CN115676972A - Garbage leachate purification method - Google Patents
Garbage leachate purification method Download PDFInfo
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- CN115676972A CN115676972A CN202211325467.4A CN202211325467A CN115676972A CN 115676972 A CN115676972 A CN 115676972A CN 202211325467 A CN202211325467 A CN 202211325467A CN 115676972 A CN115676972 A CN 115676972A
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a method for purifying landfill leachate, and belongs to the technical field of pollution control. The landfill leachate purification method comprises the following steps: and filtering the landfill leachate by adopting a tubular or multi-pore ceramic membrane component. The invention has high impurity removal rate, and the reduction range of micron-sized particles reaches more than 99 percent. The membrane is not easy to block, and the membrane component has few accumulated matters, is very easy to clean, needs short time and has low cost. The flow rate decay is slow and a satisfactory flow rate value can be obtained even when the clogging is severe. The ceramic membrane cleaning operation is simple. Corrosion resistance and long service life.
Description
Technical Field
The invention relates to a method for purifying landfill leachate, and belongs to the technical field of pollution control.
Background
The landfill leachate refers to sewage generated by digestion, rainwater leaching and scouring and surface water and underground water soaking of domestic garbage in the stacking and landfill processes. The amount of landfill leachate generated from a landfill is determined by the water capture capacity, site surface conditions, solid waste conditions, landfill structure, operating conditions, and other factors, and is limited by other factors, such as the amount of water consumed to form landfill gas, the amount of water consumed to form water vapor, and the like.
The composition of the household waste disposed of at each local municipal landfill site is substantially similar and the composition of the leachate produced is also substantially the same. Generally comprises four types of organic matters including soluble organic matters, inorganic major components, heavy metals and heterotype biomass. The soluble organic matter can be expressed as COD Cr Or TOC includes hydrocarbons, volatile fatty acids and some refractory organics, such as humic acid compounds. Inorganic major components of Ca, mg, na, K and NH 4 + 、Fe、Mn、Cl - 、SO 4 2- And the like are common inorganic elements. Heavy metals: cd. Cr, cu, pb, ni, zn, hg and metallic As. Certainly, when the product is used as a complex water body, particularly the effluent after long-term treatment and stabilization, the content of microorganisms in the leachate is high, and the product becomes another substance which cannot be ignored in the leachate.
Landfill leachate from landfills is a potential source of surface and ground water pollution. First, leachate permeates downward through the landfill site, and as time goes on, when soil under the landfill site adsorbs most organic pollutants to reach saturation, the pollutants can be fan-shaped diffusion along the groundwater flow direction, causing pollution to groundwater. Secondly, the percolate guided out through the diversion pipe of the refuse landfill is often used for farmland irrigation or discharged into rivers and lakes without being completely treated. Organic pollutants and inorganic pollutants entering rivers or farmlands along with leachate can pollute aquatic organisms and crops, and finally harm human health through a food chain and the ecological environment. Wherein, the aerobic degradation of the organic matter contained in the leachate consumes the dissolved oxygen in the sewage, and the high-concentration ammonia nitrogen usually contained in the leachate can be oxidized into nitrate under the action of digestive bacteria, so that the water body is anoxic, and the fishes and other aquatic organisms are killed in large scale. Meanwhile, after ammonia nitrogen in the percolate enters the water body, the ammonia nitrogen is converted into nitrate nitrogen and nitrite nitrogen under the action of microorganisms in the water. Nitrate nitrogen and nitrite nitrogen are precursor substances of nitroso compounds which are strong chemical carcinogens, have carcinogenic, mutagenic and teratogenic properties and are very serious in harm to human bodies. The maximum allowable concentration of nitrate nitrogen is 10mg/L according to the drinking water quality standard promulgated by the world health organization. The leachate enters the water body to accelerate the eutrophication process of the water body, after the water body is eutrophicated, algae are rapidly propagated, the ecological environment of the water body is seriously damaged, the dissolved oxygen in the water is reduced, animals, particularly fishes, in the water body die, some blue algae have the strongest toxicity and wide pollution range, and chemical substances toxic to the fishes and human beings can be released, so that a great amount of organisms in the water body die.
The main problems of the landfill leachate treatment are as follows: the rainwater and sewage diversion measures are not thorough, so that the generation amount of percolate is large; the leachate contains high-concentration ammonia nitrogen; poor biodegradability; the operation management level of the percolate treatment plant is low; the investment of the percolate treatment cost is insufficient, so that the cost of the landfill percolate treatment is reduced.
The current treatment methods of leachate include physical chemical methods and biological methods. Biological methods are divided into aerobic biological treatment, anaerobic biological treatment and a combination of the two. The aerobic treatment comprises an activated sludge process, an aeration oxidation pond, an aerobic stabilization pond, a biological rotating disc, a trickling filter and the like. The anaerobic treatment comprises an upflow sludge bed, an anaerobic immobilized bioreactor, a mixing reactor and an anaerobic stabilization pond. The physical and chemical method mainly comprises various methods such as activated carbon adsorption, chemical precipitation, chemical oxidation, chemical reduction, ion exchange, membrane dialysis, gas stripping, wet oxidation and the like, when the COD is 2000-4000 mg/L, the removal rate of the COD can reach 50% -87%, compared with biological treatment, the physical and chemical treatment is not influenced by the change of water quality and quantity, the quality of effluent is relatively stable, and particularly the BOD is treated 5 The landfill leachate which has a low COD ratio and is difficult to biologically treat has a good treatment effect. But the impurity removal rate thereof is to be further improved.
Anaerobic fermentation refers to a process in which organic substances are decomposed and metabolized by various microorganisms under certain moisture, temperature and anaerobic conditions to finally form combustible mixed gas such as methane, carbon dioxide and the like. The fermentation process comprises a liquefaction stage, an acidogenesis stage and a methanogenesis stage. A liquefaction stage: since various solid organic substances generally cannot enter microorganisms and are utilized by the microorganisms, the solid organic substances must be hydrolyzed into soluble monosaccharides, amino acids, glycerol, and fatty acids having relatively small molecular weights by extracellular enzymes and surface enzymes (surface enzymes such as cellulase, protease, and lipase) secreted by aerobic and anaerobic microorganisms. The soluble substances with relatively small molecular mass can enter the microbial cells to be further decomposed and utilized. Acid production stage: various soluble substances (monosaccharide, amino acid, fatty acid, etc.) are continuously decomposed and converted into low molecular substances, such as butyric acid, propionic acid, acetic acid, alcohol, ketone, aldehyde, etc., under the action of intracellular enzymes of cellulose bacteria, protein bacteria, fat bacteria, and pectin bacteria; and meanwhile, part of inorganic substances such as hydrogen, carbon dioxide, ammonia and the like are released. However, in this stage, acetic acid, which is the main product, accounts for about 70% or more, and is referred to as the acidogenic stage. The bacteria that participate in this phase are called acid forming bacteria. A methanogenesis stage: simple organic matters such as acetic acid and the like decomposed in the second stage are decomposed into methane and carbon dioxide by methanogens, wherein the carbon dioxide is reduced into methane under the action of hydrogen. This stage is referred to as the gas production stage, or as the methane production stage.
Disclosure of Invention
The invention aims to provide a novel method for purifying landfill leachate, which has high impurity removal rate.
In order to achieve the above object of the present invention, the method for purifying landfill leachate comprises: and filtering the landfill leachate by adopting a tubular or multi-pore ceramic membrane component.
In one embodiment, the ceramic membrane of the ceramic membrane module has an average pore size of 50nm.
In one embodiment, the ceramic membrane is an alumina porous ceramic membrane.
In one embodiment, the ceramic membrane tube diameter R of the ceramic membrane module 1 =0.032m, length L =0.2m, and a plurality of through holes, preferably 19 through holes, are uniformly distributed on the cross section of the ceramic membrane tube; preferably, the polishing length of the outer parts of the two ends of the ceramic membrane tube is 0.026m, and the thickness of the ceramic membrane tube is 0.002m.
In a specific embodiment, the landfill leachate is landfill leachate after anaerobic fermentation.
In one embodiment, the average particle size of the solids in the landfill leachate is 5 to 21 μm.
In one embodiment, the cross-flow rate of filtration is 1.2L/h and the flux of filtration is 4L/h.
In one embodiment, the filtration is stopped every 2 hours and the ceramic membrane assembly is back-flushed with 0.1 to 1mol/L sodium hydroxide.
The back flushing refers to the direction opposite to the filtering direction of the landfill leachate.
In one embodiment, the ceramic membrane assembly is back-washed with 0.1mol/L sodium hydroxide.
In one embodiment, the time for back flushing the ceramic membrane assembly with sodium hydroxide is 10min.
Has the advantages that:
1. the invention has high impurity removal rate, and the reduction range of micron-sized particles reaches more than 99 percent.
2. The membrane is not easy to block, and the membrane component has few accumulated matters, is very easy to clean, needs short time and has low cost.
3. The flow rate decay is slow and a satisfactory flow rate value can be obtained even when the clogging is severe.
4. The ceramic membrane cleaning operation is simple.
5. Corrosion resistance and long service life.
Drawings
FIG. 1 is a diagram of a filtration apparatus according to an embodiment of the present invention;
1-feedstock tank in fig. 1; 2-a peristaltic pump; 3-a membrane module; 4-valve 1; 5-valve 2; 6-a permeate side collection tank; a 7-cross-flow recovery tank.
Fig. 2 is a diagram of a filter device according to an embodiment of the present invention.
FIG. 3 is a graph showing the distribution of particle size before and after filtration through anaerobic percolate filter paper.
FIG. 4 is a graph showing the particle size distribution before and after filtration of anaerobic leachate according to example 1.
FIG. 5 is a graph showing the distribution of the particle size before and after the filtration of the aerobic leachate filter paper.
FIG. 6 is a distribution diagram of the particle size before and after the ceramic membrane filtration of the aerobic leachate.
FIG. 7 is a schematic view of a ceramic membrane module used in the examples, the left drawing being an axial view and the right drawing being a cross-sectional view.
FIG. 8 is an assembly drawing showing the use of the ceramic membrane, and the left drawing is a drawing of the housing for mounting the ceramic membrane; the right drawing shows the ceramic membrane mounted in the housing.
Detailed Description
In order to achieve the above object of the present invention, the method for purifying landfill leachate comprises: and filtering the landfill leachate by adopting a tubular or multi-pore ceramic membrane component.
In one embodiment, the ceramic membrane of the ceramic membrane module has an average pore size of 50nm.
In one embodiment, the ceramic membrane is an alumina porous ceramic membrane.
In one embodiment, the ceramic membrane module has a ceramic membrane tube diameter R 1 =0.032m, length L =0.2m, and a plurality of through holes, preferably 19 through holes, are uniformly distributed on the cross section of the ceramic membrane tube; preferably, the polishing length of the outer parts of the two ends of the ceramic membrane tube is 0.026m, and the thickness of the ceramic membrane tube is 0.002m.
In one embodiment, the landfill leachate is landfill leachate after anaerobic fermentation.
In one embodiment, the average particle size of the solids in the landfill leachate is 5 to 21 μm.
In one embodiment, the cross-flow rate of filtration is 1.2L/h and the flux of filtration is 4L/h.
In one embodiment, the filtration is stopped every 2 hours and the ceramic membrane assembly is back-flushed with 0.1 to 1mol/L sodium hydroxide.
The back flushing refers to the direction opposite to the filtering direction of the landfill leachate.
In one embodiment, the ceramic membrane assembly is back-washed with 0.1mol/L NaOH.
By comparing the back washing with tap water and sodium hydroxide solution, the effect of using the sodium hydroxide solution is more obvious in the same time.
The concentration of sodium hydroxide also needs to be ensured within a certain range, the main material of the ceramic membrane is alumina, sodium hydroxide with too high concentration is easy to generate sodium metaaluminate with alumina, the service life of the ceramic membrane is reduced, and 0.1mol/L of sodium hydroxide is generally used as backwash liquid.
In one embodiment, the time for back flushing the ceramic membrane assembly with sodium hydroxide is 10min.
The following examples are provided to further illustrate the embodiments of the present invention and are not intended to limit the scope of the present invention.
Example 1
The device is connected: an alumina porous ceramic membrane tube having an average pore diameter of 50nm was used, and the appearance thereof is shown in FIG. 7. The diameter R1=0.032m of the ceramic membrane tube, the length L =0.2m and 19 holes, the polishing length of the outer parts of the two ends of the ceramic membrane tube is 0.026m, the thickness of the ceramic membrane tube is close to 0.002m, and the polishing aims to enable the components to be connected more tightly and prevent liquid leakage. Is installed in a stainless steel shell shown in figure 8, and the stainless steel shell shown in figure 8 is provided with a feed inlet, a discharge outlet and a permeate side discharge outlet. The feed inlet and the discharge outlet are respectively matched with the cross section of the ceramic membrane tube, the discharge outlet on the permeation side is arranged on the side wall of the stainless steel tube, and the discharge outlet on the permeation side is axially vertical to the stainless steel tube. The stainless steel shell is DN32 fast-assembling interface, the material is 314 and/or 316L, the feed inlet and the discharge outlet are respectively connected with the rubber tube through the flange, as shown in figure 1 and figure 2, the rubber tube of the feed inlet is connected with the peristaltic pump 2. The material outlet of the permeation side is provided with a valve 1, the material outlet is provided with a valve 2, a rubber pipe of the material inlet is communicated with the raw material tank 1, the material outlet of the permeation side is communicated with the material collecting tank 6 of the permeation side through the valve 1, and the cross flow recovery tank 7 is communicated with the material outlet through the valve 2.
The leachate after anaerobic fermentation is adopted, the particle size of solid pollutants in the leachate is detailed in a table 1, the leachate is filled into a raw material tank 1, valves 1 and 2 are opened, and then a peristaltic pump 2 is started for filtration. The grain size number of the percolate is reduced and is obvious, and the reduction range of micron-sized grains reaches more than 99 percent. The changes before and after filtration are detailed in Table 1. The standard of the purified suspended substance reaches the GB 8978-88 comprehensive primary sewage discharge standard.
When the cross flow is 1.2L/h, the flux amount is 4L/h, after 2h of filtration, the inlet position is changed, and the flux recovery of the ceramic membrane can be completed by using 1mol/L sodium hydroxide for washing for 10min. The feasibility of the ceramic membrane filtration treatment of the leachate is illustrated.
Comparative example 1
Directly filtering the percolate after anaerobic fermentation by using filter paper. The filtration results are detailed in table 1.
TABLE 1 particle size variation before and after separation of leachate from anaerobic fermentation
| Anaerobic fermentation percolate | Comparative example 1 | Example 1 | |
| Average particle diameter μm | 20.292 | 10.421 | 6.709 |
| D50 | 5.821 | 5.821 | 3.416 |
| D90 | 14.289 | 14.289 | 9.614 |
As can be seen from Table 1, the average particle size of the percolate can be reduced by both filter paper filtration and membrane filtration, and the average particle size can be reduced from 20.292 μm to 10.421 μm by filter paper filtration, and can be further reduced to 6.709 μm after the number of particles is reduced by two orders of magnitude after membrane filtration. It can also be concluded from D50 and D90 that membrane filtration has a certain cutoff effect on the particle size distribution.
Comparative example 2
The other is identical to example 1, except that the percolate after aerobic fermentation is used.
Comparative example 3
The other is identical to comparative example 1, except that leachate after aerobic fermentation is used.
The particle size change before and after filtration of comparative examples 2 and 3 is detailed in Table 2.
TABLE 2 particle size variation before and after separation of the aerobic fermentation leachate
| Aerobic fermentation percolate | Comparative example 3 | Comparative example 2 | |
| Average particle diameter μm | 7.007 | 7.007 | 7.678 |
| D50 | 3.126 | 3.126 | 3.846 |
| D90 | 4.121 | 4.121 | 5.433 |
Claims (10)
1. The method for purifying the landfill leachate is characterized by comprising the following steps: and filtering the landfill leachate by adopting a tubular or multi-pore ceramic membrane component.
2. The landfill leachate purification method of claim 1, wherein the ceramic membrane of the ceramic membrane module has an average pore size of 50nm.
3. The landfill leachate purification method of claim 1 or 2, wherein the ceramic membrane is made of an alumina porous ceramic membrane.
4. The landfill leachate purification method according to claim 3, wherein the ceramic membrane module has a ceramic membrane tube diameter R 1 =0.032m, length L =0.2m, and a plurality of through holes, preferably 19 through holes, are uniformly distributed on the cross section of the ceramic membrane tube; preferably, the grinding length of the outer parts of the two ends of the ceramic membrane tube is 0.026m and 0.002m thick.
5. The method for purifying landfill leachate according to claim 1 or 2, wherein the landfill leachate is landfill leachate after anaerobic fermentation.
6. The landfill leachate purification method of claim 1 or 2, wherein the average particle size of the solids in the landfill leachate is 5-21 μm.
7. The method for purifying landfill leachate according to claim 1 or 2, wherein the cross flow rate of filtration is 1.2L/h, and the filtration flux is 4L/h.
8. The method for purifying landfill leachate according to claim 1 or 2, wherein the filtration is stopped every 2 hours, and the ceramic membrane module is back-washed with 0.1 to 1mol/L sodium hydroxide.
9. The landfill leachate purification method of claim 8, wherein the ceramic membrane module is back-washed with 0.1mol/L NaOH.
10. The landfill leachate purification method according to claim 8 or 9, wherein the time for back-flushing the ceramic membrane module with sodium hydroxide is 10min.
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| CN202211325467.4A CN115676972A (en) | 2022-10-27 | 2022-10-27 | Garbage leachate purification method |
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