CN107098531A - A kind of high-efficiency refuse percolate treating process - Google Patents

A kind of high-efficiency refuse percolate treating process Download PDF

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Publication number
CN107098531A
CN107098531A CN201710421092.4A CN201710421092A CN107098531A CN 107098531 A CN107098531 A CN 107098531A CN 201710421092 A CN201710421092 A CN 201710421092A CN 107098531 A CN107098531 A CN 107098531A
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membrane distillation
percolate
treating process
regulating reservoir
water outlet
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靳斌斌
刘友荣
陈燕波
郑莉
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Central and Southern China Municipal Engineering Design and Research Institute Co Ltd
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Central and Southern China Municipal Engineering Design and Research Institute Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/14—Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
    • 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
    • C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
    • 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
    • C02F1/48—Treatment of water, waste water, or sewage with magnetic or electric fields
    • C02F1/488—Treatment of water, waste water, or sewage with magnetic or electric fields for separation of magnetic materials, e.g. magnetic flocculation
    • 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
    • C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/06—Contaminated groundwater or leachate
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/14—NH3-N
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/046—Recirculation with an external loop

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

The invention discloses a kind of high-efficiency refuse percolate treating process, step includes：S1, percolate, which enter to be connected with the mixing regulating reservoir (1) of ozone, carries out oxidation Decomposition；S2, add PAC, magnetic, PAM successively into the percolate after oxidation Decomposition, add and finish rear percolate into precipitation in tube settler (3), precipitation dirt, which is back in mixing regulating reservoir (1), carries out oxidation Decomposition, and supernatant enters membrane distillation separate tank (4)；The progress membrane distillation reaction in membrane distillation separate tank (4) of S3, supernatant, is the water outlet after purification by distilling the liquid of film, is not back to progress oxidation Decomposition in mixing regulating reservoir (1) by distilling the concentrated leachate of film；It is back to after S4, the part cooling of water outlet in membrane distillation separate tank (4), the water outlet of remainder is final outflow water.By the scheme of " ozone oxidation+magnetic-coagulation+membrane distillation ", technique is simple, convenient management, and can effectively ensure outlet effect.

Description

A kind of high-efficiency refuse percolate treating process
Technical field
The present invention relates to field of garbage disposal, and in particular to a kind of high-efficiency refuse percolate treating process.
Background technology
Complicated component in percolate, pollutant concentration is high, and toxicity is big, can retain for a long time in the environment.Without place After the percolate discharge of reason, not only can polluted surface water and soil, or even can polluted drinking water source, underground water, crops, Aquatic animal etc., with bioaccumulation, teratogenesis, carcinogenic, cause gene mutation, in the healthy of the food chain top mankind Serious threat can be caused.The domestic processing method to percolate mainly has at biological treatment, materializing strategy and soil at present Reason method, wherein, " MBR+NF/RO " dual-membrane process and anaerobism+aerobic biochemistry combination process are generally to use prevailing technology, But there is also some problems." MBR+NF/RO " handling process can reach stable outlet effect, but technological process is long, Structures are more, complex management, and energy consumption is big, and film concentrate is difficult, operating cost is higher." anaerobism+aerobic biochemistry combines work Skill " can be effectively reduced BOD, COD and ammonia nitrogen in water, but ammonia nitrogen concentration is high in percolate, can cause carbon source not Foot, nutritive proportion imbalance, suppresses the activity of microorganism in biochemical treatment, causes the removal of COD in landfill leachate treatment, total nitrogen Rate is not high, and floor space is larger.
The content of the invention
In view of this, the invention provides a kind of high-efficiency refuse percolate treating process, compared to " MBR+NF/RO " film group Technique is closed, the process improving " MBR+NF/RO " technological process is long, and structures are more, complex management, and energy consumption is big, operating cost High the problem of；Compared to the biochemistry combination process of anaerobism+aerobic, the process improving " anaerobism+aerobic biochemistry combination process " Floor space is big, complex management, and water outlet CODcrThe problem of being difficult up to standard with ammonia nitrogen.
The invention provides a kind of high-efficiency refuse percolate treating process, step includes：
S1, percolate, which enter to be connected with the mixing regulating reservoir of ozone, carries out oxidation Decomposition；
S2, add PAC, magnetic, PAM successively into the percolate after oxidation Decomposition, add and finish rear percolate and enter oblique Precipitated in pipe sedimentation basin, precipitation dirt, which is back in mixing regulating reservoir, carries out oxidation Decomposition, and supernatant enters membrane distillation separate tank；
Supernatant carries out membrane distillation reaction in membrane distillation separate tank described in S3, step S2, is by the liquid for distilling film Water outlet after purification, not by distill the concentrated leachate of film be back to mixing regulating reservoir in carry out oxidation Decomposition；
It is back to after the part cooling of water outlet described in S4, step S3 in membrane distillation separate tank, the water outlet of remainder is Final outflow water.
The beneficial effects of the invention are as follows：1st, the present invention only allows the performance that hydrone passes through using film distillation technology, uses " magnetic-coagulation precipitation+membrane distillation separation ", technique is simple, convenient management, and can effectively ensure outlet effect；2nd, it is of the invention There is the performance of advanced oxidation using ozone technology, concentrate of intaking and flow back to percolate carries out aerobic digestion, enters one Oxidation Decomposition organic matter therein is walked, and carries out efficient disinfection；3rd, the present invention provides thermal source using solar energy system, real Show effective utilization and the effects of energy saving and emission reduction of green energy resource, reduce operation cost.4th, without poisonous when the present invention is handled The bad student of harmful substance, reduces secondary pollution.
Brief description of the drawings
The high-efficiency refuse percolate treating process schematic diagram that Fig. 1 provides for the present invention；
Wherein, 1 be mixing regulating reservoir, 2 for add pond, 3 be tube settler, 31 be inclined tube group, 32 be downflow weir, 4 be Membrane distillation reaction tank, 41 be distillation film component, 42 be heater, 43 be back purge system, 5 be ozone generator, 6 be lifting Pump, 7 be film water outlet circulating cooling unit, 71 be drain pipe, 72 be liquid back pipe, 73 be coolant circulation pump A, 74 be coolant circulation pump B, 75 be cooling tank, 8 be reflux pump A, 9 be outlet pipe, 10 be film water outlet on-line monitoring pipeline, 11 be gas suction pump, 12 be Solar source absorption plant, 13 are temperature monitor, and 14 be reflux pump B.
Embodiment
The invention provides a kind of high-efficiency refuse percolate treating process, step includes：
S1, percolate, which enter to be connected with the mixing regulating reservoir of ozone, carries out oxidation Decomposition；
S2, add PAC, magnetic, PAM successively into the percolate after oxidation Decomposition, add and finish rear percolate and enter oblique Precipitated in pipe sedimentation basin, precipitation dirt, which is back in mixing regulating reservoir, carries out oxidation Decomposition, and supernatant enters membrane distillation separate tank；
Supernatant carries out membrane distillation reaction in membrane distillation separate tank described in S3, step S2, is by the liquid for distilling film Water outlet after purification, not by distill the concentrated leachate of film be back to mixing regulating reservoir in carry out oxidation Decomposition；
It is back to after the part cooling of water outlet described in S4, step S3 in membrane distillation separate tank, the water outlet of remainder is Final outflow water.
This technique is long in order to solve landfill leachate treatment " MBR+NF/RO " technological process, and structures are more, and management is multiple Miscellaneous, energy consumption is big, and " anaerobism+aerobic biochemistry combination process " floor space is big, and water outlet CODcrIt is difficult with ammonia nitrogen up to standard Influenced each other between problem, each step of scheme of " ozone oxidation+magnetic-coagulation+membrane distillation ", association of mutually promoting, adopted by (1) Ozone high grade oxidation scheme is taken, can effectively solve the problems, such as that film concentrates liquid difficult degradation；(2) ozone oxidation+magnetic-coagulation is taken to sink Shallow lake scheme can reduce MBR technique one-levels denitrification, one-level nitrification, two grades of denitrifications, two grades of nitrifications, Complicated Flows of ultrafiltration, Reduce structures and streamlining management；(3) by using membrane distillation scheme, NF/RO energy consumptions and operating cost can be reduced；(4) lead to Use magnetic-coagulation+membrane distillation scheme is crossed, " anaerobism+aerobic biochemistry combination process " floor space can be saved, streamlining management, Ensure outlet effect.
It is preferred that, the O in the mixing regulating reservoir3Concentration is 0.4mg/L~0.8mg/L.
It is preferred that, the PAC dosages are 20~30mg/L, and PAM dosages are 0.8~1.2mg/L, and magnetic dosage is 3~5mg/L, the magnetic is F3O4.Magnetic is added so that water-borne glue body particle and magnetic powder particle be easier collision it is de- steady and Flco is formed, the removal efficiency of suspension is substantially increased.Meanwhile, the super hyperbaric characteristic of magnetic causes flco density to be much larger than Conventional coagulation flco, so as to greatly improve settling velocity, and completes efficiently separating for muddy water.
It is preferred that, the membrane distillation separate tank temperature maintains 45-60 DEG C, and pH is 6.0-7.5.
More preferred, the membrane distillation separate tank uses solar energy heating.By to solar energy this clean energy resource Utilize, reduce processing cost.
More preferred, what being cooled to described in step S4 made backflow is water-cooled to 10-20 DEG C.Into membrane distillation separate tank Supernatant realize that membrane distillation reacts under the action of thermal difference that solar heating system and cooling backwater are provided so that vapor Opposite side, and final outflow water are entered from the side of film, the percolate of concentration is back to mixing regulating reservoir through reflux pump and carries out oxygen Change and decompose.
It is preferred that, the long 1-1.2m of inclined tube in tube settler described in step S2, inclination angle is 60 °, and the inclined tube top depth of water is 0.5-1.0m。
Below in conjunction with specific embodiment to a kind of high-efficiency refuse percolate treating process of the invention provided with further Explanation.The embodiments described below is exemplary, is only used for explaining the present invention, and is not considered as limiting the invention.
Experimental method in following embodiments, is conventional method unless otherwise specified.Reality used in following embodiments Test material unless otherwise specified, be that market is commercially available.
Embodiment one
Present embodiments provide a kind of high-efficiency refuse percolate treating process, and the device that the technique is used.
The device that above-mentioned technique is used includes：The mixing regulating reservoir 1 that is sequentially connected, add pond 2, tube settler 3, film and steam Evaporate reaction tank 4.
It is described mixing the inner space of regulating reservoir 1 connected with an ozone generator 5, it is described mixing regulating reservoir 1 delivery port and Elevator pump 6 is connected by water pipe, and the elevator pump 6 is connected with adding the water inlet in pond 2 by water pipe.
The pond 2 that adds includes the PAC that is sequentially connected and adds area 21, magnetic and add area 22, PAM to add area 23.
The inner upper of tube settler 3 is provided with inclined tube group 31, and the inclined tube group includes many length 1-1.2m, inclined Oblique angle is 60 ° of inclined tube, and the inclined tube top depth of water is 0.5-1.0m.The outlet at bottom of tube settler 3 and reflux pump A8 Connection, the reflux pump A8 is connected with mixing regulating reservoir 1.Downflow weir 32, the overflow are provided with above the side wall of tube settler 3 Weir 32 is connected with membrane distillation reaction tank 4 by water pipe.
Distillation film component 41, heater 42, back purge system 43 are provided with the membrane distillation reaction tank 4.The distillation Membrane module 41 is plate and frame component, and distillation film is used to be used in hydrophobicity PVF pvdf membrane or polypropylene PP films, the present embodiment Hydrophobicity PVF pvdf membrane.The distillation film component 41 is connected with film water outlet circulating cooling unit 7, and it is cold that the film goes out water circulation But time liquid that unit 7 includes the drain pipe 71 being connected with the liquid outlet of distillation film component 41 and is connected with the liquid return hole of distillation film component 41 Pipe 72, the drain pipe 71 is connected with coolant circulation pump A73, the liquid back pipe 72 and coolant recirculation pump B74, cooling tank 75 according to Secondary connection, the outlet of the drain pipe 71 is connected with the entrance of liquid back pipe 72, outlet pipe 9, and the outlet pipe 9 and film water outlet are online Monitoring pipeline 10 is connected.The membrane distillation reaction tank 4 is internally located at the lower section of distillation film component 41 and is provided with back purge system 43, steams Membrane module 41 and back purge system 43 is evaporated to fix by the support of the bottom steel frame of membrane distillation reaction tank 4 respectively.Specifically, backwash Device 43 carries out gas bleed by the solarization air cap on pipeline to film surface, and the back purge system 43 connects with gas suction pump 11 Connect, intermittent duty, decelerating membrane pollution.The heater 42 is connected with solar source absorption plant 12, the membrane distillation reaction The inside of pond 4 is connected with temperature monitor 13.The inner bottom part of membrane distillation reaction tank 4 is connected with reflux pump B14, the reflux pump B14 is connected with mixing regulating reservoir 1.
The high-efficiency refuse percolate treating process, including：
S1, the percolate flow by gravity enter mixing regulating reservoir 1, and carry out oxidation point in mixing regulating reservoir 1 Solution, wherein ozone comes from O in ozone generator 2, the mixing regulating reservoir 1 in mixing regulating reservoir 13Concentration be 0.4mg/L~ 0.8mg/L。
Percolate after S2, oxidation Decomposition is entered by elevator pump 6 adds pond 2, and passes sequentially through PAC and add area 21, magnetic Powder (F3O4) add area 22, PAM and add area 23 and enter back into tube settler 3, the PAC dosages are 20~30mg/L, and PAM is thrown Dosage is 0.8~1.2mg/L, F3O4Dosage is 3~5mg/L.Added by PAC, magnetic and PAM mixing, wherein, magnetic Powder is added so that it is de- steady and forms flco that water-borne glue body particle and magnetic powder particle are easier collision, substantially increases suspension Removal efficiency.Meanwhile, the super hyperbaric characteristic of magnetic causes flco density to be much larger than conventional coagulation flco, so as to greatly improve Settling velocity, and complete efficiently separating for muddy water；In addition, the precipitating sludge in the tube settler 3 flows back through reflux pump A8 To mixing regulating reservoir 1, percolate supernatant discharges water to membrane distillation separate tank 4 by the top downflow weir 32 of tube settler 3；
The temperature difference that S3, the supernatant into membrane distillation separate tank 4 are provided in solar heating system and cooling recirculation system 7 Under effect, realize that membrane distillation reacts by distillation film component 41 so that vapor enters on the inside of film on the outside of the film, and it is final from Inner side water outlet, the percolate of concentration is back to mixing regulating reservoir 1 through reflux pump B14；The solar heating system is by solar energy Absorption plant 12 and solar heat collector 42 are constituted, and wherein solar heat collector 42 is arranged in the outer of distillation film component 41 Side, and provide energy by solar energy absorption plant 12；The cooling recirculation system is by coolant circulation pump A73, coolant circulation pump B74 Constituted with cooling tank 75, wherein cooling system is connected with the inner side of distillation film component 41, realize the cooling circulation of water；
S4, the distillation film water outlet enter film water outlet monitoring device 10 by coolant circulation pump A73 rear portions, and finally Water outlet is realized, a part enters distillation film component 41 after cooling tank 75, to maintain the lasting progress of cooling recirculation system；It is described The temperature T of membrane distillation separate tank 4 maintains 45-55 DEG C, and pH is 6.5-7.5, and cooling system temperature T maintains 10-15 DEG C；It is described mixed Close the O in regulating reservoir 13Concentration 0.4mg/L~0.8mg/L；The PAC dosages are 20~30mg/L, and PAM dosages are 0.8 ~1.2mg/L, F3O4Dosage is 3~5mg/L；Tube settling district (7) the inclined tube plagioclase is generally 1-1.2m, and inclination angle is 60 °, the inclined tube top depth of water is 0.5-1.0m；The back purge system 43 is arranged in the lower section of membrane module 41.Wherein membrane module 41 Fixed respectively by the support of reaction tank bottom steel frame with back purge system 43, relative position is as shown in the figure.Back purge system 43 By the solarization air cap on pipeline, gas bleed is carried out to film surface, wherein gas enters pipeline through backwashing pump 11.
The percolate of Hubei refuse landfill is handled using above-mentioned technique, percolate influent CODcrConcentration For 4500mg/L, BOD5Concentration is 1200mg/L, NH3- N concentration is 2000mg/L, and SS concentration is 800mg/L；
In test run, distillation film reaction pond water temperature (T) is 50-60 DEG C, and cooling system temperature T maintains 15-20 DEG C, PH is 6.0-7.5, and reactor continuous service, initial membrane flux is 15.0-20.0L/m2h.Ozone regulating reservoir O3Concentration 0.6mg/L； PAC dosages are 20.0mg/L, and PAM dosages are 1.0mg/L, F3O4Dosage is 4mg/L.
Testing water outlet result is：Water outlet CODcrConcentration is 82.0mg/L, BOD5Concentration is 15.0mg/L, NH3- N concentration is 21.0mg/L, SS concentration are 12.0mg/L.As a result show, COD in percolatecrClearance reached 98.1%, BOD5 Clearance reaches 98.7%, realizes NH3The 98.9% of-N ions is removed.
Embodiment two
A kind of high-efficiency refuse percolate treating process is present embodiments provided, the device of use is identical with embodiment one, had Body treatment process steps and the processing step of embodiment one are basically identical, and difference is：
The percolate of above-mentioned Hubei refuse landfill is handled, in test run, film reaction water temperature is distilled It is 45-55 DEG C to spend (T), and cooling system temperature T maintains 10-15 DEG C, and pH is 6.5-7.5, and reactor continuous service, initial film is led to Measure as 15.0-20.0L/m2h.Ozone regulating reservoir O3Concentration 0.4mg/L；PAC dosages are 25.0mg/L, and PAM dosages are 0.8mg/L, F3O4Dosage is 5mg/L.
Testing water outlet result is：Water outlet CODcrConcentration is 80.0mg/L, BOD5Concentration is 16.0mg/L, NH3- N concentration is 20.0mg/L, SS concentration are 11.0mg/L.Treatment effect and embodiment one are basically identical.
Embodiment three
A kind of high-efficiency refuse percolate treating process is present embodiments provided, the device of use is identical with embodiment one, had Body treatment process steps and the processing step of embodiment one are basically identical, and difference is：
The percolate of above-mentioned Hubei refuse landfill is handled, in test run, film reaction water temperature is distilled It is 48-58 DEG C to spend (T), and cooling system temperature T maintains 12-17 DEG C, and pH is 6.0-7.0, and reactor continuous service, initial film is led to Measure as 15.0-20.0L/m2h.Ozone regulating reservoir O3Concentration 0.8mg/L；PAC dosages are 30.0mg/L, and PAM dosages are 1.2mg/L, F3O4Dosage is 3mg/L.
Testing water outlet result is：Water outlet CODcrConcentration is 83.0mg/L, BOD5Concentration is 15.0mg/L, NH3- N concentration is 23.0mg/L, SS concentration are 12.0mg/L.Treatment effect and embodiment one are basically identical.
The foregoing is only presently preferred embodiments of the present invention, be not intended to limit the invention, it is all the present invention spirit and Within principle, any modification, equivalent substitution and improvements made etc. should be included in the scope of the protection.

Claims (7)

1. a kind of high-efficiency refuse percolate treating process, it is characterised in that：Step includes：
S1, percolate, which enter to be connected with the mixing regulating reservoir (1) of ozone, carries out oxidation Decomposition；
S2, add PAC, magnetic, PAM successively into the percolate after oxidation Decomposition, add that to finish rear percolate heavy into inclined tube Precipitated in shallow lake pond (3), precipitation dirt, which is back in mixing regulating reservoir (1), carries out oxidation Decomposition, and supernatant is separated into membrane distillation Pond (4)；
Supernatant described in S3, step S2 carries out membrane distillation reaction in membrane distillation separate tank (4), is net by distilling the liquid of film Water outlet after change, is not back to progress oxidation Decomposition in mixing regulating reservoir (1) by distilling the concentrated leachate of film；
It is back to after the part cooling of water outlet described in S4, step S3 in membrane distillation separate tank (4), the water outlet of remainder is most Whole water outlet.
2. high-efficiency refuse percolate treating process as claimed in claim 1, it is characterised in that：In the mixing regulating reservoir (1) O3Concentration is 0.4mg/L~0.8mg/L.
3. high-efficiency refuse percolate treating process as claimed in claim 1, it is characterised in that：The PAC dosages be 20~ 30mg/L, PAM dosage are 0.8~1.2mg/L, and magnetic dosage is 3~5mg/L, and the magnetic is F3O4。
4. high-efficiency refuse percolate treating process as claimed in claim 1, it is characterised in that：The membrane distillation separate tank (4) Interior temperature maintains 45-60 DEG C, and pH is 6.0-7.5.
5. high-efficiency refuse percolate treating process as claimed in claim 4, it is characterised in that：The membrane distillation separate tank (4) Using solar energy heating.
6. high-efficiency refuse percolate treating process as claimed in claim 4, it is characterised in that：It is described to be cooled to be cooled to 10-20℃。
7. high-efficiency refuse percolate treating process as claimed in claim 1, it is characterised in that：In the tube settler (3) The long 1-1.2m of inclined tube, inclination angle is 60 °, and the inclined tube top depth of water is 0.5-1.0m.
CN201710421092.4A 2017-06-07 2017-06-07 A kind of high-efficiency refuse percolate treating process Pending CN107098531A (en)

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CN107473481A (en) * 2017-08-31 2017-12-15 河海大学 The garbage percolation liquid treating system and method for ultrasonic stripping film distillation technology combination
CN108467150A (en) * 2018-03-22 2018-08-31 中山市天乙能源有限公司 A kind of leachate pretreatment method of garbage incinerating power plant
CN108751550A (en) * 2018-05-25 2018-11-06 中节能工程技术研究院有限公司 A kind of processing method and processing system of landfill leachate tail water
CN110550815A (en) * 2019-07-29 2019-12-10 郑州大学 Device and method for advanced treatment of old landfill leachate
CN110902967A (en) * 2019-12-10 2020-03-24 中国科学院生态环境研究中心 Wastewater treatment method and wastewater treatment system based on sequencing batch membrane biological reaction
CN113698015A (en) * 2020-05-21 2021-11-26 河海大学 Electro-catalysis and membrane distillation-based landfill leachate concentrated solution treatment system and method
CN113800726A (en) * 2021-10-27 2021-12-17 苏州绿业环境发展有限公司 Method for treating landfill leachate and concentrated solution
CN115259566A (en) * 2022-08-16 2022-11-01 深圳市环境科学研究院 Method for deep biological treatment of nanoscale electronic chip wastewater

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Publication number Priority date Publication date Assignee Title
CN107473481A (en) * 2017-08-31 2017-12-15 河海大学 The garbage percolation liquid treating system and method for ultrasonic stripping film distillation technology combination
CN108467150A (en) * 2018-03-22 2018-08-31 中山市天乙能源有限公司 A kind of leachate pretreatment method of garbage incinerating power plant
CN108751550A (en) * 2018-05-25 2018-11-06 中节能工程技术研究院有限公司 A kind of processing method and processing system of landfill leachate tail water
CN110550815A (en) * 2019-07-29 2019-12-10 郑州大学 Device and method for advanced treatment of old landfill leachate
CN110902967A (en) * 2019-12-10 2020-03-24 中国科学院生态环境研究中心 Wastewater treatment method and wastewater treatment system based on sequencing batch membrane biological reaction
CN113698015A (en) * 2020-05-21 2021-11-26 河海大学 Electro-catalysis and membrane distillation-based landfill leachate concentrated solution treatment system and method
CN113800726A (en) * 2021-10-27 2021-12-17 苏州绿业环境发展有限公司 Method for treating landfill leachate and concentrated solution
CN115259566A (en) * 2022-08-16 2022-11-01 深圳市环境科学研究院 Method for deep biological treatment of nanoscale electronic chip wastewater

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Application publication date: 20170829