CN111253016A - Treatment system and method for landfill leachate - Google Patents

Treatment system and method for landfill leachate Download PDF

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CN111253016A
CN111253016A CN202010209535.5A CN202010209535A CN111253016A CN 111253016 A CN111253016 A CN 111253016A CN 202010209535 A CN202010209535 A CN 202010209535A CN 111253016 A CN111253016 A CN 111253016A
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tank
enters
membrane
effluent
composite
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吴昊
陈越
丁庆章
周玲
陈建军
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Zhejing Yiqing Environmental Protection Engineering Co ltd
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Zhejing Yiqing Environmental Protection Engineering 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
    • 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
    • C02F1/34—Treatment of water, waste water, or sewage with mechanical oscillations
    • C02F1/36—Treatment of water, waste water, or sewage with mechanical oscillations ultrasonic vibrations
    • 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
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • 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
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • 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
    • C02F3/00—Biological 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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2833—Anaerobic digestion processes using fluidized bed reactors

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  • Engineering & Computer Science (AREA)
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  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

The invention relates to a system and a method for treating landfill leachate, which comprises a pretreatment subsystem, a biochemical treatment subsystem, an advanced treatment subsystem and a membrane treatment subsystem which are sequentially communicated, wherein the pretreatment subsystem comprises a grid, an oil separation tank, an adjusting tank and an ultrasonic air stripping and floating tank which are sequentially communicated; the biochemical treatment subsystem comprises a composite anaerobic fluidized bed reactor and a composite membrane bioreactor which are communicated in sequence, the advanced treatment subsystem comprises an electrocatalytic oxidation device and a sand filter tank which are communicated in sequence, and the membrane treatment subsystem comprises a disc tube type reverse osmosis membrane processor. The invention pretreats the landfill leachate firstly, reduces ammonia nitrogen and COD, and improves biodegradability; the effluent of the oxidation pond enters a biochemical treatment system, the biochemical effluent enters an electrocatalytic oxidation device, the electrocatalytic effluent enters a sand filter tank, the effluent enters a DTRO membrane treatment system, and the membrane effluent is directly discharged or recycled; the invention has the advantages of reliable process, stable operation, standard effluent and the like.

Description

Treatment system and method for landfill leachate
Technical Field
The invention belongs to the technical field of water treatment, and particularly relates to a system and a method for treating landfill leachate.
Background
According to statistical data, the harmless treatment rate of domestic garbage in China is on the trend of increasing year by year, and the garbage treatment and disposal modes in China are mainly sanitary landfill and incineration. Since the non-combustible waste is finally disposed of by landfill, either in a near-stage garbage disposal method mainly for landfill or in a future garbage disposal method mainly for incineration. The most interesting problem for landfill sites is the problem of leachate treatment.
The leachate is a liquid containing organic or inorganic components generated under the physical, biological and chemical actions of compaction, fermentation and the like in the process of stacking and landfill of the garbage and under the seepage action of precipitation and other external incoming water, and the leachate generally has the characteristics of high pollutant content, high ammonia nitrogen content, high chromaticity, strong toxicity, long pollution time and the like, and is high-concentration organic wastewater with complex components. With the increase of landfill age, the degradation rate of microorganisms to organic matters in the garbage, the water holding capacity of the garbage and the permeability of water can be changed, most of the organic matters in percolate of middle and old aged landfill sites are long-chain carbohydrate or humus which are difficult to degrade, and the landfill site has the characteristics of low content of biodegradable substances and high ammonia nitrogen concentration.
The treatment method of the landfill leachate comprises a physical-chemical method, the physical-chemical method mainly comprises various methods such as activated carbon adsorption, chemical precipitation, density separation, chemical oxidation, chemical reduction, ion exchange, membrane dialysis, gas stripping and wet oxidation, and when COD is 2000-4000 mg/L, the removal rate of the COD by the physical-chemical method can reach 50-87%. Compared with biological treatment, the physicochemical treatment is not influenced by the change of water quality and quantity, the effluent quality is more stable, especially to BOD5The landfill leachate which has a low COD ratio (0.07-0.20) and is difficult to biologically treat has a good treatment effect. But the physical and chemical method has higher treatment cost and is not suitable for treating the large-water-volume landfill leachate.
Disclosure of Invention
The invention aims to provide a system and a method for treating landfill leachate, which have the advantages of reliable process, stable operation and standard effluent.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a treatment system for landfill leachate comprises a pretreatment subsystem, a biochemical treatment subsystem, an advanced treatment subsystem and a membrane treatment subsystem which are sequentially communicated, wherein the pretreatment subsystem comprises a grid, an oil separation tank, an adjusting tank and an ultrasonic air stripping tank which are sequentially communicated; the biochemical treatment subsystem comprises a composite anaerobic fluidized bed reactor (UBF) and a composite membrane bioreactor (HMBR) which are communicated in sequence, the advanced treatment subsystem comprises an electrocatalytic oxidation device and a sand filter tank which are communicated in sequence, and the membrane treatment subsystem comprises a disc tube type reverse osmosis membrane (DTRO) processor.
Preferably, the ultrasonic air-stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor are respectively communicated with a sludge concentration tank, and the sludge concentration tank is communicated with the membrane filter press. Discharging sludge generated by the ultrasonic air-stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, and transporting the dewatered dry sludge to the outside for final treatment.
The invention also provides a method for treating the landfill leachate, which comprises the following steps:
(1) the garbage percolate sequentially enters a grid, an oil separation tank and an adjusting tank;
(2) the wastewater enters an ultrasonic air-stripping flotation tank from a regulating tank, and a demulsifier is added;
(3) the effluent of the air floatation tank enters an oxidation tank, and an oxidant is added;
(4) the effluent of the oxidation pond enters a composite anaerobic fluidized bed reactor (UBF);
(5) the effluent of the composite anaerobic fluidized bed reactor enters a composite membrane bioreactor (HMBR);
(6) the effluent of the composite membrane bioreactor enters an electrocatalytic oxidation device;
(7) the effluent of the electrocatalytic oxidation device enters a sand filter tank;
(8) the effluent of the sand filtration tank enters a disc tube type reverse osmosis membrane (DTRO) processor, and the effluent is discharged after reaching the standard or reclaimed water is recycled;
(9) discharging sludge generated by the ultrasonic air-stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, transporting the dewatered sludge out for final treatment, and refluxing the sewage to the regulating tank.
Ultrasonic air stripping float
Toxic and refractory substances and multi-carbon-chain complex organic matter macromolecules are directly degraded into single-carbon substances and low-molecular organic matters by ultrasonic waves, so that the biodegradability of the waste water is improved. When ultrasonic waves with certain intensity pass through a wastewater medium, a series of physical and chemical effects are generated. The ultrasonic wave acts on different sound intensities, sound densities and sound frequencies in the wastewater to generate the following seven physical and chemical effects: mechanical effect, thermal effect, dissolved oxygen and cavitation cleaning effect, pyrolysis digestion and free radical oxidation effect, acoustic flow promoting particle moving effect, biochemical reaction accelerating mass transfer effect, and sludge flocculation precipitation accelerating thixotropic effect. The ultrasonic wave has a promoting effect on the flocculation of the wastewater.
Combined anaerobic fluidized bed reactor (UBF)
The granular sludge and the biological membrane are integrated, and the operation result shows that COD (chemical oxygen demand) is high when the garbage percolate with large water quality change and high pollutant concentration is treatedCr、BOD5The removal rate of SS and ammonia nitrogen is more than 99.8 percent, and the technology is feasible, economical and reasonable.
UBF has a very high biosolid retention time (SRT) and can effectively degrade toxic substances, and is an effective and economical technique for treating high-concentration organic wastewater. UBF is a reaction apparatus for treating organisms by using fluidization technology, which takes sand and soft filler in equipment as fluidization carriers, takes sewage as flowing medium, and anaerobic microorganisms are combined on the surfaces of the sand and the soft filler in a biofilm form and are automatically mixed when methane gas is generated in a circulating pump or a sewage treatment process, so that the sewage is in a flowing state. When the sewage passes through the bed body in an up-flow mode, the sewage is continuously contacted and reacted with the carrier attached with the anaerobic biomembrane in the bed, and the purposes of decomposing and adsorbing organic matters in the sewage through an anaerobic reaction are achieved. The UBF has the advantages of high efficiency, small occupied area and suitability for organic sewage treatment engineering with higher concentration.
Combined type membrane bioreactor (HMBR)
HMBR is a novel efficient sewage treatment system formed by organically combining a membrane separation technology with a traditional wastewater bioreactor. The HMBR integrates the common advantages of biodegradation and efficient interception of the membrane in an activated sludge process, can greatly improve the effluent of a system, and can effectively delay membrane pollution and improve the service efficiency of the membrane due to lower sludge concentration in a membrane component separation zone. The method utilizes the HMBR technology to research the deamination operation environment of landfill leachate, the removal rate of ammonia nitrogen reaches 95% -98%, and the HMBR is adopted to treat high-concentration ammonia nitrogen landfill leachate, so that macromolecular substances can be effectively degraded, and the ammonia nitrogen can be efficiently removed. Particularly, the removal of ammonia nitrogen in the landfill leachate at the middle and later stages is difficult for landfill leachate treatment, and the old landfill leachate is treated by adopting the HMBR process, so that the sludge concentration in the HMBR is higher, and a great effect on the removal of ammonia nitrogen is achieved.
DTRO disc tube type reverse osmosis
The DTRO process for treating the landfill leachate has the advantages of strong stability, simple maintenance and low energy consumption, and the DTRO membrane component effectively avoids the scaling of the membrane, lightens the membrane pollution and prolongs the service life of the reverse osmosis membrane.
Compared with other membrane components, the disc-tube reverse osmosis has the following three obvious characteristics: wide channel, short flow path and high popularity. The three characteristics determine that the disc-tube reverse osmosis technology can tolerate higher suspended matters and SDI (standard data interface) when treating percolate, namely, the blockage is avoided. Meanwhile, the three technical characteristics are embodied in specific practice, so that the disc-tube membrane technology has the following engineering characteristics: 1) the scale formation of the membrane group is less, the membrane pollution is light, and the service life of the membrane is long; 2) does not depend on pretreatment, and has good stability, safety and adaptability; 3) has very reliable processing effect; 4) the installation and maintenance are simple, the operation is convenient, and the automation degree is high; 5) the system expandability is strong.
Preferably, the demulsifier in the step (2) is one of ferric chloride, calcium chloride, ferrous sulfate, aluminum sulfate and polyaluminium chloride (PAC), and the addition amount is 0.1-1.0 g/L.
Preferably, the oxidant in the step (3) is potassium ferrate, the addition amount is 5-100 mg/l, the retention time is 0.5-2 h, and the pH value is 7-9.
The potassium ferrate is used as an efficient, novel and environment-friendly non-chlorine multifunctional wastewater treatment agent, can effectively remove various organic or inorganic pollutants and heavy metal ions in wastewater and quickly kill various bacteria, viruses and algae in the wastewater, integrates multiple functions of oxidation, disinfection, decoloration, deodorization, coagulation aid and the like, and does not produce secondary pollution and other side effects. Potassium ferrate, due to its strong oxidizing properties and the Fe (OH) produced when it dissolves in water3The adsorption effect on various anions and cations is a green, novel and efficient multifunctional water treatment agent, can effectively remove organic pollutants in water, and can safely and obviously oxidize sulfides and CN in the water-1The heavy metal also has adsorption and sedimentation effects, and can be used for disinfection, decolorization, deodorization, oxidation, sterilization, etc. Potassium ferrate to organic pollutants and NH4+The removal of-N is due to its strong oxidation and the newly formed floc structure Fe (OH)3Flocculation coordination results.
Preferably, the pH value of the composite anaerobic fluidized bed reactor is controlled to be 6.5-8, the water temperature is +/-30 ℃, and the hydraulic retention time is 18-40 h.
The sludge bed composed of high-concentration granular sludge is arranged below the UBF, the mass concentration of Mixed Liquid Suspended Solids (MLSS) can reach dozens of grams per liter, and the filter material layer composed of filler and attached biological membranes is arranged on the upper part of the UBF. Preferably, the step (4) is specifically: wastewater enters from the bottom of the composite anaerobic fluidized bed reactor, after anaerobic treatment reaction is sequentially carried out on the wastewater through a granular sludge layer and a floc sludge layer, water from the sludge layer enters a filter material layer, gas-liquid-solid separation is carried out, the water is discharged from the top of the filter material layer, and gas is conveyed out and then is stored or directly used; the hydraulic retention time of the composite anaerobic fluidized bed reactor is 12-32 h.
Preferably, the step (5) is specifically: the composite membrane bioreactor comprises an anoxic zone, an aerobic zone, a precipitation zone and an intermediate water tank, wherein the biological reaction zone of the composite membrane bioreactor is divided into the anoxic zone and the aerobic zone by a partition board, both the anoxic zone and the aerobic zone are filled with composite fillers, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition board, and the mixed liquor in the aerobic zone returns to the anoxic zone by an aeration device; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters the middle tank, and a hollow fiber membrane component is arranged in the middle tank and used for pumping and draining water.
Preferably, in the electrocatalytic oxidation device in the step (6), the direct distance between the anode and cathode plates is 2-6 mm, the voltage of the anode and cathode plates is 10-20V, the hydraulic retention time is 0.3-2 h, and the power supply current is constant at 10-200A.
Preferably, the reverse osmosis membrane used by the disc tube type reverse osmosis membrane (DTRO) processor in the step (8) is a membrane for seawater desalination, the operation pressure is 30-70 bar, the temperature is 0-40 ℃, and the system recovery rate is 50-93%.
Compared with the prior art, the invention has the beneficial effects that:
the method comprises the steps of pretreating the landfill leachate, enabling the leachate to sequentially enter a grid and an oil separation tank regulating tank, enabling effluent to enter an ultrasonic air-stripping and air-floating tank, enabling the effluent to enter an oxidation tank through air-stripping and air-floating, removing hydrogen sulfide, suspended matters, oils and the like, reducing ammonia nitrogen and COD, and improving biodegradability; the effluent of the oxidation pond enters a UBF + HMBR biochemical treatment system, the biochemical effluent enters an electrocatalytic oxidation device, the electrocatalytic effluent enters a sand filter tank, the effluent enters a DTRO membrane treatment system, and the membrane effluent is directly discharged or recycled; the invention has the advantages of reliable process, stable operation, standard effluent and the like.
Drawings
FIG. 1 is a schematic block diagram of a landfill leachate treatment system according to embodiment 1 of the present invention;
FIG. 2 is a schematic block diagram of a landfill leachate treatment system according to embodiment 2 of the present invention;
FIG. 3 is a schematic structural diagram of a combined anaerobic fluidized bed reactor according to the present invention;
FIG. 4 is a schematic structural diagram of the composite membrane bioreactor of the present invention.
Detailed Description
The invention will be further described with reference to the following figures and specific examples, without limiting the scope of the invention thereto. Those skilled in the art can and should understand that any simple changes or substitutions based on the spirit of the present invention should fall within the protection scope of the present invention.
Example 1
Referring to fig. 1, fig. 3 and fig. 4, the system for treating the landfill leachate comprises a pretreatment subsystem, a biochemical treatment subsystem, an advanced treatment subsystem and a membrane treatment subsystem which are sequentially communicated, wherein the pretreatment subsystem comprises a grid, an oil separation tank, a regulating tank and an ultrasonic air stripping tank which are sequentially communicated; the biochemical treatment subsystem comprises a composite anaerobic fluidized bed reactor (UBF) and a composite membrane bioreactor (HMBR) which are communicated in sequence, the advanced treatment subsystem comprises an electrocatalytic oxidation device and a sand filter tank which are communicated in sequence, and the membrane treatment subsystem comprises a disc tube type reverse osmosis membrane (DTRO) processor.
The composite anaerobic fluidized bed reactor comprises a shell 1, and a granular sludge layer 2, a floc sludge layer 3 and a filter material layer 4 which are arranged in the shell, wherein the granular sludge layer 2, the floc sludge layer 3 and the filter material layer 4 are arranged from bottom to top; the filter bed 4 is arranged in the upper part of the housing at the volume 1/3. The composite anaerobic fluidized bed reactor has sludge bed comprising high concentration granular sludge below it, Mixed Liquid Suspended Solid (MLSS) in the concentration up to several ten g/L, and filtering material layer comprising stuffing and biomembrane on the top. The waste water enters from the bottom of the composite anaerobic fluidized bed reactor, after anaerobic treatment reaction is carried out sequentially through a granular sludge layer and a floc sludge layer, the water from the sludge layer enters a filter material layer, gas-liquid-solid separation is carried out, the water is discharged from the top of the filter material layer, and the gas is conveyed out and then is stored or directly used.
The composite membrane bioreactor comprises an anoxic zone 5, an aerobic zone 6, a settling zone 7 and an intermediate water tank 8 which are communicated in sequence, wherein a partition plate 9 is arranged between the anoxic zone 5 and the aerobic zone 6, and a hollow fiber membrane component 10 is arranged in the intermediate water tank 8. The biological reaction zone of the composite membrane bioreactor is divided into an anoxic zone and an aerobic zone by a partition plate, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition plate, and the mixed liquor in the aerobic zone flows back to the anoxic zone by an aeration device; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters the middle tank, and a hollow fiber membrane component is arranged in the middle tank and used for pumping and draining water.
The anoxic zone 5 is internally provided with a first combined filler 11, and the aerobic zone 6 is internally provided with a second combined filler 12. The two areas are both provided with the combined filler, so that the impact load resistance of a treatment system can be improved, the concentration of activated sludge in the reactor can be reduced, and the membrane pollution amount can be delayed on the basis of maintaining the membrane flux. The distance between the anode and the cathode in the electrocatalytic oxidation device is 2-6 mm.
Example 2
Referring to fig. 2-4, the system for treating the landfill leachate comprises a pretreatment subsystem, a biochemical treatment subsystem, an advanced treatment subsystem and a membrane treatment subsystem which are sequentially communicated, wherein the pretreatment subsystem comprises a grid, an oil separation tank, a regulating tank and an ultrasonic air stripping and floating tank which are sequentially communicated; the biochemical treatment subsystem comprises a composite anaerobic fluidized bed reactor (UBF) and a composite membrane bioreactor (HMBR) which are communicated in sequence, the advanced treatment subsystem comprises an electrocatalytic oxidation device and a sand filter tank which are communicated in sequence, and the membrane treatment subsystem comprises a disc tube type reverse osmosis membrane (DTRO) processor.
The ultrasonic air stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor are respectively communicated with a sludge concentration tank, and the sludge concentration tank is communicated with the membrane filter press. Discharging sludge generated by the ultrasonic air-stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, and transporting the dewatered dry sludge to the outside for final treatment.
The composite membrane bioreactor is communicated with the composite anaerobic fluidized bed reactor through a sludge backflow device, so that the sludge backflow is realized.
The composite anaerobic fluidized bed reactor comprises a shell 1, and a granular sludge layer 2, a floc sludge layer 3 and a filter material layer 4 which are arranged in the shell, wherein the granular sludge layer 2, the floc sludge layer 3 and the filter material layer 4 are arranged from bottom to top; the filter bed 4 is arranged in the upper part of the housing at the volume 1/3. The composite anaerobic fluidized bed reactor has sludge bed comprising high concentration granular sludge below it, Mixed Liquid Suspended Solid (MLSS) in the concentration up to several ten g/L, and filtering material layer comprising stuffing and biomembrane on the top. The waste water enters from the bottom of the composite anaerobic fluidized bed reactor, after anaerobic treatment reaction is carried out sequentially through a granular sludge layer and a floc sludge layer, the water from the sludge layer enters a filter material layer, gas-liquid-solid separation is carried out, the water is discharged from the top of the filter material layer, and the gas is conveyed out and then is stored or directly used.
The composite membrane bioreactor comprises an anoxic zone 5, an aerobic zone 6, a settling zone 7 and an intermediate water tank 8 which are communicated in sequence, wherein a partition plate 9 is arranged between the anoxic zone 5 and the aerobic zone 6, and a hollow fiber membrane component 10 is arranged in the intermediate water tank 8. The biological reaction zone of the composite membrane bioreactor is divided into an anoxic zone and an aerobic zone by a partition plate, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition plate, and the mixed liquor in the aerobic zone flows back to the anoxic zone by an aeration device; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters the middle tank, and a hollow fiber membrane component is arranged in the middle tank and used for pumping and draining water.
The anoxic zone 5 is internally provided with a first combined filler 11, and the aerobic zone 6 is internally provided with a second combined filler 12. The two areas are both provided with the combined filler, so that the impact load resistance of a treatment system can be improved, the concentration of activated sludge in the reactor can be reduced, and the membrane pollution amount can be delayed on the basis of maintaining the membrane flux. The distance between the anode and the cathode in the electrocatalytic oxidation device is 2-6 mm.
Example 3
Is used for treating percolate of certain refuse landfill
Water quality of inlet water: CODcr＝80000mg/l，BOD5＝9000mg/l，SS＝3000mg/l，NH3-N＝4000mg/l，TP＝2000mg/l, color 6000;
the treatment method of the landfill leachate comprises the following steps:
(1) the garbage percolate sequentially enters a grid, an oil separation tank and an adjusting tank, floating slag is removed by the grid, floating oil is removed by the oil separation tank, water quantity and water quality are uniform by the adjusting tank, and solid particles are prevented from settling and being cooled;
(2) the wastewater enters an ultrasonic air-stripping tank from a regulating tank, and a demulsifier is added to separate emulsified oil from a water phase so as to remove most suspended matters and colloidal particles;
the demulsifier is ferric chloride, and the addition amount is 0.5 g/L;
(3) the effluent of the air floatation tank enters an oxidation tank, and an oxidant is added to degrade the wastewater and improve the biodegradability;
the oxidant is potassium ferrate, the adding amount is 55mg/l, the retention time is 1.5h, and the pH value is 7-9;
(4) the effluent of the oxidation tank enters UBF, the wastewater enters from the bottom of the reactor, and after anaerobic treatment reaction sequentially through a granular sludge layer and a floc sludge layer, the water from the sludge layer enters a filter material layer, is subjected to gas-liquid-solid separation, and is discharged from the top of the filter material layer; controlling the pH value of the wastewater at 6.5-8, controlling the water temperature to be +/-30 ℃, and controlling the water power retention time of UBF to be 30 h;
(5) the water from the UBF tank enters HMBR, and the composite membrane bioreactor comprises an anoxic zone, an aerobic zone, a settling zone and an intermediate water tank; the hydraulic retention time of the UBF is 22 h;
the biological reaction zone of the composite membrane bioreactor is divided into an anoxic zone and an aerobic zone by a partition board, the two zones are both filled with combined fillers, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition board, and the mixed liquor in the aerobic zone can flow back to the anoxic zone by an aeration device, so that the smooth proceeding of denitrification is facilitated, and the removal rate of total nitrogen is improved; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters an intermediate water tank, and a hollow fiber membrane component is arranged in the intermediate water tank and used for pumping and draining water;
the HMBR can improve the impact load resistance of a treatment system, reduce the concentration of activated sludge in a reactor and delay the membrane pollution amount on the basis of maintaining membrane flux by adding the filler in the bioreactor;
(6) the HMBR effluent enters an electrocatalytic oxidation device, the direct distance between the anode and cathode plates in the electrocatalytic oxidation device is 4mm, the voltage of the anode and cathode plates is 15V, the hydraulic retention time is 1.5h, and the power supply current is constant at 110A;
(7) the water discharged from the electrocatalytic oxidation device enters a sand filter tank for further decontaminating sludge and suspended matters;
(8) the effluent of the sand filtration tank enters DTRO, and the effluent is discharged after reaching the standard or reclaimed water is recycled;
the reverse osmosis membrane used by the disc tube type reverse osmosis membrane (DTRO) processor is a membrane for seawater desalination, the operating pressure is 55bar, the temperature is 25 ℃, and the system recovery rate is 50-93%;
(9) discharging sludge generated by the ultrasonic air stripping flotation tank, the UBF and the HMBR reactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, transporting the dewatered sludge for final treatment, and refluxing the sewage to a regulating tank.
And (3) effluent quality: the wastewater after treatment reaches GB16889-2008 discharge standard, CODcr＝40mg/l，BOD5＝10mg/l，SS＝5mg/l，NH3-N-3 mg/l, TP-1 mg/l, color-10, pH 7.2.
Example 4
Is used for treating percolate of certain refuse landfill
Water quality of inlet water: CODcr＝80000mg/l，BOD5＝9000mg/l，SS＝3000mg/l，NH3-N4000 mg/l, TP 2000mg/l, color 6000;
the treatment method of the landfill leachate comprises the following steps:
(1) the garbage percolate sequentially enters a grid, an oil separation tank and an adjusting tank, floating slag is removed by the grid, floating oil is removed by the oil separation tank, water quantity and water quality are uniform by the adjusting tank, and solid particles are prevented from settling and being cooled;
(2) the wastewater enters an ultrasonic air-stripping tank from a regulating tank, and a demulsifier is added to separate emulsified oil from a water phase so as to remove most suspended matters and colloidal particles;
the demulsifier is polyaluminium chloride, and the addition amount is 0.2 g/L;
(3) the effluent of the air floatation tank enters an oxidation tank, and an oxidant is added to degrade the wastewater and improve the biodegradability;
the oxidant is potassium ferrate, the addition amount is 10mg/l, the retention time is 1.0h, and the pH value is 7-9;
(4) the effluent of the oxidation tank enters UBF, the wastewater enters from the bottom of the reactor, and after anaerobic treatment reaction sequentially through a granular sludge layer and a floc sludge layer, the water from the sludge layer enters a filter material layer, is subjected to gas-liquid-solid separation, and is discharged from the top of the filter material layer; controlling the pH value of the wastewater at 6.5-8, controlling the water temperature to be +/-30 ℃, and controlling the water retention time of UBF to be 20 h;
(5) the water from the UBF tank enters HMBR, and the composite membrane bioreactor comprises an anoxic zone, an aerobic zone, a settling zone and an intermediate water tank; the hydraulic retention time of the UBF is 15 h;
the biological reaction zone of the composite membrane bioreactor is divided into an anoxic zone and an aerobic zone by a partition board, the two zones are both filled with combined fillers, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition board, and the mixed liquor in the aerobic zone can flow back to the anoxic zone by an aeration device, so that the smooth proceeding of denitrification is facilitated, and the removal rate of total nitrogen is improved; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters an intermediate water tank, and a hollow fiber membrane component is arranged in the intermediate water tank and used for pumping and draining water;
(6) the HMBR effluent enters an electrocatalytic oxidation device, the direct distance between the anode and cathode plates in the electrocatalytic oxidation device is 2mm, the voltage of the anode and cathode plates is 10V, the hydraulic retention time is 0.8h, and the power supply current is constant and is 50A;
(7) the water discharged from the electrocatalytic oxidation device enters a sand filter tank for further decontaminating sludge and suspended matters;
(8) the effluent of the sand filtration tank enters DTRO, and the effluent is discharged after reaching the standard or reclaimed water is recycled;
the reverse osmosis membrane used by the disc tube type reverse osmosis membrane (DTRO) processor is a membrane for seawater desalination, the operating pressure is 30bar, the temperature is 15 ℃, and the system recovery rate is 50-93%;
(9) discharging sludge generated by the ultrasonic air stripping flotation tank, the UBF and the HMBR reactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, transporting the dewatered sludge for final treatment, and refluxing the sewage to a regulating tank.
And (3) effluent quality: the wastewater after treatment reaches GB16889-2008 discharge standard, CODcr＝80mg/l，BOD5＝20mg/l，SS＝15mg/l，NH3-N-10 mg/l, TP-2 mg/l, color-20, pH 7.5.
Example 5
Is used for treating percolate of certain refuse landfill
Water quality of inlet water: CODcr＝80000mg/l，BOD5＝9000mg/l，SS＝3000mg/l，NH3-N4000 mg/l, TP 2000mg/l, color 6000;
the treatment method of the landfill leachate comprises the following steps:
(1) the garbage percolate sequentially enters a grid, an oil separation tank and an adjusting tank, floating slag is removed by the grid, floating oil is removed by the oil separation tank, water quantity and water quality are uniform by the adjusting tank, and solid particles are prevented from settling and being cooled;
(2) the wastewater enters an ultrasonic air-stripping tank from a regulating tank, and a demulsifier is added to separate emulsified oil from a water phase so as to remove most suspended matters and colloidal particles;
the demulsifier is polyaluminium chloride, and the addition amount is 0.2 g/L;
(3) the effluent of the air floatation tank enters an oxidation tank, and an oxidant is added to degrade the wastewater and improve the biodegradability;
the oxidant is potassium ferrate, the addition amount is 10mg/l, the retention time is 1.0h, and the pH value is 7-9;
(4) the effluent of the oxidation tank enters UBF, the wastewater enters from the bottom of the reactor, and after anaerobic treatment reaction sequentially through a granular sludge layer and a floc sludge layer, the water from the sludge layer enters a filter material layer, is subjected to gas-liquid-solid separation, and is discharged from the top of the filter material layer; controlling the pH value of the wastewater at 6.5-8, controlling the water temperature to be +/-30 ℃, and controlling the water retention time of UBF to be 20 h;
(5) the water from the UBF tank enters HMBR, and the composite membrane bioreactor comprises an anoxic zone, an aerobic zone, a settling zone and an intermediate water tank; the hydraulic retention time of the UBF is 15 h;
the biological reaction zone of the composite membrane bioreactor is divided into an anoxic zone and an aerobic zone by a partition board, the two zones are both filled with combined fillers, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition board, and the mixed liquor in the aerobic zone can flow back to the anoxic zone by an aeration device, so that the smooth proceeding of denitrification is facilitated, and the removal rate of total nitrogen is improved; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters an intermediate water tank, and a hollow fiber membrane component is arranged in the intermediate water tank and used for pumping and draining water;
(6) the HMBR effluent enters an electrocatalytic oxidation device, the direct distance between the anode and cathode plates in the electrocatalytic oxidation device is 2mm, the voltage of the anode and cathode plates is 10V, the hydraulic retention time is 0.8h, and the power supply current is constant and is 50A;
(7) the water discharged from the electrocatalytic oxidation device enters a sand filter tank for further decontaminating sludge and suspended matters;
(8) the effluent of the sand filtration tank enters DTRO, and the effluent is discharged after reaching the standard or reclaimed water is recycled;
the reverse osmosis membrane used by the disc tube type reverse osmosis membrane (DTRO) processor is a membrane for seawater desalination, the operating pressure is 30bar, the temperature is 15 ℃, and the system recovery rate is 50-93%;
(9) discharging sludge generated by the ultrasonic air stripping flotation tank, the UBF and the HMBR reactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, transporting the dewatered sludge for final treatment, and refluxing the sewage to a regulating tank.
And (3) effluent quality: the wastewater after treatment reaches GB16889-2008 discharge standard, CODcr＝80mg/l，BOD5＝20mg/l，SS＝15mg/l，NH3-N-10 mg/l, TP-2 mg/l, color-20, pH 7.5.
Example 6
Is used for treating percolate of certain refuse landfill
Water quality of inlet water: CODcr＝80000mg/l，BOD5＝9000mg/l，SS＝3000mg/l，NH3-N4000 mg/l, TP 2000mg/l, color 6000;
the treatment method of the landfill leachate comprises the following steps:
(1) the garbage percolate sequentially enters a grid, an oil separation tank and an adjusting tank, floating slag is removed by the grid, floating oil is removed by the oil separation tank, water quantity and water quality are uniform by the adjusting tank, and solid particles are prevented from settling and being cooled;
(2) the wastewater enters an ultrasonic air-stripping tank from a regulating tank, and a demulsifier is added to separate emulsified oil from a water phase so as to remove most suspended matters and colloidal particles;
the demulsifier is ferrous sulfate, and the addition amount is 1.0 g/L;
(3) the effluent of the air floatation tank enters an oxidation tank, and an oxidant is added to degrade the wastewater and improve the biodegradability;
the oxidant is potassium ferrate, the addition amount is 100mg/l, the retention time is 2.0h, and the pH value is 7-9;
(4) the effluent of the oxidation tank enters UBF, the wastewater enters from the bottom of the reactor, and after anaerobic treatment reaction sequentially through a granular sludge layer and a floc sludge layer, the water from the sludge layer enters a filter material layer, is subjected to gas-liquid-solid separation, and is discharged from the top of the filter material layer; controlling the pH value of the wastewater at 6.5-8, controlling the water temperature to be +/-30 ℃, and controlling the water retention time of UBF to be 40 h;
(5) the water from the UBF tank enters HMBR, and the composite membrane bioreactor comprises an anoxic zone, an aerobic zone, a settling zone and an intermediate water tank; the hydraulic retention time of the UBF is 30 h;
the biological reaction zone of the composite membrane bioreactor is divided into an anoxic zone and an aerobic zone by a partition board, the two zones are both filled with combined fillers, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition board, and the mixed liquor in the aerobic zone can flow back to the anoxic zone by an aeration device, so that the smooth proceeding of denitrification is facilitated, and the removal rate of total nitrogen is improved; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters an intermediate water tank, and a hollow fiber membrane component is arranged in the intermediate water tank and used for pumping and draining water;
(6) the HMBR effluent enters an electrocatalytic oxidation device, the direct distance between the anode and cathode plates in the electrocatalytic oxidation device is 6mm, the voltage of the anode and cathode plates is 20V, the hydraulic retention time is 2h, and the power supply current is constant at 150A;
(7) the water discharged from the electrocatalytic oxidation device enters a sand filter tank for further decontaminating sludge and suspended matters;
(8) the effluent of the sand filtration tank enters DTRO, and the effluent is discharged after reaching the standard or reclaimed water is recycled;
the reverse osmosis membrane used by the disc tube type reverse osmosis membrane (DTRO) processor is a membrane for seawater desalination, the operating pressure is 60bar, the temperature is 40 ℃, and the system recovery rate is 50-93%;
(9) discharging sludge generated by the ultrasonic air stripping flotation tank, the UBF and the HMBR reactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, transporting the dewatered sludge for final treatment, and refluxing the sewage to a regulating tank.
And (3) effluent quality: the wastewater after treatment reaches GB16889-2008 discharge standard, CODcr＝50mg/l，BOD5＝15mg/l，SS＝10mg/l，NH36mg/l of-N, 1.5mg/l of TP, 10 in color, pH 7.3.
Example 7
For treating leachate of certain kitchen waste
Water quality of inlet water: 60000mg/l COD, BOD5＝14000mg/l，NH3-N1500 mg/l, SS 5000mg/l, color 5000;
referring to example 1, effluent quality: the wastewater after treatment reaches the primary standard of GB8978-1996 integrated wastewater discharge Standard, the COD is 50mg/l, and the BOD5＝10mg/l，NH3-N-5 mg/l, SS-30 mg/l, color-10, pH 7.4.
Example 8
Treatment of percolate from certain domestic refuse landfill
Water quality of inlet water: CODcr＝35000mg/l，BOD5＝8000mg/l，NH3-N1200 mg/l, SS 2500mg/l, color 4000;
referring to example 1, effluent quality: the treated wastewater reaches the water reuse standards of GB16889-2008 table 2 and GB/T18920-2002, CODcr＝20mg/l，BOD＝3mg/l，NH3-N-4 mg/l, SS-6 mg/l, color-8, pH 7.2.

Claims (10)

1. The utility model provides a landfill leachate's processing system which characterized in that: the system comprises a pretreatment subsystem, a biochemical treatment subsystem, an advanced treatment subsystem and a membrane treatment subsystem which are sequentially communicated, wherein the pretreatment subsystem comprises a grid, an oil separation tank, a regulating tank and an ultrasonic air stripping tank which are sequentially communicated; the biochemical treatment subsystem comprises a composite anaerobic fluidized bed reactor and a composite membrane bioreactor which are communicated in sequence, the advanced treatment subsystem comprises an electrocatalytic oxidation device and a sand filter tank which are communicated in sequence, and the membrane treatment subsystem comprises a disc tube type reverse osmosis membrane processor.
2. The landfill leachate treatment system of claim 1, wherein: the ultrasonic air stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor are respectively communicated with a sludge concentration tank, and the sludge concentration tank is communicated with the membrane filter press.
3. A method for treating landfill leachate is characterized by comprising the following steps:
(1) the garbage percolate sequentially enters a grid, an oil separation tank and an adjusting tank;
(2) the wastewater enters an ultrasonic air-stripping flotation tank from a regulating tank, and a demulsifier is added;
(3) the effluent of the air floatation tank enters an oxidation tank, and an oxidant is added;
(4) the effluent of the oxidation pond enters a composite anaerobic fluidized bed reactor;
(5) the water discharged from the composite anaerobic fluidized bed reactor enters a composite membrane bioreactor;
(6) the effluent of the composite membrane bioreactor enters an electrocatalytic oxidation device;
(7) the effluent of the electrocatalytic oxidation device enters a sand filter tank;
(8) the outlet water of the sand filter tank enters a disc tube type reverse osmosis membrane processor, and the outlet water reaches the standard and is discharged or reclaimed water is recycled;
(9) discharging sludge generated by the ultrasonic air-stripping flotation tank, the composite anaerobic fluidized bed reactor and the composite membrane bioreactor into a sludge concentration tank, dewatering the sludge treated by the sludge concentration tank in a membrane filter press, transporting the dewatered sludge out for final treatment, and refluxing the sewage to the regulating tank.
4. The method for treating landfill leachate according to claim 3, wherein the method comprises the following steps: the demulsifier in the step (2) is one of ferric chloride, calcium chloride, ferrous sulfate, aluminum sulfate and polyaluminium chloride, and the addition amount is 0.1-1.0 g/L.
5. The method for treating landfill leachate according to claim 3, wherein the method comprises the following steps: in the step (3), the oxidant is potassium ferrate, the addition amount is 5-100 mg/l, the retention time is 0.5-2 h, and the pH value is 7-9.
6. The method for treating landfill leachate according to claim 3, wherein the method comprises the following steps: the pH value of the composite anaerobic fluidized bed reactor is controlled to be 6.5-8, the water temperature is +/-30 ℃, and the hydraulic retention time is 18-40 h.
7. The method for treating landfill leachate according to claim 3, wherein the step (4) is specifically: wastewater enters from the bottom of the composite anaerobic fluidized bed reactor, sequentially passes through a granular sludge layer and a floc sludge layer to carry out anaerobic treatment reaction, and then water from the sludge layer enters a filter material layer to carry out gas-liquid-solid separation and is discharged from the top of the filter material layer; the hydraulic retention time of the composite anaerobic fluidized bed reactor is 12-32 h.
8. The method for treating landfill leachate according to claim 3, wherein the step (5) is specifically: the composite membrane bioreactor comprises an anoxic zone, an aerobic zone, a precipitation zone and an intermediate water tank, wherein the biological reaction zone of the composite membrane bioreactor is divided into the anoxic zone and the aerobic zone by a partition board, both the anoxic zone and the aerobic zone are filled with composite fillers, the mixed liquor in the anoxic zone enters the aerobic zone from the lower part of the partition board, and the mixed liquor in the aerobic zone returns to the anoxic zone by an aeration device; the aerobic zone is connected with the sedimentation zone through the bottom of the tank, the sedimentation effluent enters the middle tank, and a hollow fiber membrane component is arranged in the middle tank and used for pumping and draining water.
9. The method for treating landfill leachate according to claim 3, wherein the method comprises the following steps: in the step (6), the direct distance between the anode and the cathode plate in the electrocatalytic oxidation device is 2-6 mm, the voltage of the anode and the cathode plate is 10-20V, the hydraulic retention time is 0.3-2 h, and the power supply current is constant and is 10-200A.
10. The method for treating landfill leachate according to claim 3, wherein the method comprises the following steps: the reverse osmosis membrane used by the disc-tube reverse osmosis membrane processor in the step (8) is a membrane for seawater desalination, the operating pressure is 30-70 bar, the temperature is 0-40 ℃, and the system recovery rate is 50-93%.
CN202010209535.5A 2020-03-23 2020-03-23 Treatment system and method for landfill leachate Pending CN111253016A (en)

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112811717A (en) * 2020-12-29 2021-05-18 水清华(天津)环保科技有限公司 Landfill leachate treatment process
CN112960842A (en) * 2021-02-08 2021-06-15 四川环科美能环保科技有限公司 Treatment method of hazardous waste incineration wastewater
CN113415956A (en) * 2021-07-30 2021-09-21 广州市天瑞环保科技有限公司 Sewage treatment system for biological maintenance
CN114105377A (en) * 2021-10-25 2022-03-01 苏州镐丰环境科技有限公司 Landfill leachate treatment system and process
CN114956475A (en) * 2022-06-16 2022-08-30 杭州碟滤膜技术有限公司 Landfill leachate treatment system and method

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112811717A (en) * 2020-12-29 2021-05-18 水清华(天津)环保科技有限公司 Landfill leachate treatment process
CN112960842A (en) * 2021-02-08 2021-06-15 四川环科美能环保科技有限公司 Treatment method of hazardous waste incineration wastewater
CN113415956A (en) * 2021-07-30 2021-09-21 广州市天瑞环保科技有限公司 Sewage treatment system for biological maintenance
CN114105377A (en) * 2021-10-25 2022-03-01 苏州镐丰环境科技有限公司 Landfill leachate treatment system and process
CN114956475A (en) * 2022-06-16 2022-08-30 杭州碟滤膜技术有限公司 Landfill leachate treatment system and method
CN114956475B (en) * 2022-06-16 2023-12-08 杭州碟滤膜技术有限公司 Landfill leachate treatment system and method

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