CN115093054A - Harmless treatment method for landfill leachate - Google Patents
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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Abstract
The invention particularly relates to a harmless treatment method of landfill leachate, which comprises the steps of sequentially adding a polymeric ferric sulfate solution and a polyacrylamide solution into the landfill leachate to obtain a coagulated turbid liquid, standing for layering, taking supernatant, and sequentially passing through SiC and Al 2 O 3 Filtering with the ceramic membrane. Through the scheme, the coagulation effluent water of treatment need not through the time of standing frequently, has improved landfill leachate's treatment effeciency, and the antipollution performance of ceramic membrane itself is just stronger, only need can drop into service again after simple physics washs when the filter cake layer is too thick, makes this patent have higher economic benefits, the pollution problem of solution landfill leachate that can high-efficient economy.
Description
Technical Field
The invention belongs to the technical field of garbage treatment, and particularly relates to a garbage leachate harmless treatment method.
Background
The landfill leachate is a blackish brown liquid with high pollutant concentration and pungent smell generated by natural rainfall, microbial degradation of the garbage and the like in the landfill process. The landfill leachate has the water quality characteristics different from those of urban sewage, and the properties of the landfill leachate depend on various factors such as the components of the garbage, the landfill time, the climatic conditions, the design of a landfill site and the like. Generally speaking, the landfill leachate has the characteristics of high concentration of pollutants such as organic matters, ammonia nitrogen, heavy metals and the like, large change of water quality and water quantity and the like. Landfill leachate causes pollution to underground water, surface water and the surrounding environment of a landfill site, causes surface water to be anoxic, water quality to deteriorate and eutrophic, threatens drinking water and industrial water sources, and causes the water quality of the underground water to deteriorate and lose the utilization value. Leachate contains a great deal of toxic substances and has high concentration, which is becoming a great threat to the environment. The leachate is discharged into rivers and lakes without treatment, and the organic pollutants and the inorganic pollutants in the leachate can pollute aquatic organisms and crops, destroy the ecological environment, enter human bodies through food chains and directly threaten the health of human beings. Therefore, proper treatment and utilization of landfill leachate is a problem to be solved urgently.
Compared with the traditional organic membrane, the ceramic membrane has stronger firmness and more superiority, but the garbage leachate contains soluble organic matters, suspended matters, colloids, soluble salts, soluble solids and other pollutants, so that serious pollution to the ceramic membrane is easily caused, and the single ceramic membrane treatment technology has lower removal efficiency on the organic matters.
Disclosure of Invention
The invention aims to provide a harmless treatment method of landfill leachate, which aims to solve the technical problems.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for innocent treatment of landfill leachate, comprising the following steps: sequentially adding a polymeric ferric sulfate solution and a polyacrylamide solution into the landfill leachate to obtain a coagulated turbid liquid, standing for layering, and sequentially passing the supernatant through SiC and Al 2 O 3 Filtering with the ceramic membrane.
The invention can also further comprise the following technical scheme: the method for sequentially adding the polyferric sulfate solution and the polyacrylamide solution into the landfill leachate comprises the following steps:
adding a polyferric sulfate solution into landfill leachate in a high-speed stirring state, stirring until a preset first time length, adding a polyacrylamide solution, stirring until the preset first time length is reached, then switching to low-speed stirring until a preset second time length is reached, wherein the speed of the high-speed stirring is 5 times of the speed of the low-speed stirring, and the preset second time length is 40 times of the preset first time length.
The invention can also further comprise the following technical scheme: the mass fraction of the polymeric ferric sulfate solution is 10%, the mass fraction of the polyacrylamide solution is 1%, the feeding amount of the polymeric ferric sulfate solution corresponding to unit volume of landfill leachate is 7-14g/L, and the feeding amount of the polyacrylamide solution corresponding to unit volume of landfill leachate is 10 mg/L.
The invention can also further comprise the following technical scheme: the optimal feeding amount of the polymeric ferric sulfate solution is 12 g/L.
The invention can also further comprise the following technical scheme: before the polyferric sulfate solution and the polyacrylamide solution are sequentially added into the landfill leachate, the method further comprises the following steps:
and adjusting the pH value of the landfill leachate to a preset pH value range, wherein the preset pH value range is 4-12.
The invention can also further comprise the following technical scheme: the optimal range of the preset pH value is 7-8.
The invention can further comprise the following technical scheme: the effective filtering area of the ceramic membrane of the SiC is 0.03136m 2 The pure water flux is 4669.63L/(m) 2 H) transmembrane pressure difference of 0.065 MPa.
The invention can also further comprise the following technical scheme: the Al is 2 O 3 The effective filtering area of the ceramic membrane is 0.024424m 2 The pure water flux is 924.78L/(m) 2 H) transmembrane pressure difference of 0.09 MPa.
Wherein, the invention can alsoThe technical scheme is as follows: taking supernatant to sequentially pass through SiC and Al 2 O 3 Before the ceramic membrane filtration of (3), the method further comprises: SiC and Al to be assembled 2 O 3 The ceramic membrane is put into pure water for exhausting.
The invention can also further comprise the following technical scheme: taking supernatant to sequentially pass through SiC and Al 2 O 3 After the ceramic membrane filtration of (3), the method further comprises: to be mixed with SiC and Al 2 O 3 When the filter cake of the ceramic membrane reaches the preset thickness, removing the filter cake by a physical cleaning method, and removing the SiC and Al of the filter cake 2 O 3 The ceramic membrane is put into recycling use again.
Has the advantages that:
according to the technical scheme, the treated coagulation effluent does not need to be subjected to complex and long standing time, the treatment efficiency of the garbage leachate is improved, in addition, the pH of the effluent treated by the polymeric ferric sulfate is not greatly changed and is still about neutral, the harm of the coagulation effluent to the ceramic membrane is small, the pollution resistance of the ceramic membrane is strong, and the ceramic membrane can be put into use after being simply physically cleaned when the filter cake layer is too thick, so that the composite filter cake has high economic benefit, and the pollution problem of the garbage leachate can be efficiently and economically solved.
Drawings
FIG. 1 is a schematic diagram showing the change of effluent COD with the addition of a coagulant;
FIG. 2 is a schematic diagram showing the variation of effluent total phosphorus with the addition of a coagulant;
FIG. 3 shows the effluent UV of the present invention 254 Schematic diagram of the change with the addition of coagulant;
FIG. 4 is a schematic diagram showing the change of effluent COD with pH according to the present invention;
FIG. 5 is a schematic diagram showing the variation of total phosphorus in effluent with pH according to the present invention;
FIG. 6 shows the effluent UV of the present invention 254 Schematic as a function of pH;
FIG. 7 is a schematic representation of the flux of a membrane of the present invention as a function of pressure differential across the membrane;
FIG. 8 is a schematic of the flux of the membrane of the present invention as a function of time;
FIG. 9 is a schematic diagram showing the change of COD with filtration time according to the present invention;
FIG. 10 is a schematic representation of total phosphorus as a function of filtration time in accordance with the present invention;
FIG. 11 is a graph showing turbidity as a function of filtration time according to the present invention;
FIG. 12 shows UV light of the present invention 254 Schematic as a function of filtration time;
FIG. 13 is a schematic diagram showing the change of COD removal rate in a continuous membrane test according to the present invention;
FIG. 14 is a graph showing the variation of TP removal rate in a continuous membrane test according to the present invention;
FIG. 15 shows that the present invention is UV 254 The removal rate is shown in a continuous membrane test.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below with reference to specific embodiments, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
The technical conception of the invention is as follows:
the polyferric sulfate (PFS) is an inorganic polymer coagulant with excellent performance, the morphological character is a faint yellow amorphous powdery solid which is very easy to dissolve in water, and a water solution with the mass fraction of 10 percent is a reddish brown transparent solution, so that the polyferric sulfate (PFS) has the advantages of hygroscopicity, excellent coagulation performance, compact alum floc and high settling speed; removing turbidity, decolorizing, deoiling, dewatering, sterilizing, deodorizing, removing algae, and removing COD and BOD from water 5 And the pH change of the effluent after coagulation is small, and the effluent is not easy to corrode equipment. The ceramic micro-filtration membrane is a filtration membrane widely applied in oily wastewater treatment, can not only be subjected to chemical and physical cleaning, but also has high thermal stability, and the surface is not easy to scale and the membrane flux is not easy to decrease. However, landfill leachate contains a large amount of soluble organic mattersSuspended matters, soluble salts and other pollutants easily cause serious membrane pollution, and a single membrane treatment technology has low removal efficiency on organic matters. Although the ceramic membrane separation technology has the characteristics of good oil removal effect and simple operation, various pollutants in the landfill leachate easily cause membrane pollution, the service life of the membrane is influenced, and the membrane pollution is an unsolved technical problem.
When the polymeric ferric sulfate can provide nuclear hydroxyl complexes with various components in the coagulation treatment process, the components have various coagulation effects on particles in wastewater or colloidal particles in water. The high-valence complex ions with relatively small molecular mass are attracted by electronegative colloidal particles and suspended matters in the landfill leachate to enter the compact layer, so that the double electric layers of the compressed colloidal particles are compressed, the zeta potential is reduced, and the colloidal particles are rapidly destabilized and aggregated. When the ceramic membrane is used for filtration, raw liquid flows at a high speed in membrane pores, clarified penetrating fluid is small molecular substances (water molecules) and flows out of the membrane through micro nano pores under the pressure of liquid flow, and concentrated turbid liquid is large molecular substances (containing organic substances, bacteria and the like) and is intercepted by the membrane, so that the raw liquid achieves the purposes of separation, concentration, purification, sterilization and the like. When the adding amount of the polymeric ferric sulfate is 12g/L, the adding amount of the polyacrylamide is 10mg/L and the pH value is 8, the pollutant removal efficiency of the coagulated effluent is higher and the operation is stable. The treatment conditions of the two ceramic membranes on the coagulated effluent are integrated, and the effluent filtered by the SiC ceramic membrane is treated by Al under the same operation condition 2 O 3 The effluent after being filtered by the ceramic membrane has good quality, and the coagulated effluent treated by the ceramic membrane does not need to be subjected to long standing time, so that the treatment efficiency of the garbage leachate is improved. In addition, the pH value of the effluent treated by the polymeric ferric sulfate is not greatly changed and is still about neutral, the harmfulness of the coagulated effluent to the ceramic membrane is small, the pollution resistance of the ceramic membrane is relatively strong, and the ceramic membrane can be put into use after being cleaned simply physically when the filter cake layer is too thick, namely the ceramic membrane has relatively high economic benefit and can efficiently and economically solve the pollution problem of the landfill leachate.
Specifically, the harmless treatment method of the landfill leachate comprises the following steps: towards the refuseSequentially adding polymeric ferric sulfate solution and polyacrylamide solution into the percolate to obtain coagulated turbid liquid, standing for layering, taking supernatant, and sequentially passing through SiC and Al 2 O 3 Filtering with the ceramic membrane. Wherein, the polyferric sulfate solution and the polyacrylamide solution are both aqueous solutions and are added into the landfill leachate sample in a wet adding manner.
The invention can further comprise the following technical scheme: the method for sequentially adding the polyferric sulfate solution and the polyacrylamide solution into the landfill leachate comprises the following steps:
in a 250mL beaker, adding sulfuric acid or sodium hydroxide solution into 100mL landfill leachate under a high-speed stirring state, and then adjusting the pH value to corresponding gradients, wherein the gradients are respectively 4, 5, 6, 7, 8, 9, 10, 11 and 12.
Placing the landfill leachate with the adjusted pH value on a magnetic stirrer, stirring at a high speed of 300r/min for 30s to a preset first time, respectively adding 10 mass percent of polyferric sulfate into the landfill leachate to enable the adding concentration gradient to be 7, 8, 9, 10, 11, 12, 13, 14 and 15g/L, continuously stirring at a high speed for 30s to a preset first time, then stirring at a low speed of 60r/min for 20min until a preset second time is reached, adding 1 mass percent of polyacrylamide to enable the adding concentration to be 10mg/L, standing for 30min, taking supernatant to measure COD, total phosphorus and UV (ultraviolet) 254 。
The supernatant was treated with SiC ceramic membrane and Al 2 O 3 Ceramic film of (3) and SiC and Al 2 O 3 The ceramic membrane is used for membrane filtration, an effluent water sample is taken every 2 hours, and the membrane flux, the effluent turbidity, the COD concentration and the UV are measured simultaneously 254 . Wherein the effective filtering area of the SiC ceramic membrane is 0.03136m 2 The pure water flux is 4669.63L/(m) 2 H) transmembrane pressure difference of 0.065 MPa. Al (Al) 2 O 3 The effective filtering area of the ceramic membrane is 0.024424m 2 The pure water flux is 924.78L/(m) 2 H) transmembrane pressure difference of 0.09 MPa.
Finally, cleaning the filter cake on the membrane in a physical mode, and removing SiC and Al of the filter cake 2 O 3 Of a ceramic membraneTo be put into recycling use again.
Further, the parameters of the steps are verified through experiments:
as shown in FIGS. 1 to 3, COD, total phosphorus and UV measured for the supernatant after coagulation 254 . As can be seen from figure 1, the COD concentration of the coagulation water is firstly reduced and then increased along with the increase of the addition of the polymeric ferric sulfate, when the addition of the coagulant is 12g/L, the COD concentration can be reduced to 522.33mg/L at the lowest, and the removal rate reaches 64.92%. As can be seen in FIG. 2, the total phosphorus effluent concentration decreases with the increase of the addition of the coagulant, and when the addition of the polymeric ferric sulfate is 12g/L, the concentration of the total phosphorus in the effluent is reduced from 6.10mg/L of the landfill leachate to 0.27mg/L, the removal rate is as high as 95.55%, and the total phosphorus concentration is remarkably reduced. As can be seen from figure 3, the effluent UV of the landfill leachate after coagulation 254 The addition amount of the coagulant is reduced along with the increase of the addition amount of the coagulant, the lowest addition amount of the coagulant reaches 2.37AU/cm when the addition amount of the coagulant is 14g/L, and when the addition amount of the coagulant is 12g/L, the effluent UV (ultraviolet) is 254 The value of (A) is 2.79AU/cm, and the removal rate is also 74.77%.
As shown in fig. 4-6, the parameters of the removal rate of landfill leachate in different pH ranges are compared. As can be seen from FIG. 4, with the increase of pH, the COD concentration of the coagulated water is in the trend of descending first and then ascending, and when the pH of the landfill leachate is 8-9, the COD removal rate is basically kept equal and can reach more than 56%. As can be seen from FIG. 5, the total phosphorus concentration of the coagulated water generally shows a tendency of decreasing first and then increasing with the increase of pH, and when the pH is 7-9, the total phosphorus concentration of the coagulated water reaches below 0.5mg/L, and the yielding water is stable. When the pH value is 7, the effluent concentration of the total phosphorus reaches the lowest value, namely 0.22mg/L, and the removal rate can reach 97.14 percent. When the pH value is 8, the total phosphorus concentration is 0.26mg/L, and the removal rate is about 96.29 percent. UV (ultraviolet) light 254 As shown in FIG. 6, the pH of the stock solution was decreased and then increased, and the pH was too low, which resulted in UV at pH 3 254 The value changes to a greater extent during the measurement, so UV at pH 3 is rejected 254 Experimental data. When the pH of the landfill leachate is 7, UV 254 The effluent is the lowest and is about 1.23AU/cm, and the removal rate is about 88.89%. When the pH is 8, the effluent is UV 254 1.41AU/cm, and 87.23% removal rateHigh removal efficiency. Considering that the pH value of the landfill leachate is within the range of 8.02 +/-0.1 and the pollutant removal efficiency difference is not large when the pH value is 7 and 8, if the pH value of the landfill leachate is within the range of 7-8, which is neutral and alkaline, the landfill leachate can be directly subjected to subsequent coagulation treatment without being treated.
Before the ceramic membrane is filtered, a ceramic membrane, a vacuum gauge and a silicon hose of a small self-priming booster pump are connected, and after the connection is finished, the ceramic membrane is placed in pure water to be filtered for a period of time, so that gas in the ceramic membrane is removed completely, meanwhile, the air tightness of the device is checked, the ceramic membrane is placed in a glass cylinder filled with a certain amount of coagulated water to be filtered after the air tightness is determined to be free from air leakage and the gas in the ceramic membrane is removed completely. Flux under different transmembrane pressure differences is measured when the ceramic membrane filters pure water before the coagulation effluent is filtered, so that the flux of the membrane is preliminarily determined. As can be seen from FIG. 7, in pure water, as the transmembrane pressure difference increases, the flux increases and Al 2 O 3 The minimum transmembrane pressure difference of the ceramic membrane is 0.02MPa, and the membrane flux is 114.11L/(m) at the minimum 2 H) the flux is almost 0 when the transmembrane pressure difference is less than 0.01MPa, and the maximum transmembrane pressure difference can reach 0.09MPa, wherein the flux is 924.78L/(m) at most 2 H). The minimum transmembrane pressure difference of the SiC ceramic membrane is 0.01MPa, and the membrane flux is 402.63L/(m) at the minimum 2 H) maximum transmembrane pressure difference of 0.065MPa, at which the flux is at most 4669.63L/(m) 2 H). The transmembrane pressure difference is adjusted to the maximum when the coagulation effluent is filtered. The membrane flux of the ceramic membrane was measured after the operation of the membrane filtration apparatus, and it can be seen from fig. 8 that the membrane flux of both types of ceramic membranes tended to decrease with the increase of the operation time, and within 12h, Al was present 2 O 3 The ceramic film is reduced to 296.45L/(m) 2 H), the membrane flux of the SiC ceramic membrane is always kept low and is only 78.10L/(m) at the lowest 2 H), it can be seen that Al is present in the experiment 2 O 3 Has stronger anti-pollution capability than SiC. The COD effluent condition of the coagulated effluent filtered by the ceramic membranes is shown in figure 9, within 12h, the COD concentrations of the effluent of the two ceramic membranes have certain fluctuation, but the range is not large, and the COD effluent concentration of the SiC ceramic membrane is obviously lower than that of the COD effluent of the Al ceramic membrane 2 O 3 The lowest COD effluent concentration of the ceramic membrane is about 524.19mg/L, the removal rate is about 64.82 percent, and the COD removal rate is improved by 8.82 percent compared with the COD removal rate of coagulation effluent before the membrane passes through. Al-containing compound 2 O 3 The highest COD removal rate of the effluent after the ceramic membrane is about 58.87 percent, and the COD removal rate is only improved by 2.87 percent. The SiC ceramic membrane is obviously superior to Al in terms of COD removal efficiency 2 O 3 A ceramic membrane. As can be seen from FIG. 10, the total phosphorus concentration of the coagulated water after being filtered by the two membranes is relatively stable, the total phosphorus concentration of the water from the SiC ceramic membrane is 0.24-0.26mg/L, the removal rate is 95.72-95.93%, and Al is 2 O 3 The total phosphorus concentration of the ceramic membrane effluent is 0.33-0.37mg/L, and the removal rate is 93.98-94.5%. Although the total phosphorus effluent concentration is lower, it can be seen that the difference between the total phosphorus concentration after membrane filtration and the total phosphorus concentration of effluent without membrane filtration is not great, which also indicates that the total phosphorus removal capability of the two ceramic membranes adopted in the experiment on the landfill leachate coagulation effluent is poor. The garbage leachate which is not subjected to coagulation treatment is dark brown, has low transparency and high turbidity of 216.5NTU, has a decoloring effect on colored substances in the garbage leachate, the turbidity of the coagulated supernatant after standing for 30min is measured to be 4.1NTU, 98.11% of turbidity is removed only through coagulation treatment, and the coagulation has a good removing effect on the turbidity. In the presence of SiC and Al respectively 2 O 3 After the ceramic membrane, a certain water sample is taken to detect the turbidity, and as can be seen from fig. 11, the turbidity is detected by Al 2 O 3 The turbidity of the coagulation effluent filtered by the ceramic membrane is stable, and within 12 hours, Al is contained 2 O 3 The turbidity of the ceramic membrane effluent is always lower than 0.65NTU, and the turbidity removal rate can reach 99.82 percent compared with the turbidity removal rate of the landfill leachate stock solution. The effluent turbidity after the SiC treatment is higher in the first two hours, and the analysis reason is that the aperture of the SiC ceramic membrane is larger, and the effluent turbidity is higher due to the fact that fine particles in the coagulated water sample pass through the ceramic membrane at the initial stage of operation. After the equipment is operated for 2 hours, a thick filter cake layer is formed on the surface of the membrane, so the turbidity removal rate is increased, the effluent turbidity shows a trend of decreasing along with time from the 4 th hour, and after the equipment is operated for 12 hours, the effluent turbidity of the SiC ceramic membrane can be reduced to 0.68NTU, the removal rate reaches 99.69%, and Al are removed 2 O 3 The turbidity of the effluent of the ceramic membrane is similar, but the membrane flux and the stability of the ceramic membrane are both higher than that of Al 2 O 3 Poor ceramic film, therefore Al 2 O 3 The effect of the ceramic membrane on removing turbidity is better than that of the SiC ceramic membrane. UV (ultraviolet) for coagulating effluent by ceramic membrane filtration 254 The effect of (2) is shown in FIG. 12, and it can be seen that the UV of the coagulated water is affected by the two ceramic membranes 254 The removal is stable, within 12 hours of operation, the removal rate of the SiC ceramic membrane is higher than that of the Al ceramic membrane 2 O 3 Ceramic membrane can remove UV in 84.26% raw water 264 To pass through Al 2 O 3 The removal rate of the ceramic membrane effluent can only reach 75.49%.
As shown in fig. 13-15, the landfill leachate continuously passes through SiC and Al after being coagulated 2 O 3 Parameters after ceramic membrane change. The removal rate after COD passing through the membrane is shown in FIG. 13, and the COD concentration of the effluent of the SiC ceramic membrane is lower than that of Al on the whole in the 12-hour operation period 2 O 3 Ceramic membrane filtration with SiC ceramic membrane followed by Al 2 O 3 The COD removal rate of the ceramic membrane filtered water is obviously increased and is more stable than that of single membrane filtered water, and the highest COD removal rate can reach 59.99%. The removal rate of the total phosphorus in the ceramic membrane effluent is shown in figure 10, and the trend that the removal rate of the total phosphorus after the two-stage ceramic membrane filtration is increased from fluctuation can be seen, but the removal effect of the ceramic membrane on the total phosphorus is generally poor, so that the concentration of the total phosphorus in the two-stage membrane filtration effluent is similar to that of Al 2 O 3 The ceramic membrane effluent concentration and the removal rate are not greatly improved. FIG. 11 shows the warp of Al 2 O 3 Ceramic membrane filtered effluent UV 254 Compared with the method of singly passing through a SiC ceramic membrane, the method has higher effluent concentration and two-stage combination of the ceramic membrane to UV 254 The removal efficiency is not obvious, and is similar to the SiC ceramic membrane with better water outlet effect, and the highest removal efficiency is 84.29%.
Furthermore, it should be understood that although the present description refers to embodiments, not every embodiment may contain only a single embodiment, and such description is for clarity only, and those skilled in the art should integrate the description, and the embodiments may be combined as appropriate to form other embodiments understood by those skilled in the art.
Claims (10)
1. A method for innocent treatment of landfill leachate is characterized by comprising the following steps: sequentially adding a polymeric ferric sulfate solution and a polyacrylamide solution into the landfill leachate to obtain a coagulated turbid liquid, standing for layering, and sequentially passing the supernatant through SiC and Al 2 O 3 Filtering with the ceramic membrane.
2. The method of claim 1, wherein the sequential addition of the polyferric sulfate solution and the polyacrylamide solution to the landfill leachate comprises:
adding a polyferric sulfate solution into landfill leachate in a high-speed stirring state, stirring until a preset first time length, adding a polyacrylamide solution, stirring until the preset first time length is reached, then switching to low-speed stirring until a preset second time length is reached, wherein the speed of the high-speed stirring is 5 times of the speed of the low-speed stirring, and the preset second time length is 40 times of the preset first time length.
3. The method according to claim 1 or 2, wherein the mass fraction of the polyferric sulfate solution is 10%, the mass fraction of the polyacrylamide solution is 1%, the feeding amount of the polyferric sulfate solution per unit volume of landfill leachate is 7-14g/L, and the feeding amount of the polyacrylamide solution is 10 mg/L.
4. The method of claim 3, wherein the optimum dosage of the polyferric sulfate solution is 12 g/L.
5. The method of claim 1 or 2, wherein before the sequential addition of the polyferric sulfate solution and the polyacrylamide solution to the landfill leachate, the method further comprises:
and adjusting the pH value of the landfill leachate to a preset pH value range, wherein the preset pH value range is 4-12.
6. The method according to claim 5, wherein the preset pH value is in the optimal range of 7-8.
7. The method of claim 1, wherein the SiC ceramic membrane has an effective filtration area of 0.03136m 2 The pure water flux is 4669.63L/(m) 2 H) transmembrane pressure difference of 0.065 MPa.
8. The method of claim 1, wherein the Al is 2 O 3 The effective filtering area of the ceramic membrane is 0.024424m 2 The pure water flux is 924.78L/(m) 2 H) transmembrane pressure difference of 0.09 MPa.
9. The method of claim 1, wherein the supernatant is sequentially passed through SiC and Al 2 O 3 Before the ceramic membrane filtration of (3), the method further comprises: SiC and Al to be assembled 2 O 3 The ceramic membrane is put into pure water for exhausting.
10. The method of claim 1, wherein the supernatant is sequentially passed through SiC and Al 2 O 3 After the ceramic membrane filtration of (3), the method further comprises: to be mixed with SiC and Al 2 O 3 When the filter cake of the ceramic membrane reaches the preset thickness, removing the filter cake by a physical cleaning method, and removing the SiC and Al of the filter cake 2 O 3 The ceramic membrane is put into recycling use again.
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