is wide 10 meters, bucket is highly 2.5 meters, and available depth is 2 meters, and the residence time is 13 hours, in order to reduce pollution of the ferro-aluminum ion for MBR films in follow-up MBR film process units, the step can effectively precipitate the aging sludge of contact-oxidation pool water outlet carrying.Further remove the COD in waste water simultaneously, the COD clearances of this element are 25% or so, unit water outlet COD ＜ 600mg/L.
Waste water enters in MBR reaction tanks in next step, and carries out MBR film process.
Reach primary standard to ensure to discharge water quality, immersion MBR membrane treatment appts are designed in MBR reaction tanks.Waste water carries out nitrification and denitrification reaction in MBR reaction tanks, can further remove the pollutants such as COD, BOD, ammonia nitrogen.Membrane bioreactor (MBR) technology is the New Wastewater Treatment Technology art that membrane separation technique organically combines with biotechnology, and it is retained the activated sludge in biochemical reaction tank and larger molecular organicses using membrane separation plant, saves second pond.Film-bioreactor technique enhances the function of bioreactor by the isolation technics of film significantly, and by two-stage aerobic biochemical treatment before, the biodegradability in water is reduced to 0.23 (BOD/COD) left and right, biochemical reduces, in conventional treatment process, the water in this stage has been difficult processing, but in membrane bioreactor, passes through the retention to activated sludge, bacterium, the bacterium of some hardly degraded organic substances of degraded is set to retain propagation, by the culture of the activated sludge of 2 months, domestication, greatly improve activated sludge concentration, bacterial species significantly increase.Membrane bioreactor makes its hydraulic detention time (HRT) and sludge retention time (SRT) to control respectively simultaneously.
MBR reaction tanks available depth is 3.5 meters.Reaction tank is divided into anaerobic zone, catalytic oxidation area and film process area three parts.Membrane module uses hollow fiber ultrafiltration membrane, and membrane material is Kynoar (PVDF), and membrane aperture is 0.2 μm, monolithic membrane area 20m2Aquifer yield is 3.8M3/ piece .d.The film process area residence time be 24 hours, sludge concentration 4500mg/L, water outlet COD in 90mg/L or so, SS=0, SDI value≤3, turbidity≤0.46NTU, meet nanofiltration inflow requirement.
System is after two-stage aerobic biochemistry, COD biodegradabilities in waste water also gradually reduce, COD in water can not be effectively reduced using the aeration method of routine, and use membrane bioreactor, it can be when water outlet, do not take away activated sludge, so since provide a good growing environment for breeding slower some processing difficult degradations COD microorganisms, this is not accomplish in conventional aerobic activated sludge process.
Water outlet by MBR reaction tanks and MBR film process is discharged after being handled further across nanofiltration (NF).The aperture of nanofiltration is mostly nanoscale, and boundary is between ultrafiltration and reverse osmosis filter.Nanofiltration is promoted by external pressure, and the TDS in water is retained.Because reverse osmosis membrane has very high rejection to all ions in water, and retention of the NF membrane to water intermediate ion has higher selectivity, and NF membrane only has very high rejection to divalent ion and molecular weight for 200-1000 organic matter.Therefore, from the technique of nanofiltration, without from reverse osmosis process, you can to ensure having higher clearance to COD in water, turn avoid dirty the problem of blocking up after reverse osmosis membrane long-time, extend the service life of system, reduce the operating cost of system.
In the present embodiment, nanofiltration is arranged using 2+1, uses the antipollution NF membrane of 6 U.S. TFC series, aquifer yield >=7m3/ h, is controlled using constant pressure frequency conversion, and Stress control produces water COD≤10mg/L in 0.35-0.4Mpa, the μ s.cm of conductance≤1000, reaches reclaimed water standard, and meet Guangdong Province's provincial standard《Sewage Water Emissions limit》(DB44/26-2001) the first period first discharge standard requirement.

Claims (10)

1. a kind of sewage water treatment method of percolate, it is characterised in that methods described includes step：(1) pre-treatment step, the pre-treatment step carry out flocculation preformed precipitate including percolate is added into flocculant in the basic conditions；(2) part denitrogenation is carried out through circulation blow-removing pond and stripping tower after alkalizing, (3) carry out anaerobic reaction in UASB anaerobic reactors；(4) Aerobic Process for Treatment is carried out using two-stage catalytic oxidation；(5) handled in membrane biological reaction pond；(6) percolate by the processing of membrane biological reaction pond is further handled with nanofiltration.
A kind of 2. sewage water treatment method of percolate according to claim 1, it is characterised in that：The alkalescence condition of the step (1) refers to pH value between 9~11, and flocculant is made using lime in step (1), and percolate preformed precipitate is no less than 2 hours after flocculant is added.
A kind of 3. sewage water treatment method of percolate according to claim 1, it is characterised in that：The step (2) refers to, add alkali in the percolate by pretreatment, ammonium ion therein is set to be converted into free ammonia, and percolate is set to flow into circulation blow-removing pond, delivered to again with pumping at the top of stripping tower and carry out spray water distribution, air blast is carried out from bottom to top from stripping tower bottom simultaneously, and polylith spiral board, the water counter current contacting that air stream sprays through polylith spiral board and top from bottom to top are installed inside the stripping tower.
A kind of 4. sewage water treatment method of percolate according to claim 3, it is characterised in that：Circulation blow-removing pond recycle ratio is 100: 25~35, and the gas liquid ratio of air blast is 400~800: 1, and processing air quantity is 11000~18000m3/h。
A kind of 5. method for treating garbage percolation liquid according to claim 1, it is characterised in that：Also include between the step (2) and step (3), the percolate through part deamination is flowed into horizontal sedimentation tank and carries out advection sedimentation, and flocculant is added before advection sedimentation；The flocculant is preferably using polymerization chlorine Change ferro-aluminum, the dosage of PAFC is 30~40mg/L, and pH value control is 7.5~9.
A kind of 6. sewage water treatment method of percolate according to claim 1, it is characterised in that：The residence time that the step (3) carries out anaerobic reaction in UASB anaerobic reactors is no less than 50 hours, water inlet uses the bottom that equally distributed perforated pipe water-locator makes waste water be uniformly introduced UASB reactors, temperature of reactor is stable at 30 DEG C~40 DEG C, and pH stable is 7~8.
A kind of 7. sewage water treatment method of percolate according to claim 6, it is characterised in that：In the step (3), percolate is flowed into before UASB anaerobic reactors, is introduced into anaerobism intermediate pool, and stop and be no less than 12 days in anaerobism intermediate pool.
A kind of 8. sewage water treatment method of percolate according to claim 1, it is characterised in that：When the step (4) carries out Aerobic Process for Treatment in two-stage contact oxidation pond, the residence time is no less than 60 hours, and intermediate sedimentation pond of the residence time no less than 10 hours is set behind two-stage contact oxidation pond.
A kind of 9. sewage water treatment method of percolate according to claim 8, it is characterised in that：The step (4) carries out Aerobic Process for Treatment using two-stage catalytic oxidation and referred to, two-stage contact oxidation pond is divided into aerobic area, first order catalytic oxidation area, anoxic zone, four, second level catalytic oxidation area different zones, each region is equipped with different aeration quantity, sewage is being purified the degraded of the organic matter in sewage, ammonia nitrogen and phosphorus by different microorganisms flora under anaerobism, anoxic, aerobic situation；Sewage and activated sludge are subjected to mixed processing after the aerobic area receiving UASB anaerobic effluents, dissolved oxygen control is no less than 17 hours in 0.5-1.0mg/L, hydraulic detention time；The first order catalytic oxidation area uses fiber soft-filler as biomembrane contact medium, and dissolved oxygen control is no less than 17 hours in 2.5-3.5mg/L, gas-water ratio 10-15: 1 of aeration, hydraulic detention time；The anoxic zone is without aeration, and the simultaneous oxygen bacterium allowed in water consumes remaining oxygen in water in metabolic process, carries out denitrification denitrogenation, and hydraulic detention time is no less than 12 hours；The second level catalytic oxidation area uses fiber soft-filler as biomembrane contact medium, and dissolved oxygen control is no less than 14 hours in 2.0-2.5mg/L, hydraulic detention time.
A kind of 10. method for treating garbage percolation liquid according to claim 1, it is characterised in that：The membrane biological reaction pond of the step (5) includes anaerobic zone, catalytic oxidation area and film process area three parts, and residence time of the percolate in film process area is that membrane module used hollow fiber ultrafiltration membrane no less than 20 hours.
CN201610438930.4A 2016-06-20 2016-06-20 A kind of sewage water treatment method of percolate Pending CN107522344A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610438930.4A CN107522344A (en) 2016-06-20 2016-06-20 A kind of sewage water treatment method of percolate

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610438930.4A CN107522344A (en) 2016-06-20 2016-06-20 A kind of sewage water treatment method of percolate

Publications (1)

Publication Number Publication Date
CN107522344A true CN107522344A (en) 2017-12-29

Family

ID=60734355

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610438930.4A Pending CN107522344A (en) 2016-06-20 2016-06-20 A kind of sewage water treatment method of percolate

Country Status (1)

Country Link
CN (1) CN107522344A (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110294565A (en) * 2019-04-15 2019-10-01 中山市天乙能源有限公司 A kind of percolate MBR treatment process of garbage incinerating power plant
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

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110294565A (en) * 2019-04-15 2019-10-01 中山市天乙能源有限公司 A kind of percolate MBR treatment process of garbage incinerating power plant
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
CN111285554B (en) * 2020-03-21 2022-08-12 云南兴滇实业有限公司 Method for deep purification treatment of landfill leachate

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
US8623213B2 (en) Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
CN101767914B (en) Method for treating garbage leachate
CN204897650U (en) Chemistry pharmacy effluent disposal system
CN206767868U (en) A kind of garbage percolation liquid treating system
CN103880253B (en) Garbage leachate advanced treatment method and Fenton reaction tower
CN105060627A (en) Chemical pharmacy wastewater comprehensive treatment system
CN202519137U (en) Combined treatment device of waste incineration field percolate
CN105060598A (en) Chemical pharmacy wastewater pretreatment system
CN102134141A (en) Method for treating garbage leachate
CN110395851A (en) High aititude urban wastewater treatment method based on nitrogen phosphorus capture and whole process autotrophic denitrification
CN201932982U (en) Combined system using micro-electrolysis-MBR (membrane bio-reactor) combined technology to treat printing and dyeing wastewater
CN101659502B (en) Method for treating waste leachate by utilizing high denitrification shared type Orbal oxidation ditch
CN108314255A (en) A kind of efficient Chinese herbal medicine extraction sewage treatment process
CN207828063U (en) A kind of coking wastewater processing system
CN109502911A (en) A kind of sewage water treatment method
CN1193943C (en) Garbage infiltration liquid treating method
CN107522344A (en) A kind of sewage water treatment method of percolate
CN208071544U (en) A kind of railway communication system production wastewater treatment system
CN106145351A (en) The processing equipment of garbage incinerating power plant Leachate site
CN109320029A (en) Liquor production wastewater processing method and system
CN204727736U (en) Waste leachate waste water processing

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20171229

WD01 Invention patent application deemed withdrawn after publication