CN209143952U - A kind of processing unit of aged refuse in MSW landfill percolate - Google Patents
A kind of processing unit of aged refuse in MSW landfill percolate Download PDFInfo
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- CN209143952U CN209143952U CN201821547979.4U CN201821547979U CN209143952U CN 209143952 U CN209143952 U CN 209143952U CN 201821547979 U CN201821547979 U CN 201821547979U CN 209143952 U CN209143952 U CN 209143952U
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Abstract
The utility model provides a kind of processing unit of aged refuse in MSW landfill percolate, belongs to water treatment field.Tthe utility model system nitrate recirculation ratio example is higher, has stronger anti impulsion load ability；It is not required to additional carbon, the preferential organic matter using in garbage filter carries out pre-denitrification and denitrogenation, and electrocatalytic oxidation denitrogenation is as supplement and checks on, it is ensured that system nitrogen removal rate meets discharge standard；Electrocatalytic oxidation removes total nitrogen, and total nitrogen removal cost, which is lower than, adds carbon source method denitrogenation；System does not have dope with high salt to generate, and is not required to investment and the high dope processing equipment with high salt of operating cost；Select the screening system low to ion rejection rate, the high-concentration waste water and low concentration wastewater screened out carries out Electrocatalytic oxidation respectively, system salt content is controllable, inorganic salts are avoided to build up the treatment effeciency for influencing biochemical treatment, it is suitable for industrial applications, discharge outlet is discharged quality and is better than " household refuse landfill sites contamination control standard " (GB 16889-2008).
Description
Technical field
The utility model relates to technical field of sewage, and in particular to a kind of aged refuse in MSW landfill percolate
Processing unit.
Background technique
It during consumer waste filling and embedding and closes in considerably long one period later, it will generate organic containing high concentration
The landfill leachate of object, ammonia nitrogen and heavy metal, landfill leachate have complicated component and lower biodegradability, lead to rubbish
Rubbish percolate processing difficulty is big, complex treatment process, investment construction is at high cost, operating cost is higher.
At present garbage leachate treatment process mainly use biochemical treatment, UF membrane, high-level oxidation technology with and combinations thereof
Technique.Biochemical treatment mainly has anaerobism, aerobic treatment process combination；Membrane separation technique has micro-filtration, ultrafiltration, nanofiltration and reverse osmosis place
Reason technology, advanced oxidation processes have chemical oxidization method, ultraviolet/Catalyzed by Ultrasonic Wave oxidizing process, electrochemical oxidation process etc..At present application compared with
Mostly more mature treatment process is biochemical treatment+UF membrane, in recent years using the small-scale of simple membrane separation process such as DTRO
Landfill leachate treatment case is also more and more.The reverse osmosis landfill leachate treatment station of all designs all has a problem that:
The concentrate processing difficulty with high salt of reverse osmosis generation is big.Generally using advanced oxidation and evaporation and concentration processing counter-infiltration dope, deposit
In the drawback that investment cost is high, processing cost is big.
In order to avoid the generation of dope with high salt, sight is turned to high-level oxidation technology by wastewater processing technology personnel, using height
The patent and document of grade oxidation technology processing landfill leachate are also more and more, but the Engineering Projects of mature application is rarely reported.
Chemical oxidization method such as the methods of Fenton method, Fenton-like method, potassium ferrate oxidation, have and add reagent cost height, reacted
Process control control requires the disadvantages of high, sludge yield is big；Ultrasonic wave/ultraviolet light auxiliary catalysis oxidizing process has cost of equipment maintenance
It is high, require water quality treatment and reaction condition high, treatment effect the drawbacks such as to be not sufficiently stable；Electrocatalytic oxidation technique oxidation efficiency
Height, effect are good, and secondary pollution is small, have more wide prospect for landfill leachate treatment.Electro-catalytic oxidation technology at present
It is mainly used for the pretreatment of landfill leachate biochemistry, middle section processing or simple end-o f-pipe -control, ton charges for water and electricity and is up to tens of degree, ton
Water invests nearly ten thousand yuan, it is difficult to large-scale engineering application.
Utility model content
The purpose of this utility model is to provide a kind of processing units of aged refuse in MSW landfill percolate.This is practical
The processing unit of the landfill leachate of novel offer reduces processing system without dope discharge, the discharge without secondary sludge, power consumption,
It is suitable for industrial applications.
In order to realize above-mentioned purpose of utility model, the utility model the following technical schemes are provided:
The utility model provides a kind of processing unit of aged refuse in MSW landfill percolate, including
Grid/grid (1) with percolate import；
The collecting pit (2) being connected to the water outlet of the grid/grid (1)；
The level-one anoxic pond (3) being connected to the water outlet of the collecting pit (2)；
The aerobic tank (4) being connected to the water outlet of the level-one anoxic pond (3)；
The second level anoxic pond (5) being connected to the water outlet of the aerobic tank (4)；
The first MBR system being connected to respectively with the water outlet (5-1) of the second level anoxic pond (5) and bypass outlet (5-2)
(6) connect with mixed liquor reflux pump (8), the outlet of the mixed liquor reflux pump (8) and the water inlet of the level-one anoxic pond (3)
It is logical；
The intermediate pool (9) that is connected to respectively with water outlet, sludge outlet and the sludge reflux mouth of first MBR system (6),
First residual sludge pump (16) and sludge reflux pump (7), the outlet of first residual sludge pump (16) and sludge dewatering system
(18) feed inlet connection, the outlet of the sludge reflux pump (7) is connected to the water inlet of aerobic tank (4)；
The screening system (10) being connected to the water outlet of the intermediate pool (9)；
The small molecule electro-catalysis being connected to respectively with the small molecule water outlet of the screening system (10) and macromolecular water outlet
Oxidation unit (11) and macromolecular electrocatalysis oxidation apparatus (12), what is be arranged in the macromolecular electrocatalysis oxidation apparatus (12) is pre-
Oxidation exit port and exhaustive oxidation outlet are connected to the water inlet of second MBR system (13) and level-one anoxic pond (3) respectively；
The second residual sludge pump (17) for being connected to respectively with the sludge outlet of second MBR system (13) and water outlet and
The outlet of sterilization pool (14), second residual sludge pump (17) is connected to sludge dewatering system (18)；
The water outlet of the small molecule electrocatalysis oxidation apparatus (11) is connected to the water inlet of the sterilization pool (14)；
The discharge outlet (15) being connected to the water outlet of the sterilization pool (14).
Preferably, it is provided with anaerobic reation pool (19) between the collecting pit (2) and level-one anoxic pond (3), it is described
The water outlet of anaerobic reation pool (19) and the collecting pit (2) is also connected to the water inlet of level-one anoxic pond (3).
Preferably, the MBR film in first MBR system (6) and the second MBR system (13) is hydrophilic modifying polytetrafluoroethyl-ne
Alkene microfiltration membranes, the aperture of the hydrophilic modifying polytetrafluoroethylene (PTFE) microfiltration membranes are 0.08~0.4 μm.
Preferably, the molecular cut off range of the screening system (10) is 500~3500, monovalence zwitterion rejection
Lower than 10~20%.
Preferably, the volumetric ratio of the level-one anoxic pond (3), aerobic tank (4) and second level anoxic pond (5) is 30~45:55
~40:8~10.
Preferably, the cathode of the small molecule electrocatalysis oxidation apparatus (11) uses stainless steel or Ti electrode, and anode uses
Titanium-based catalyst coatings electrode or DSA anode with similar catalysis oxidation organic contamination performance, pole plate distance is 10~30mm.
Preferably, the cathode of the macromolecular electrocatalysis oxidation apparatus (12) uses stainless steel or Ti electrode, and anode uses
Titanium-based catalyst coatings electrode, pole plate distance are 10~50mm.
Preferably, the catalyst coat of the titanium-based catalyst coatings electrode independently uses iridium ruthenium coating, and the iridium ruthenium applies
Layer with a thickness of 8~20 microns.
Preferably, the molecular cut off range of the screening system (10) is 500~3500, monovalence zwitterion rejection
Lower than 10~20%.
The utility model provides a kind of processing unit of aged refuse in MSW landfill percolate, system nitrate recirculation ratio example
It is higher, there is stronger anti impulsion load ability；It is not required to additional carbon, the preferential organic matter using in garbage filter carries out preposition
Denitrification denitrogenation, electrocatalytic oxidation denitrogenation is as supplement and checks on, it is ensured that system nitrogen removal rate meets discharge standard；Electro-catalysis
Oxidation removal total nitrogen, total nitrogen removal cost, which is lower than, adds carbon source method denitrogenation；System does not have dope with high salt to generate, and is not required to invest and transport
The high dope processing equipment with high salt of row expense；Select the screening system low to ion rejection rate, the high-concentration waste water screened out
Electrocatalytic oxidation is carried out respectively with low concentration wastewater, and system salt content is controllable, and avoiding inorganic salts from building up influences biochemical treatment
Treatment effeciency is suitable for industrial applications, and final discharge outlet water outlet quality is better than " household refuse landfill sites contamination control standard "
(GB 16889-2008)。
Detailed description of the invention
Fig. 1 is the processing unit schematic diagram of aged refuse in MSW landfill percolate that embodiment 1 provides, in figure, 1- lattice
Grid/grid, 2- collecting pit, 3- level-one anoxic pond, 4- aerobic tank, 5- second level anoxic pond, the first MBR system of 6-, 7- sludge reflux
Pump, 8- mixed liquor reflux pump, 9- intermediate pool, 10- screening system, 11- small molecule electrocatalysis oxidation apparatus, 12- macromolecular electricity are urged
Change oxidation unit, the second MBR system of 13-, 14- sterilization pool, 15- discharge outlet, 16- residual sludge pump, 17- residual sludge pump, 18-
Sludge dewatering system, 5-1 are water outlet, and 5-2 is bypass outlet；
Fig. 2 is the processing unit schematic diagram of aged refuse in MSW landfill percolate that embodiment 2 provides, in figure, 1- lattice
Grid/grid, 2- collecting pit, 3- level-one anoxic pond, 4- aerobic tank, 5- second level anoxic pond, the first MBR system of 6-, 7- sludge reflux
Pump, 8- mixed liquor reflux pump, 9- intermediate pool, 10- screening system, 11- small molecule electrocatalysis oxidation apparatus, 12- macromolecular electricity are urged
Change oxidation unit, the second MBR system of 13-, 14- sterilization pool, 15- discharge outlet, 16- residual sludge pump, 17- residual sludge pump, 18-
Sludge dewatering system, 19- anaerobic reation pool, 5-1 are water outlet, and 5-2 is bypass outlet.
Specific embodiment
The utility model provides a kind of processing unit of aged refuse in MSW landfill percolate, as shown in Figure 1, including
Grid/grid (1) with percolate import；
The collecting pit (2) being connected to the water outlet of the grid/grid (1)；
The level-one anoxic pond (3) being connected to the water outlet of the collecting pit (2)；
The aerobic tank (4) being connected to the water outlet of the level-one anoxic pond (3)；
The second level anoxic pond (5) being connected to the water outlet of the aerobic tank (4)；
The first MBR system being connected to respectively with the water outlet (5-1) of the second level anoxic pond (5) and bypass outlet (5-2)
(6) connect with mixed liquor reflux pump (8), the outlet of the mixed liquor reflux pump (8) and the water inlet of the level-one anoxic pond (3)
It is logical；
The intermediate pool (9) that is connected to respectively with water outlet, sludge outlet and the sludge reflux mouth of first MBR system (6),
First residual sludge pump (16) and sludge reflux pump (7), the outlet of first residual sludge pump (16) and sludge dewatering system
(18) feed inlet connection, the outlet of the sludge reflux pump (7) is connected to the water inlet of aerobic tank (4)；
The screening system (10) being connected to the water outlet of the intermediate pool (9)；
The small molecule electro-catalysis being connected to respectively with the small molecule water outlet of the screening system (10) and macromolecular water outlet
Oxidation unit (11) and macromolecular electrocatalysis oxidation apparatus (12), what is be arranged in the macromolecular electrocatalysis oxidation apparatus (12) is pre-
Oxidation exit port and exhaustive oxidation outlet are connected to the water inlet of second MBR system (13) and level-one anoxic pond (3) respectively；
The second residual sludge pump (17) for being connected to respectively with the sludge outlet of second MBR system (13) and water outlet and
The outlet of sterilization pool (14), second residual sludge pump (17) is connected to sludge dewatering system (18)；
The water outlet of the small molecule electrocatalysis oxidation apparatus (11) is connected to the water inlet of the sterilization pool (14)；
The discharge outlet (15) being connected to the water outlet of the sterilization pool (14).
In the embodiments of the present invention, it is further preferably provided with and detests between the collecting pit (2) and level-one anoxic pond (3)
Water inlet of the water outlet of oxygen reaction tank (19), the anaerobic reation pool (19) and the collecting pit (2) also with level-one anoxic pond (3)
Mouth connection, as shown in Figure 2.
In the present invention, the MBR film in first MBR system (6) and the second MBR system (13) is preferably hydrophilic
Modified Teflon microfiltration membranes, the aperture of the hydrophilic modifying polytetrafluoroethylene (PTFE) microfiltration membranes are preferably 0.08~0.4 μm.
In the embodiments of the present invention, the screening system (10) uses nanofiltration UF membrane.
In the embodiments of the present invention, the molecular cut off of the screening system (10) ranges preferably from 500~
3500, monovalence zwitterion rejection is preferably shorter than 10~20%.
In the present invention, the cathode of the small molecule electrocatalysis oxidation apparatus (11) preferably uses stainless steel or titanium electricity
Pole, anode preferably use titanium-based catalyst coatings electrode or the DSA anode with similar catalysis oxidation organic contamination performance, pole plate away from
From preferably 10~30mm.
In the present invention, the cathode of the macromolecular electrocatalysis oxidation apparatus (12) preferably uses stainless steel or titanium electricity
Pole, anode preferably use titanium-based catalyst coatings electrode, pole plate distance preferably 10~50mm.
In the present invention, the catalyst coat of the titanium-based catalyst coatings electrode is independently preferably applied using iridium ruthenium
Layer, the thickness of the iridium ruthenium coating is preferably 8~20 microns.
In the embodiments of the present invention, the level-one anoxic pond (3), aerobic tank (4) and second level anoxic pond (5) appearance
Product is than being 30~45:55~40:8~10, and the volume of first MBR system (6) is depending on film group arrangement space needs.
The utility model additionally provides a kind of aged refuse in MSW landfill using device described in above-mentioned technical proposal
Leachate processing method, comprising the following steps:
(1) landfill leachate is entered by percolate import and enters collecting pit after grid/grid (1) is pre-processed
(2), pretreating waste percolate is obtained；
(2) the pretreating waste percolate for obtaining the step (1) successively carries out in level-one anoxic pond (3) preposition anti-
Nitrification carries out Aerobic Process for Treatment in aerobic tank (4) and carries out endogenous denitrification in second level anoxic pond (5), obtains endogenous anti-nitre
Water is dissolved, the endogenous denitrification water part carries out preposition anti-nitre through bypass outlet (5-2) and mixed liquor reflux pump (8) reflux
Change, partially enters the first MBR system (6) through water outlet (5-1) and carry out the first MBR processing, obtain the first MBR water outlet and first
MBR sludge, the first MBR sludge part flows back into row Aerobic Process for Treatment through sludge reflux mouth and sludge reflux pump (7), remaining dirty
Mud enters sludge dewatering system (18) after sludge outlet and the first residual sludge pump (16) and carries out sludge dewatering；
(3) the first MBR water outlet obtained the step (2) enters intermediate pool (9) and enters screening system (10) progress afterwards
Diaphragm screen point, obtains the high-concentration waste water containing larger molecular organics and the low concentration wastewater containing small organic molecule；
(4) high-concentration waste water containing larger molecular organics that the step (3) obtains is entered into macromolecular electrocatalytic oxidation
Makeup sets (12) and carries out macromolecular electrocatalytic oxidation, obtains macromolecular electrocatalytic oxidation waste water, the macromolecular electrocatalytic oxidation
The pre-oxidation waste water of waste water through pre-oxidation outlet return carry out Prepositive denitrification, the macromolecular electrocatalytic oxidation waste water it is thorough
Oxidized waste water enters the second MBR system (13) through exhaustive oxidation outlet and carries out the 2nd MBR processing, obtains the 2nd MBR water outlet and the
Two MBR sludge, it is de- that the 2nd MBR sludge enters sludge dewatering system (18) progress sludge after the second residual sludge pump (17)
Water, the 2nd MBR water outlet enters after sterilization pool (14) carries out disinfection through water outlet discharges through discharge outlet (15)；
The low concentration wastewater containing small organic molecule that the step (3) obtains is entered into the makeup of small molecule electrocatalytic oxidation
It sets (11) and carries out small molecule electrocatalytic oxidation, obtain small molecule electrocatalytic oxidation waste water, the small molecule electrocatalytic oxidation waste water
It is discharged after carrying out disinfection into sterilization pool (14) through discharge outlet (15).
The utility model enters collecting pit after landfill leachate is carried out grid/grid pretreatment, obtains pretreating waste
Percolate.The utility model does not have special restriction to the source of the aged refuse in MSW landfill percolate, using ability
Percolate from garbage filling field known to field technique personnel.
In the present invention, the grid/grid pretreatment can remove the sundries of 2mm or more.
In the present invention, when being further preferably provided with anaerobic reaction between the collecting pit (2) and level-one anoxic pond (3)
When pond (19), the preferred control parameter of anaerobic reation pool: pH value 6.5~7.5,20~25 DEG C of temperature, CODcr volumetric loading
6kg/m3D, upflow velocity 1m/h.
In the present invention, it is preferably 80% that collecting pit (2) water outlet, which enters the ratio of anaerobic reation pool (19), institute
Stating collecting pit (2) water outlet to enter the ratio of level-one anoxic pond (3) is preferably 20%.
After obtaining pretreating waste percolate, the utility model successively carries out the pretreating waste percolate preposition anti-
Nitrification, Aerobic Process for Treatment and endogenous denitrification obtain endogenous denitrification water outlet, before the endogenous denitrification water part reflux carries out
Denitrification is set, is partially handled through the first MBR, the first MBR water outlet and the first MBR sludge are obtained, the first MBR sludge part returns
Stream carries out Aerobic Process for Treatment, and excess sludge carries out sludge dewatering.
In the present invention, the first MBR processing parameter preferably includes: pH value 6.5~8.5, and 20~35 DEG C of temperature,
0.3~0.6kg/m of MLSS concentration 10000~20000mg/L, CODcr volumetric loading3D, 0.06~0.12kg/ of total nitrogen load
m38~12L/m of d, MBR membrane flux2H, MBR membrane cisterna return sludge ratio (R2) are 200~300%.
In the present invention, the reflux ratio (R1) of endogenous denitrification water part reflux be preferably 100~
300%.In the utility model, the endogenous denitrification water part flow back when, using endogenous denitrification be discharged in nitrification liquid
In the carbon source that contains carry out Prepositive denitrification, nitrite nitrogen, nitrate nitrogen are reduced into nitrogen, while partial organic substances are gone
It removes.
In the present invention, the Aerobic Process for Treatment includes carbonization and nitrification, and most of organic matter is removed, while ammonia nitrogen
It is oxidized to nitrite nitrogen and nitrate nitrogen.
The utility model does not have special limit to the concrete mode of the Prepositive denitrification, Aerobic Process for Treatment and endogenous denitrification
It is fixed, using mode well known to those skilled in the art.
After obtaining the first MBR water outlet, the first MBR is discharged and carries out diaphragm screen point by the utility model, obtains containing big point
The high-concentration waste water (F2) of sub- organic matter and low concentration wastewater (F1) containing small organic molecule.
In the present invention, the molecular cut off of the diaphragm screen point ranges preferably from 500~3500, monovalence zwitterion
Rejection is preferably shorter than 10~20%.
After obtaining the high-concentration waste water containing larger molecular organics, the utility model is by described containing larger molecular organics
High-concentration waste water carries out macromolecular electrocatalytic oxidation, obtains macromolecular electrocatalytic oxidation waste water, the macromolecular electrocatalytic oxidation
Wastewater fraction reflux carries out Prepositive denitrification, partially handles through the 2nd MBR, obtains the 2nd MBR water outlet and the 2nd MBR sludge, institute
It states the 2nd MBR sludge and carries out sludge dewatering, the 2nd MBR water outlet is discharged after carrying out disinfection；
After obtaining the low concentration wastewater containing small organic molecule, the utility model is by described containing small organic molecule
Low concentration wastewater carries out small molecule electrocatalytic oxidation, obtains small molecule electrocatalytic oxidation waste water, the small molecule electrocatalytic oxidation
Waste water discharges after carrying out disinfection.
In the present invention, the macromolecular electrocatalytic oxidation is described preferably successively including pre-oxidation and exhaustive oxidation
The time of pre-oxidation is preferably 20~60min, and voltage is preferably 5~9V, and current density is preferably 150~300A/m2；It is described thorough
The time of bottom oxidation is preferably 20~60min, and voltage is preferably 4~6V, and current density is preferably 100~200A/m2。
In the present invention, the macromolecular electrocatalytic oxidation wastewater fraction reflux carries out the reflux ratio of Prepositive denitrification
It (F4) is preferably 20~100%.In the present invention, the macromolecular electrocatalytic oxidation wastewater fraction is handled through the 2nd MBR
Ratio (F3) be preferably 0~80%, when the high-concentration waste water containing larger molecular organics conductivity be lower than 4000 μ s/cm
When, it carries out exhaustive oxidation waste water ratio (F3) and takes low value 0, when the conductivity of the high-concentration waste water containing larger molecular organics is more than
20000 μ s/cm carry out exhaustive oxidation waste water ratio (F3) and take high level 80%.
In the present invention, the 2nd MBR processing parameter preferably includes: pH value 6.5~8.5, and 20~35 DEG C of temperature,
0.2~0.4kg/m of MLSS concentration 6000~15000mg/L, CODcr volumetric loading310~15L/m of d, MBR membrane flux2H,
MBR membrane cisterna return sludge ratio 200~300%, aluminium salt or molysite dosage and water inlet total phosphorus molar ratio 1.3:1.
In the present invention, the small molecule electrocatalytic oxidation preferably successively includes quick oxidation panel and exhaustive oxidation
Section, the time of the quick oxidation panel are preferably 10~20min, and voltage is preferably 5~8V, and current density is preferably 100~
150A/m2；The time of the exhaustive oxidation section is preferably 20~40min, and voltage is preferably 4~6V, and current density is preferably 60
~100A/m2。
The utility model does not have special restriction to the concrete mode of the disinfection and discharge, using those skilled in the art
Well known mode.
Below in conjunction with the embodiments of the present invention, the technical solution in the utility model is carried out clear, complete
Ground description.Obviously, the described embodiments are only a part of the embodiments of the utility model, instead of all the embodiments.Base
In the embodiments of the present invention, institute obtained by those of ordinary skill in the art without making creative efforts
There are other embodiments, fall within the protection scope of the utility model.
Embodiment 1
Certain percolate from garbage filling field (10 ton/days)
Processing unit is as shown in Figure 1:
Amount of inlet water: 10 ton/days；
Landfill leachate influent quality is as shown in table 1.
1 landfill leachate influent quality of table
Processing step is as follows:
Garbage filter flows back into collecting pit (2) by the sundries liquid that grid/grid (1) removes 2mm or more, by above-mentioned step
Suddenly treated, and landfill leachate initially enters level-one anoxic pond (3), the nitrification liquid warp to come with second level anoxic pond (5) reflux
(5-2) carries out Prepositive denitrification using the carbon source in water inlet, subsequently enters aerobic tank (4) and is further carbonized and is nitrified, so
Enter second level anoxic pond (5) afterwards and carry out endogenous denitrification, it is preposition that 200% mixed liquor (R2) flows back into level-one anoxic pond (3) progress
Denitrogenation；The water outlet of second level anoxic pond (5) denitrification enters back into the first MBR system (6) through (5-1) and carries out Aerobic Process for Treatment and solid-liquid point
From 200% sludge (R1) flows back into aerobic tank (4), and about 10% excess sludge is discharged into sludge dewatering through residual sludge pump (16)
System (18) is carried out dehydrating, and the clear water after MBR UF membrane enters intermediate pool (9).The waste water of intermediate pool (9) enters retention point
Son amount is 600, the nanofiltration membrane (10) of sodium chloride rejection 40% sieves the organic matter in water inlet, is obtained containing about 30%
(F2) high-concentration waste water and 70% low concentration wastewater of (F1) containing small organic molecule of the larger molecular organics of left and right.Big point
Sub- high-concentration waste water enter macromolecular electrocatalysis oxidation apparatus carry out segmentation carry out pre-oxidation and exhaustive oxidation.Macromolecular electro-catalysis
Oxidation unit cathode uses stainless steel electrode, and anode uses titanium-based catalyzed oxidation coatings electrode.After pre-oxidation 40min,
80% (F4) waste water returns to level-one anoxic pond (3) and continues with；20% (F3) waste water continues exhaustive oxidation, reacts 40min,
Biological treatment and separation of solid and liquid are carried out subsequently into the second MBR system (13), water outlet is directly discharged into sterilization pool (14)；Contain small point
The low concentration wastewater of sub- organic matter enters small molecule electrocatalysis oxidation apparatus (11) and is aoxidized.Small molecule electrocatalysis oxidation apparatus
(11) cathode uses stainless steel, and anode uses titanium-based catalyst coatings electrode.Exhaustive oxidation is divided into quick oxidation panel and exhaustive oxidation
Section, quick oxidation panel time 20min, exhaustive oxidation section reaction time 20min, water outlet are discharged into sterilization pool (14)；Sterilization pool (14)
In waste water it is sterile-processed after, into discharge outlet (15) direct emission.
Main control parameters:
1) the first MBR control parameter: PH 6.5,20 DEG C of temperature, MLSS concentration 15000mg/L, CODcr volumetric loading
0.33kg/m3D, total nitrogen load 0.066kg/m3D, MBR membrane flux 10L/m2H, MBR membrane cisterna return sludge ratio 300%,
Second level anoxic pond to level-one anoxic pond mixed liquid recycle ratio 200%,
2) level-one anoxic pond, aerobic tank, second level anoxic pond and the first MBR system total measurement (volume) 1500m3, level-one anoxic pond accounts for
33%, aerobic tank accounts for 50%, and second level anoxic pond accounts for 10%, and the first MBR system accounts for 7%.
3) MBR film uses hydrophilic modifying polytetrafluoroethylene (PTFE) microfiltration membranes, 0.1 micron of aperture.
4) screening system uses nanofiltration UF membrane, screening system molecular cut off range 600, monovalent ion rejection 10-
20%.
Macromolecular electrocatalysis oxidation apparatus cathode uses stainless steel, and anode uses titanium-based catalyst coatings electrode, pole plate distance
10mm.Pre-oxidation time 40min, voltage 6V, current density, 300A/m2；Exhaustive oxidation reaction time 40min, voltage
4.2V, current density, 150A/m2。
6) macromolecular electrocatalysis oxidation apparatus pre-oxidizes ratio 80%, and 20% enters exhaustive oxidation.
7) the second MBR system control parameter: PH 6.5,22 DEG C of temperature, MLSS concentration 10000mg/L, CODcr volumetric loading
0.3kg/m3D, MBR membrane flux 15L/m2H, MBR membrane cisterna return sludge ratio 200%, aluminium chloride dosage: aluminium element with into
Water total phosphorus (TP) mole coin 1.3:1.
8) small molecule electrocatalysis oxidation apparatus cathode use stainless steel, anode use titanium-based catalyst coatings electrode, pole plate away from
From 10mm, quick oxidation panel voltage 5.0V, current density 125A/m2, quick oxidation time 20min；Exhaustive oxidation section electricity
Press 4.2V, current density 100A/m2, quick oxidation time 20min.
9) for the ease of comparison: screening system water outlet is directly entered small molecule electrocatalysis oxidation apparatus and is reacted
180min, voltage 4.5V, current density 150A/m2。
10) catalyst coat of titanium-based catalyst coatings electrode used in macromolecular and small molecule electrocatalysis oxidation apparatus uses iridium
Ruthenium coating, 10 microns of coating layer thickness.
Treatment effect:
1) discharge outlet water outlet is measured, the results are shown in Table 2, and as can be seen from Table 2, the water outlet of the present embodiment is better than
The limit value of defined in " household refuse landfill sites contamination control standard " (GB 16889-2008).
2 discharge outlet effluent quality measurement result of table
2) it is not required to additional carbon, total nitrogen may conform to discharge standard.
3) total nitrogen 10.7kg is removed, carbon source method denitrogenation expense is saved: with 58~60% technical grade sodium acetate 181.9kg, taking
With 363.8 yuan.
4) system does not have dope with high salt to generate.
5) screening system low to ion rejection rate is selected, the high-concentration waste water segmentation Electrocatalytic oxidation screened out, 80% is high
Concentration waste water pre-oxidizes circular treatment, the direct qualified discharge of 20% deep oxidation, and system salt content is no more than 4000mg/L.
6) it is not required to add advanced oxidation agent (dangerous material), avoids secondary pollution from generating, be easily managed simultaneously.
7) the first MBR system water outlet direct electrochemistry oxidation, 150A/m2, voltage 4.5V, reaction 3 hours, water outlet CODcr
350mg/L, is not achieved discharge standard, and ton water power consumption reaches 60kwh.
8) according to the hierarchical segmented Electrocatalytic oxidation of difference of pollutant oxidation characteristic, treatment effeciency is improved, and the reaction time shortens.
Small molecule low concentration wastewater by 40min can qualified discharge, ton water power consume 9.5kwh, macromolecular high-concentration waste water pre-oxidation electricity
Consumption consumes 7.6kwh by final draining meter ton water power, and macromolecular exhaustive oxidation power consumption is by final draining meter ton water power consumption
0.8kwh, electrocatalytic oxidation total energy consumption 17.9kwh.
Embodiment 2
Certain percolate from garbage filling field (10 ton/days)
Processing unit is as shown in Figure 2:
Amount of inlet water: 10 ton/days；
Landfill leachate influent quality is as shown in table 3.
3 landfill leachate influent quality of table
Processing step is as follows:
Landfill leachate enters collecting pit (2) after grid/grid (1) removes the sundries of 2mm or more, most of waste water
(F6,80%) carries out anaerobic reaction in anaerobic reation pool (19) to remove most of organic matter, and small part waste water (F5,20%) is straight
It taps into level-one anoxic pond (3), the nitrification liquid that mixed liquor reflux pump (8) reflux comes in second level anoxic pond (5) is using in water inlet
Carbon source carry out Prepositive denitrification, subsequently enter aerobic tank (4) and be further carbonized and nitrified, subsequently into second level anoxic pond
(5) carry out endogenous denitrification, 200% mixed liquor (R2) through sludge reflux pump (7) flow back into level-one anoxic pond (3) carry out it is preposition anti-
Nitrify denitrogenation；The water outlet of second level anoxic pond (5) denitrification enters back into the first MBR system (6) and carries out Aerobic Process for Treatment and separation of solid and liquid,
300% sludge (R1) flows back into aerobic tank (4), and about 15% excess sludge is discharged into sludge dewatering system (18) through sludge pump (16)
It is carried out dehydrating, the clear water after MBR UF membrane enters intermediate pool (9)；The clear water of intermediate pool (9) enters molecular cut off and is
2500, the nanofiltration membrane screening system (10) of sodium chloride rejection 40% sieves the organic matter in water inlet, obtains containing about
The high-concentration waste water (F2) and 70% or so the low concentration wastewater containing small organic molecule of 30% or so larger molecular organics
(F1)；Macromolecular high-concentration waste water enter macromolecular electrocatalysis oxidation apparatus (12) carry out segmentation carry out pre-oxidation and thorough oxygen
Change, macromolecular electrocatalysis oxidation apparatus (12) cathode uses Ti electrode, and anode uses titanium-based catalyzed oxidation coatings electrode.By pre-
After aoxidizing 60min, 50% waste water (F4) returns to level-one anoxic pond and continues with；50% waste water (F3) continues exhaustive oxidation,
60min is reacted, carries out Aerobic Process for Treatment and separation of solid and liquid subsequently into the second MBR system (13), excess sludge is through sludge pump (17)
It is discharged into sludge dewatering system (18) to be handled, water outlet is directly discharged into sterilization pool (14)；Low concentration containing small organic molecule
Waste water enters small molecule electrocatalysis oxidation apparatus (11) and carries out exhaustive oxidation.Small molecule electrocatalysis oxidation apparatus (11) cathode uses
Stainless steel, anode use titanium-based catalyst coatings electrode.Exhaustive oxidation is divided into quick oxidation panel and exhaustive oxidation section, quick oxidation panel
Time 15min, exhaustive oxidation section reaction time 35min, water outlet are discharged into sterilization pool (14)；Sterilization pool (14) waste water is sterile-processed
Enter discharge outlet (15) direct emission afterwards.
Main control parameters:
1) anaerobic reation pool control parameter: pH7.5,25 DEG C of temperature, CODcr volumetric loading 6kg/m3D, upflow velocity
1m/h。
2) the first MBR system parameter: pH 7.5,25 DEG C of temperature, MLSS concentration 15000mg/L, CODcr volumetric loading
0.4kg/m3D, total nitrogen load 0.08kg/m3D, MBR membrane flux 10L/m2H, MBR membrane cisterna return sludge ratio (R1) is
300%, the mixed liquid recycle ratio (R2) of second level anoxic pond (5) to level-one anoxic pond (3) is 200%.
3) level-one anoxic pond, aerobic tank, second level anoxic pond and the first MBR system total measurement (volume) 300m3, level-one anoxic pond (3)
33% is accounted for, aerobic tank (4) accounts for 50%, and second level anoxic pond (5) accounts for 10%, and the first MBR system (6) accounts for 7%.
4) MBR film uses hydrophilic modifying polytetrafluoroethylene (PTFE) microfiltration membranes, 0.1 micron of aperture.
7) screening system (10) uses Ultra filtration membrane, screening system molecular cut off range 3500, monovalent ion retention
Rate is lower than 10-20%.Screening obtains the high-concentration waste water (F2) and 75% or so of the larger molecular organics containing about 25% or so
Include the low concentration wastewater (F1) containing small organic molecule.
5) macromolecular electrocatalysis oxidation apparatus (12) cathode uses stainless steel, and anode uses titanium-based catalyst coatings electrode, pole
Plate distance 30mm.Pre-oxidation time 60min, voltage 6V, current density 250A/m2；Exhaustive oxidation reaction time 60min,
Voltage 5V, current density 150A/m2。
6) it is 50% that macromolecular electrocatalysis oxidation apparatus (12) pre-oxidation, which returns to the waste water ratio (F4) of level-one anoxic pond, into
The waste water ratio (F3) for entering exhaustive oxidation is 50%.
7) the second MBR system (13) control parameter: pH7.5,25 DEG C of temperature, MLSS concentration 15000mg/L, CODcr volume
Load 0.3kg/m3D, MBR membrane flux 15L/m2H, MBR membrane cisterna return sludge ratio 200%, ferric trichloride dosage: iron member
Element and water inlet total phosphorus molar ratio 1.1:1.
8) small molecule electrocatalysis oxidation apparatus (11) cathode uses stainless steel, and anode uses titanium-based catalyst coatings electrode, pole
Plate distance 30mm, quick oxidation panel voltage 5.6V, current density 125A/m2, quick oxidation panel reaction time 15min；Thorough oxygen
Change section voltage 4.5V, current density 80A/m2, exhaustive oxidation section reaction time 35min.
9) catalyst coat of titanium-based catalyst coatings electrode used in macromolecular and small molecule electrocatalysis oxidation apparatus (11,12)
Using ruthenium tin antimony coat, 10 microns of coating layer thickness.
Treatment effect:
1) discharge outlet water outlet is measured, the results are shown in Table 4, and as can be seen from Table 4, the water outlet of the present embodiment is better than
The limit value of defined in " household refuse landfill sites contamination control standard " (GB 16889-2008).
4 discharge outlet effluent quality measurement result of table
2) it is not required to additional carbon, total nitrogen may conform to discharge standard.
3) electrocatalytic oxidation removes total nitrogen 18.74kg, saves carbon source and adds expense: with 58~60% technical grade sodium acetates and
318kg, 636.8 yuan of expense.
4) system does not have dope with high salt to generate.
5) screening system low to ion rejection rate is selected, the high-concentration waste water segmentation Electrocatalytic oxidation screened out, 50% is high
Concentration waste water pre-oxidizes circular treatment, and direct qualified discharge, system contain after the processing of the second MBR system again after 50% deep oxidation
Salt amount is no more than 6000mg/L.
6) it is not required to add advanced oxidation agent (dangerous material), avoids secondary pollution from generating, be easily managed simultaneously.
7) the first MBR system water outlet direct electrochemistry oxidation, 150A/m2, voltage 4.5V, reaction 3 hours, water outlet CODcr
336.8mg/L, is not achieved discharge standard, and ton water power consumption reaches 60kwh.
8) according to the hierarchical segmented Electrocatalytic oxidation of difference of pollutant oxidation characteristic, treatment effeciency is improved, and the reaction time shortens.
Small molecule low concentration wastewater by 50min can qualified discharge, ton water power consume 11.9kwh, macromolecular high-concentration waste water pre-oxidation
Power consumption consumes 8.3kwh by final draining meter ton water power, and macromolecular exhaustive oxidation power consumption is by final draining meter ton water power consumption
2.8kwh, electrocatalytic oxidation total energy consumption 23.0kwh.
The above is only the preferred embodiment of the utility model, it is noted that for the common skill of the art
For art personnel, without departing from the principle of this utility model, several improvements and modifications can also be made, these improve and
Retouching also should be regarded as the protection scope of the utility model.
Claims (7)
1. a kind of processing unit of aged refuse in MSW landfill percolate, which is characterized in that including
Grid/grid (1) with percolate import；
The collecting pit (2) being connected to the water outlet of the grid/grid (1)；
The level-one anoxic pond (3) being connected to the water outlet of the collecting pit (2)；
The aerobic tank (4) being connected to the water outlet of the level-one anoxic pond (3)；
The second level anoxic pond (5) being connected to the water outlet of the aerobic tank (4)；
The first MBR system (6) for being connected to respectively with the water outlet (5-1) of the second level anoxic pond (5) and bypass outlet (5-2) and
Mixed liquor reflux pump (8), the outlet of the mixed liquor reflux pump (8) are connected to the water inlet of the level-one anoxic pond (3)；
The intermediate pool (9) that is connected to respectively with water outlet, sludge outlet and the sludge reflux mouth of first MBR system (6), first
Residual sludge pump (16) and sludge reflux pump (7), the outlet and sludge dewatering system (18) of first residual sludge pump (16)
Feed inlet connection, the outlet of the sludge reflux pump (7) is connected to the water inlet of aerobic tank (4)；
The screening system (10) being connected to the water outlet of the intermediate pool (9)；
The small molecule electrocatalytic oxidation being connected to respectively with the small molecule water outlet of the screening system (10) and macromolecular water outlet
Device (11) and macromolecular electrocatalysis oxidation apparatus (12), the middle pre-oxidation being arranged of the macromolecular electrocatalysis oxidation apparatus (12)
Outlet and exhaustive oxidation outlet are connected to the water inlet of the second MBR system (13) and level-one anoxic pond (3) respectively；
The second residual sludge pump (17) and disinfection being connected to respectively with the sludge outlet of second MBR system (13) and water outlet
The outlet in pond (14), second residual sludge pump (17) is connected to sludge dewatering system (18)；
The water outlet of the small molecule electrocatalysis oxidation apparatus (11) is connected to the water inlet of the sterilization pool (14)；
The discharge outlet (15) being connected to the water outlet of the sterilization pool (14).
2. the apparatus according to claim 1, which is characterized in that be arranged between the collecting pit (2) and level-one anoxic pond (3)
Have anaerobic reation pool (19), the water outlet of the anaerobic reation pool (19) and the collecting pit (2) also with level-one anoxic pond (3)
Water inlet connection.
3. device according to claim 1 or 2, which is characterized in that first MBR system (6) and the second MBR system
(13) the MBR film in is hydrophilic modifying polytetrafluoroethylene (PTFE) microfiltration membranes, and the aperture of the hydrophilic modifying polytetrafluoroethylene (PTFE) microfiltration membranes is only
Stand is 0.08~0.4 μm.
4. the apparatus according to claim 1, which is characterized in that the level-one anoxic pond (3), aerobic tank (4) and second level lack
The volumetric ratio in oxygen pond (5) is 30~45:55~40:8~10.
5. the apparatus according to claim 1, which is characterized in that the cathode of the small molecule electrocatalysis oxidation apparatus (11) is adopted
With stainless steel or Ti electrode, DSA of the anode using titanium-based catalyst coatings electrode or with similar catalysis oxidation organic contamination performance
Anode, pole plate distance are 10~30mm.
6. the apparatus according to claim 1, which is characterized in that the cathode of the macromolecular electrocatalysis oxidation apparatus (12) is adopted
With stainless steel or Ti electrode, anode uses titanium-based catalyst coatings electrode, and pole plate distance is 10~50mm.
7. device according to claim 5 or 6, which is characterized in that the catalyst coat of the titanium-based catalyst coatings electrode
Independently use iridium ruthenium coating, the iridium ruthenium coating with a thickness of 8~20 microns.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821547979.4U CN209143952U (en) | 2018-09-21 | 2018-09-21 | A kind of processing unit of aged refuse in MSW landfill percolate |
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| CN201821547979.4U CN209143952U (en) | 2018-09-21 | 2018-09-21 | A kind of processing unit of aged refuse in MSW landfill percolate |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109081522A (en) * | 2018-09-21 | 2018-12-25 | 南宁市桂润环境工程有限公司 | A kind of processing unit and method of aged refuse in MSW landfill percolate |
| CN110436714A (en) * | 2019-08-26 | 2019-11-12 | 桂润环境科技股份有限公司 | A kind of sulfur-bearing, processing unit and processing method containing ammonia nitrogen landfill leachate |
| CN115196812A (en) * | 2021-04-08 | 2022-10-18 | 富钰精密组件（昆山）有限公司 | Wastewater treatment system and wastewater treatment method |
-
2018
- 2018-09-21 CN CN201821547979.4U patent/CN209143952U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109081522A (en) * | 2018-09-21 | 2018-12-25 | 南宁市桂润环境工程有限公司 | A kind of processing unit and method of aged refuse in MSW landfill percolate |
| CN109081522B (en) * | 2018-09-21 | 2023-09-19 | 桂润环境科技股份有限公司 | Treatment device and method for landfill leachate of household garbage landfill |
| CN110436714A (en) * | 2019-08-26 | 2019-11-12 | 桂润环境科技股份有限公司 | A kind of sulfur-bearing, processing unit and processing method containing ammonia nitrogen landfill leachate |
| CN115196812A (en) * | 2021-04-08 | 2022-10-18 | 富钰精密组件（昆山）有限公司 | Wastewater treatment system and wastewater treatment method |
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