CN115536214A - Method for treating leachate of waste incineration plant - Google Patents
Method for treating leachate of waste incineration plant Download PDFInfo
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- CN115536214A CN115536214A CN202211242576.XA CN202211242576A CN115536214A CN 115536214 A CN115536214 A CN 115536214A CN 202211242576 A CN202211242576 A CN 202211242576A CN 115536214 A CN115536214 A CN 115536214A
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Images
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides a method for treating leachate of a waste incineration plant, which comprises the following steps: s1, performing solid-liquid separation treatment on the leachate of the waste incineration plant to obtain primary purified leachate and a first solid-phase product; s2, performing multistage anaerobic treatment on the primary purified percolate to obtain a gas-phase product, a first liquid-phase product and a second solid-phase product; s3, performing biochemical degradation treatment on the first liquid-phase product under the condition that the dissolved oxygen is 0.2-0.8 mg/L to obtain nitrogen and a second liquid-phase product; the biochemical degradation treatment process is a simultaneous shortcut nitrification anaerobic ammonia oxidation denitrification process, the participating microorganisms comprise nitrosobacteria, anaerobic ammonia oxidation bacteria and heterotrophic denitrifying bacteria, and the biochemical degradation treatment process comprises the nitrosobacteria nitrosation process, the anaerobic ammonia oxidation process and the heterotrophic denitrifying bacteria denitrifying process. The method can obviously reduce the total nitrogen and COD content and has low energy consumption.
Description
Technical Field
The invention relates to the technical field of treatment of leachate of a waste incineration plant, in particular to a treatment method of the leachate of the waste incineration plant.
Background
The garbage incineration treatment technology has the advantages of reducing, harmless and recycling household garbage and the like, and is gradually widely applied in recent years. However, the process of increasing the calorific value by stacking fermentation before incineration of garbage generates a large amount of leachate which has the characteristics of complex components, high pollutant concentration, high toxicity and the like and is difficult to treat. Different from the leachate generated by a refuse landfill, the quality of the leachate of a refuse incineration plant has the following characteristics: (1) the COD concentration is higher, generally 25000-75000 mg/L; (2) High biodegradability, BOD 5 The ratio of COD to/is greater than 0.3; (3) the ammonia nitrogen concentration is high, generally 1000-2800 mg/L; (4) The salt content is high, the conductivity is high, the total hardness can reach 6500-11000 mg/L, and the chloride ion concentration can reach 3000-5000 mg/L; (5) the concentration of suspended matters is high (about 10000 mg/L); (6) the pH is low (about 4 to 6).
Based on the water quality characteristics of the leachate of the waste incineration plant, most of the prior leachate processes of the waste incineration plant adopt a combined process of pretreatment, anaerobism, aerobic MBR (membrane bioreactor), NF (nanofiltration) and RO (reverse osmosis). Although the above anaerobic process has low energy consumption, high load and capability of recovering bioenergy, the removal of organic substances is not thorough and has little effect on nitrogen removal. In order to remove the organic substances, anaerobic treatment is usually adopted in the prior art, and 60 to 95.5 percent of the organic substances in the leachate can be removed through the anaerobic treatment. However, the leachate from a waste incineration plant has an ultra-high COD concentration, and is difficult to remove by anaerobic treatment, so that high-content COD still remains in the anaerobic effluent. The conventional nitrification-denitrification process is generally adopted for denitrification through an aerobic MBR denitrification process, but the denitrification efficiency of the process is low, and the operation cost is high.
In addition, the ammonia nitrogen concentration of leachate in a waste incineration plant is high, and in order to reduce the ammonia nitrogen concentration and improve the quality of treated effluent, a single-stage or multi-stage A/O-MBR water treatment process (anaerobic-aerobic MBR process) is usually adopted to further remove the total nitrogen and COD content in the leachate. However, the lack of anaerobic treatment for removing the residual high concentration COD requires more aeration, which results in more energy consumption for aeration and is not favorable for reducing the treatment cost. In addition, because the ammonia nitrogen concentration in the leachate of the waste incineration plant is high, in order to ensure the smooth operation of the nitrification-denitrification process, not only a large amount of aeration is needed, but also longer hydraulic retention time and higher reflux ratio are needed to ensure that the system is not poisoned and collapsed due to overhigh ammonia nitrogen concentration, and the processes all need higher energy consumption and operation cost.
On the basis, in order to solve the problems in the prior art, a method for treating leachate from a waste incineration plant, which has a good treatment effect, low energy consumption and low treatment cost, needs to be provided.
Disclosure of Invention
The invention mainly aims to provide a method for treating leachate of a waste incineration plant, which aims to solve the problems of low total nitrogen and COD removal rate, high energy consumption and high treatment cost in the prior art.
In order to achieve the above object, one aspect of the present invention provides a method for treating leachate of a waste incineration plant, the method comprising: s1, performing solid-liquid separation treatment on leachate of a waste incineration plant to obtain primary purified leachate and a first solid-phase product; s2, performing multistage anaerobic treatment on the primary purified percolate to obtain a gas-phase product, a first liquid-phase product and a second solid-phase product; s3, performing biochemical degradation treatment on the first liquid-phase product under the condition that the dissolved oxygen is 0.2-0.8 mg/L to obtain nitrogen and a second liquid-phase product; the biochemical degradation treatment process is a simultaneous shortcut nitrification anaerobic ammonia oxidation denitrification process, the participating microorganisms comprise nitrosobacteria, anaerobic ammonia oxidation bacteria and heterotrophic denitrifying bacteria, and the biochemical degradation treatment process comprises the nitrosobacteria nitrosation process, the anaerobic ammonia oxidation process and the heterotrophic denitrifying process.
Furthermore, the biochemical degradation treatment process is carried out in a membrane bioreactor, the hydraulic retention time in the membrane bioreactor is 2-5 days, and the treatment temperature is 30-35 ℃.
Furthermore, the membrane in the membrane bioreactor is a tubular ceramic membrane, the aperture of the tubular ceramic membrane is 0.1-0.8 mu m, and the membrane flux is 18-20L/(m) 2 H); preferably, the biochemical degradation treatment process is carried out in an external cross-flow membrane bioreactor.
Furthermore, a dissolved oxygen online monitoring device is adopted to detect and regulate the dissolved oxygen in real time, so that the concentration of the dissolved oxygen in the biochemical degradation treatment process is 0.2-0.5 mg/L.
Further, the multistage anaerobic treatment comprises the steps of sequentially carrying out primary anaerobic treatment and secondary anaerobic treatment on the primary purified percolate, wherein the primary anaerobic treatment is carried out in a primary anaerobic reactor, the secondary anaerobic treatment is carried out in a secondary anaerobic reactor, and the primary anaerobic reactor and the secondary anaerobic reactor are arranged in series; wherein, in the first-stage anaerobic treatment process, the reaction temperature is 33-38 ℃, the hydraulic retention time is 5-10 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is measured to be 85-90%; in the second-stage anaerobic treatment process, the reaction temperature is 33-38 ℃, the hydraulic retention time is 2-5 days, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 65-85%.
Furthermore, the COD concentration in the first liquid phase product is 800-1000 mg/L, and the TN value is 1100-2600 mg/L.
Further, the solid-liquid separation treatment sequentially comprises: s4, filtering the percolate of the waste incineration plant by using a filtering device to remove solid impurities and hair; s5, carrying out sedimentation treatment by adopting a sedimentation tank to remove soil and sandstone; and S6, homogenizing by using an adjusting tank to obtain primary purified percolate and a first solid-phase product.
Further, filteringThe screening aperture of the device is 2-4 mm; the surface load of the sedimentation tank is 0.35 to 0.85m 3 /(m 2 H), the time of the sedimentation treatment is 1 to 2h.
Further, the treatment method of the leachate of the waste incineration plant also comprises the following steps: carrying out nanofiltration treatment on the second liquid-phase product under the condition of first operating pressure to obtain nanofiltration liquid and first concentrated liquid; carrying out reverse osmosis treatment on the nanofiltration liquid under the condition of a second operation pressure to obtain first purified water and second concentrated liquid; under the condition of a third operating pressure, disc-tube reverse osmosis concentrated solution reduction treatment is respectively carried out on the first concentrated solution and the second concentrated solution to obtain second purified water and a third concentrated solution; in the nanofiltration treatment process, the pH of the second liquid-phase product is 6.5-6.8, the nanofiltration membrane adopted in the nanofiltration treatment is one or more of polyvinylidene fluoride membrane, polytetrafluoroethylene and ceramic, the cut-off molecular weight of the nanofiltration membrane is 200-1000 daltons, and the first operating pressure is 0.5-0.7 MPa; preferably, the molecular weight cut-off of the nanofiltration membrane is 150-300 daltons; the reverse osmosis membrane adopted in the reverse osmosis treatment is one or more of polyamide, acetate fiber and polyamide, the reverse osmosis membrane can separate ions with the particle size of less than 1nm, and the second operating pressure is 1-3 MPa; the third operating pressure is 3-6 MPa.
Furthermore, the COD of the leachate of the waste incineration plant is 25000-75000 mg/L, the numerical value of BOD5/COD is 0.5-0.8, the ammonia nitrogen is 1000-2500 mg/L, the total hardness is 6500-11000 mg/L, the chloride ion concentration is 3000-5000 mg/L, the suspended matter concentration is 5000-10000 mg/L, and the pH value is 4-6.
By applying the technical scheme of the invention, the solid-liquid separation treatment process can remove suspended matters such as silt and the like in the leachate of the waste incineration plant, and avoid blocking equipment used in the subsequent treatment process. By carrying out multistage anaerobic treatment on the primary purified percolate, on the one hand, compared with single-stage anaerobic treatment, the multistage anaerobic treatment process can be adopted to further degrade organic matters in the percolate of the waste incineration plant, so that the COD concentration of the percolate can be reduced in a targeted manner; in the second aspect, the multistage anaerobic treatment is beneficial to improving the yield of the biogas, the subsequent recycling and reutilization and improving the economic benefit by improving the removal rate of organic matters; in the third aspect, the multistage anaerobic treatment can remove organic matters to the maximum extent, and the subsequent process is prevented from being influenced by organic matter inhibition.
Under the condition of the dissolved oxygen, by adopting the SNAD process based on the membrane bioreactor, nitrosobacteria carry out a nitrosation process on ammonia Nitrogen (NH) 4 + ) Partial oxidation to nitrous Nitrogen (NO) 2 - ) The anaerobic ammonia oxidizing bacteria convert the residual ammonia nitrogen and the nitrite nitrogen generated in the nitrosation process into nitrogen gas through the anaerobic ammonia oxidizing process and simultaneously generate nitrate Nitrogen (NO) 3 - ) Finally, the nitrate nitrogen generated in the process is converted into nitrogen (N) through the denitrification process of heterotrophic denitrifying bacteria 2 ). The total nitrogen content in the percolate can be effectively reduced by performing biochemical degradation treatment under the coupling action of the three main microorganisms, and the process only performs a nitrosation process (a nitrification process is not performed, about 25% of aeration quantity is saved), requires low dissolved oxygen and small aeration quantity, and is beneficial to reducing energy consumption; the anaerobic ammonia oxidation process is an autotrophic nitrogen removal process, no additional carbon source is needed, and the operation cost is saved.
On the basis, the membrane concentrated solution can be reduced by adopting the treatment method, and the damage of the membrane concentrated solution is finally eliminated through furnace returning and burning; meanwhile, other pollutants in percolate of a waste incineration plant can be greatly reduced, so that purified water meets the reuse standard of a water supplementing standard factory of an open circulating cooling water system in the municipal sewage recycling-industrial water quality GB/T19923-2005.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 shows a schematic view of a process flow of treating leachate from a waste incineration plant according to embodiment 1 of the present invention.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
As described in the background art, the prior treatment process of the percolate of the refuse incineration plant has the problems of low removal rate of COD and total nitrogen, high energy consumption and high treatment cost. In order to solve the technical problem, the application provides a method for treating leachate in a waste incineration plant, which comprises the following steps: s1, performing solid-liquid separation treatment on leachate of a waste incineration plant to obtain primary purified leachate and a first solid-phase product; s2, performing multistage anaerobic treatment on the primary purified percolate to obtain a gas-phase product, a first liquid-phase product and a second solid-phase product; s3, performing biochemical degradation treatment on the first liquid-phase product under the condition that the dissolved oxygen is 0.2-0.8 mg/L to obtain nitrogen and a second liquid-phase product; the biochemical degradation treatment process is a simultaneous partial nitrification anaerobic ammonia oxidation and denitrification process (SNAD), the participating microorganisms comprise nitrosobacteria, anaerobic ammonia oxidation bacteria and heterotrophic denitrifying bacteria, and the biochemical degradation treatment process comprises the nitrosobacteria nitrosation process, the anaerobic ammonia oxidation process and the heterotrophic denitrifying process.
By adopting the solid-liquid separation treatment process, suspended matters such as silt in leachate of a waste incineration plant can be removed, and equipment used in a subsequent treatment process is prevented from being blocked. By carrying out multistage anaerobic treatment on the primary purified percolate, on the one hand, compared with single-stage anaerobic treatment, the multistage anaerobic treatment process can be adopted to further degrade organic matters in the percolate of the waste incineration plant, so that the COD concentration of the percolate can be reduced in a targeted manner; in the second aspect, the multistage anaerobic treatment is beneficial to improving the methane yield, the subsequent recycling and reusing and improving the economic benefit by improving the organic matter removal rate; in the third aspect, the multistage anaerobic treatment can remove organic matters to the maximum extent, and the subsequent process is prevented from being influenced by organic matter inhibition.
Under the condition of dissolved oxygen, by adopting SNAD process based on membrane bioreactor, nitrosobacteria can make ammonia Nitrogen (NH) pass through nitrosation process 4 + ) Partial oxidation to nitrous Nitrogen (NO) 2 - ) Anaerobic ammonium oxidation bacteria drugThe anaerobic ammonia oxidation process converts the residual ammonia nitrogen and nitrite nitrogen generated in the nitrite oxidation process into nitrogen and simultaneously generates nitrate Nitrogen (NO) 3 - ) Finally, the generated nitrate nitrogen is converted into nitrogen (N) through the denitrification process of heterotrophic denitrifying bacteria 2 ). The total nitrogen content in the percolate can be effectively reduced by performing biochemical degradation treatment under the coupling action of the three main microorganisms, and the process only performs a nitrosation process (a nitrification process is not performed, about 25% of aeration quantity is saved), requires low dissolved oxygen and small aeration quantity, and is beneficial to reducing energy consumption; the anaerobic ammonia oxidation process is an autotrophic nitrogen removal process, and no additional carbon source is needed, so that the operation cost is saved.
On the basis, the membrane concentrated solution can be reduced by adopting the treatment method, and the damage of the membrane concentrated solution is finally eliminated through furnace returning incineration; meanwhile, other pollutants in the percolate of the waste incineration plant can be greatly reduced, so that the purified water meets the reuse standard of the standard factory for supplementing water of an open type circulating cooling water system in the municipal sewage recycling-industrial water quality GB/T19923-2005.
In a preferred embodiment, the biochemical degradation treatment is carried out in a Membrane Bioreactor (MBR) with a hydraulic retention time of 2-5 days and a treatment temperature of 30-35 ℃. The hydraulic retention time and treatment temperature during the biochemical degradation treatment process include, but are not limited to, the ranges set forth above, and limiting the hydraulic retention time and treatment temperature within the ranges set forth above facilitates further reducing the total nitrogen content in the leachate.
In a preferred embodiment, the membrane in the membrane bioreactor is a tubular ceramic membrane, the pore diameter of the tubular ceramic membrane is 0.1-0.8 mu m, and the membrane flux is 18-20L/(m) 2 H). The membrane with the pore diameter and the membrane flux has excellent chemical corrosion resistance and high membrane treatment efficiency; meanwhile, the membrane has a good interception function, and is beneficial to intercepting microorganisms with a long generation period in the membrane bioreactor without being taken away by a liquid phase product, so that the stability of biochemical degradation treatment is improved.
In a preferred embodiment, the biochemical degradation process is carried out in an external cross-flow membrane bioreactor, i.e. a tubular membrane is arranged outside the main body of the reactor, so that the first liquid-phase product continuously circulates between the reactor and the tubular membrane, and the water and part of soluble substances in the first liquid-phase product pass through the tubular membrane under the action of pressure, thereby obtaining the second liquid-phase product. The reactor has high membrane flux and the membrane module is convenient to maintain. In addition, because the aeration quantity required by the biochemical degradation treatment is small, the membrane surface of a Membrane Bioreactor (MBR) can not be effectively washed, pollutants in percolate are more easily deposited on a membrane sheet, and the pollution of the membrane is accelerated, so that the built-in membrane bioreactor is not suitable for being adopted.
In a preferred embodiment, a dissolved oxygen online monitoring device is adopted to detect and regulate the dissolved oxygen in real time, so that the dissolved oxygen concentration in the biochemical degradation treatment process is 0.2-0.5 mg/L. For example, the online monitoring device may be a co-blowing frequency converter. The dissolved oxygen concentration includes but is not limited to above-mentioned scope, restricts it and is favorable to reducing the energy consumption in above-mentioned scope, improves the denitrogenation effect, satisfies the processing demand of waste incineration factory filtration liquid, improves the purifying effect of filtration liquid.
In a preferred embodiment, the multi-stage anaerobic treatment comprises sequentially subjecting the primary purified leachate to a primary anaerobic treatment and a secondary anaerobic treatment, the primary anaerobic treatment being performed in a primary anaerobic reactor, the secondary anaerobic treatment being performed in a secondary anaerobic reactor, and the primary anaerobic reactor being arranged in series with the secondary anaerobic reactor; wherein, in the first-stage anaerobic treatment process, the reaction temperature is 33-38 ℃, the hydraulic retention time is 5-10 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is measured to be 85-90%; in the second-stage anaerobic treatment process, the reaction temperature is 33-38 ℃, the hydraulic retention time is 2-5 days, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 65-85%. The adoption of the first-stage anaerobic treatment reaction condition and the second-stage anaerobic reaction condition is beneficial to further reducing the COD concentration.
In order to facilitate the subsequent SNAD process treatment and avoid the influence of organic matters on the SNAD process, in a preferred embodiment, the COD concentration in the first liquid-phase product is 800-1000 mg/L, and the TN value is 1100-2600 mg/L. The activity of the SNAD process treatment process can be further and obviously improved by further limiting COD and TN in the first liquid phase product, so that the denitrification effect is greatly improved.
In a preferred embodiment, the solid-liquid separation treatment comprises, in order: s4, filtering the percolate of the waste incineration plant by using a filtering device to remove solid impurities and hair; s5, performing sedimentation treatment by using a sedimentation tank to remove soil and gravels; and S6, homogenizing by using an adjusting tank to balance and stabilize the water quality and the water quantity to obtain primary purified percolate and a first solid-phase product. Large solid particles, hair, fiber substances, silt and other suspended matters in leachate of a waste incineration plant can be removed by adopting filtering and settling treatment, so that equipment used in a subsequent treatment process is prevented from being blocked; meanwhile, by adopting the homogenization treatment process, the water quality in the regulating tank can be balanced, and the precipitation and odor of suspended particles in the percolate can be avoided.
In an optional implementation mode, the basket filter is adopted to filter the leachate of the waste incineration plant, has the advantages of good intercepting effect, compact structure, high automation degree, convenience in cleaning and maintenance and the like, and can replace the traditional solid-liquid separation device such as the existing grating.
In order to further remove large solid particles, hair, fiber substances, silt and other suspended matters in the leachate of the waste incineration plant, accelerate the sedimentation of the silt and other suspended matters, improve the sedimentation efficiency and further reduce the content of the suspended matters in the leachate, in a preferred embodiment, the screening pore size of the filtering device is 2-4 mm; the surface load of the sedimentation tank is 0.35 to 0.85m 3 /(m 2 H), the time of the sedimentation treatment is 1 to 2h.
After the biochemical degradation treatment, most of the leachate contains biodegradable organic matters and nitrogen, but the leachate still contains some difficultly degradable macromolecular organic matters, inorganic salt, turbidity, soluble solids and the like, which cannot meet the standard of pollution-free discharge and needs subsequent further treatment. In a preferred embodiment, the method for treating leachate from a waste incineration plant further comprises: nano-filtering the second liquid-phase product under the first operating pressure condition to obtain a nano-filtrate and a first concentrated solution; carrying out reverse osmosis treatment on the nanofiltration liquid under the condition of a second operation pressure to obtain first purified water and second concentrated liquid; under the condition of a third operating pressure, disc-tube reverse osmosis concentrated solution reduction treatment is respectively carried out on the first concentrated solution and the second concentrated solution to obtain second purified water and a third concentrated solution; in the process of nanofiltration treatment, the pH value of the second liquid-phase product is 6.5-6.8, the nanofiltration membrane adopted in the nanofiltration treatment is one or more of polyvinylidene fluoride membrane, polytetrafluoroethylene and ceramic, the interception molecular weight of the nanofiltration membrane is 200-1000 daltons, and the first operating pressure is 0.5-0.7 MPa.
Nanofiltration (NF) treatment has high efficiency of separating and removing substances with relative molecular weight of 200-1000 daltons and divalent or multivalent ions, can intercept macromolecular organic matters, calcium ions, magnesium ions, sulfate radicals, carbonate and other divalent ions in leachate, and enables monovalent ions (such as chloride ions) to permeate through the leachate, so that nanofiltration liquid and first concentrated solution are obtained after treatment. The Reverse Osmosis (RO) treatment can remove inorganic ions, bacteria, viruses, organic matters, colloids and other impurities in the raw water, and the reverse osmosis treatment can be used for deeply treating nano-filtrate, so that first purified water and second concentrated solution are obtained. The dish-tube type reverse osmosis concentrated solution reduction treatment can improve the water yield and reduce the yield of the concentrated solution. The pH value of the second liquid-phase product, the type and the molecular weight cut-off of the nanofiltration membrane, the second operation pressure and the third operation pressure are limited in the ranges, so that the removal rate of substances with small relative molecular weight and divalent or multivalent ions is improved, the water quality of the liquid-phase product discharged after the whole process flow is treated is improved, and the discharge standard is met. Wherein the nanofiltration membrane adopted in the nanofiltration treatment is preferably a polyvinylidene fluoride membrane; the reverse osmosis membrane used for the reverse osmosis treatment is preferably polyamide.
In order to further improve the removal rate of substances with small relative molecular weight and divalent or multivalent ions, the nanofiltration membrane preferably has a molecular weight cut-off of 150 to 300 daltons.
The above-mentioned dumpsThe treatment method of the leachate in the waste incineration plant is applicable to wider water quality range. In a preferred embodiment, the leachate from a waste incineration plant has a COD of 25000 to 75000mg/L, BOD 5 The COD value is 0.5-0.8, the ammonia nitrogen is 1000-2500 mg/L, the total hardness is 6500-11000 mg/L, the chloride ion concentration is 3000-5000 mg/L, the suspended matter concentration is 5000-10000 mg/L, and the pH value is 4-6.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the present application as claimed.
The water quality was tested by a water and wastewater quality test method (fourth edition).
Example 1
The household garbage is conveyed to a garbage incineration plant, the heat value of the household garbage is improved after 3 days of stacking fermentation, and garbage leachate is generated at the same time. The process flow shown in fig. 1 is adopted to treat the leachate of the waste incineration plant, wherein the quality of the inlet water of the leachate (inlet water) of the waste incineration plant is as follows: COD is 45000mg/L, BOD 5 The value is 26000mg/L, the ammonia nitrogen is 1600mg/L, the total hardness is 10000mg/L, the chloride ion concentration is 4000mg/L, the suspended matter concentration is 3000mg/L, and the pH value is 6.
The leachate is firstly filtered by a basket filter (the screening aperture is 2 mm) to remove impurities such as large-particle solids, hairs and the like, and then enters a vertical flow type sedimentation tank for sedimentation treatment. Wherein the time of the sedimentation process is 1h, and the surface load of the sedimentation tank is 0.5m 3 /(m 2 H). After sediment treatment is carried out to remove suspended matters such as silt in the percolate, the effluent overflows into a regulating tank for homogenization treatment. The bottom of the adjusting tank is provided with 2 stirrers for stirring treatment, wherein one stirrer is positioned at the bottom of the adjusting tank, and the other stirrer is positioned in the middle of the adjusting tank. The retention time of the inlet water of the regulating tank in the homogenizing treatment process is 10 days, and the regulating tank can store the yield of the percolate for 15 days at most. The COD concentration in the primary purified percolate obtained after the solid-liquid separation treatment is 45000mg/L and BOD 5 The COD value is 0.58 and the ammonia nitrogen is 1600mg/L.
And after the primary purified percolate is buffered, homogenized and adjusted by an adjusting tank, the primary purified percolate is sequentially pumped into a first anaerobic reactor and a second anaerobic reactor. Wherein, in the first-stage anaerobic treatment process, the reaction temperature is 35 ℃, the hydraulic retention time is 9 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is 88 percent; in the second-stage anaerobic treatment process, the reaction temperature is 35 ℃, the hydraulic retention time is 4 days, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 85%. After the multi-stage anaerobic treatment process, methane (gas phase product) and a first liquid phase product are obtained. Wherein, the methane can realize energy recovery through biogas power generation, the COD concentration of the obtained first liquid phase product is 810mg/L, and the TN value is 1800mg/L.
And (3) carrying out SNAD process treatment, namely biochemical degradation treatment, by adopting an up-flow sludge bed external cross-flow tubular membrane reactor to obtain a second liquid phase product and nitrogen. The aperture of the tubular ceramic membrane in the reactor is 0.2 mu m, and the membrane flux is 20L/(m) 2 H). The hydraulic retention time in the membrane bioreactor is 4 days, and the treatment temperature is 35 ℃; meanwhile, the concentration of dissolved oxygen in the membrane bioreactor is 0.2mg/L.
Nano-filtering the second liquid-phase product by using a SUEZ DK8040F30 membrane under the pressure of 0.5MPa, wherein the molecular weight cut-off is 150-300 daltons, and obtaining nano-filtrate and first concentrated solution; wherein the pH of the second liquid phase product is 6.8 and the nanofiltration treatment temperature is 25 ℃.
And (3) performing reverse osmosis treatment on the nanofiltration solution by using a Dow SW30HRLE-400 membrane under the pressure condition of 1.5MPa to obtain first purified water and second concentrated solution.
The test results show that the water quality parameters of the first purified water are as follows: COD is 5mg/L, TN value is 10mg/L, total hardness is 15mg/L, chloride ion concentration is 210mg/L, and can meet the recycling standard.
And under the pressure condition of 3.5MPa, performing disc-tube reverse osmosis concentrated solution reduction treatment on the first concentrated solution and the second concentrated solution respectively to obtain second purified water and third concentrated solution.
The total yield of the first purified water and the second purified water is 85% through testing, and the concentrated solution is reduced to 15%; the water quality parameters of the second purified water are as follows: COD is 5mg/L, TN value is 10mg/L, total hardness is 15mg/L, chloride ion concentration is 210mg/L, and the second purified water can meet the recycling standard.
Example 2
The difference from example 1 is that: the dissolved oxygen concentration in the external cross-flow tubular membrane reactor of the upflow sludge blanket is 0.5mg/L.
Example 3
The difference from example 1 is that: the dissolved oxygen concentration in the external cross-flow tubular membrane reactor of the upflow sludge blanket is 0.8mg/L.
Example 4
The difference from example 1 is that: the hydraulic retention time in the external cross-flow tubular membrane reactor of the upflow sludge blanket is 2 days, and the treatment temperature in the process of biochemical degradation treatment (SNAD process treatment) is 35 ℃.
Example 5
The difference from example 1 is that: the hydraulic retention time in the external cross-flow tubular membrane reactor of the upflow sludge blanket is 5 days, and the treatment temperature in the process of biochemical degradation treatment (SNAD process treatment) is 30 ℃.
Example 6
The difference from example 1 is that: the hydraulic retention time in the external cross-flow tubular membrane reactor of the upflow sludge blanket is 1 day, and the treatment temperature in the process of biochemical degradation treatment (SNAD process treatment) is 25 ℃. The hydraulic retention time is too short and the temperature is too low to start successfully.
Example 7
The difference from example 1 is that: the aperture of the tubular ceramic membrane is 0.1 mu m, and the membrane flux is 18L/(m) 2 ·h)。
Example 8
The difference from example 1 is that: the pore diameter of the tubular ceramic membrane is 0.8 μm.
Example 9
The difference from example 1 is that: the aperture of the tubular ceramic membrane is 1 mu m, and the membrane flux is 25L/(m) 2 ·h)。
Example 10
The difference from example 1 is that: in the first-stage anaerobic treatment process, the reaction temperature is 33 ℃, the hydraulic retention time is 5 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is measured to be 85%; in the second-stage anaerobic treatment process, the reaction temperature is 33 ℃, the hydraulic retention time is 2 days, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 65%.
Example 11
The difference from example 1 is that: in the first-stage anaerobic treatment process, the reaction temperature is 38 ℃, the hydraulic retention time is 10 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is 88 percent; in the second-stage anaerobic treatment process, the reaction temperature is 38 ℃, the hydraulic retention time is 5 days, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 85%.
The longer hydraulic retention time and higher temperature of the anaerobic process in example 11 did not significantly improve COD removal compared to example 1. Under the same conditions, higher temperatures require more energy consumption in order to ensure a longer hydraulic retention time, requiring a larger building volume.
Example 12
The difference from example 1 is that: in the first-stage anaerobic treatment process, the reaction temperature is 25 ℃, the hydraulic retention time is 2 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is measured to be 30%; in the second-stage anaerobic treatment process, the reaction temperature is 25 ℃, the hydraulic retention time is 1 day, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 20%. The COD concentration of the first liquid phase product is 25200mg/L, and the TN value is 1850mg/L.
When the process conditions are adopted, the system cannot normally operate, and the effluent cannot meet the process requirements of the subsequent membrane.
Comparative example 1
The difference from example 1 is that: the conventional single-stage (one-stage) anaerobic treatment is adopted, wherein the reaction temperature is 35 ℃, and the hydraulic retention time is 9 days. After the first-order anaerobic treatment process is finished, the COD removal rate is 88 percent and the COD concentration is 5400mg/L.
With the above process conditions, high concentrations of COD resulted in unsuccessful start-up of the SNAD system.
Comparative example 2
The difference from example 1 is that: the dissolved oxygen amount in the biochemical degradation treatment (SNAD process treatment) process is 2mg/L.
By adopting the process conditions, as anaerobic ammonium oxidation bacteria of a main microorganism in the SNAD process are absolute anaerobic bacteria, the bacteria can not grow due to overhigh dissolved oxygen, and the SNAD process can not be started successfully.
Comparative example 3
The difference from example 1 is that: the immersed membrane bioreactor is adopted for treatment.
The external cross-flow type membrane bioreactor realizes material circulation cross flow by pressurizing through a circulating pump, and materials flow in a disordered manner inside the membrane to scour the surface of the membrane and relieve membrane pollution; submerged membrane bioreactors generally mitigate membrane fouling by aeration scouring the membrane surface; because the SNAD process has small aeration amount, the sludge is quickly covered and accumulated on the surface of the membrane due to insufficient membrane surface scouring force when the submerged membrane bioreactor is adopted for treatment, the blockage of the membrane is easily caused, the membrane washing frequency is increased, and the water production process is influenced.
The water quality parameters of the primary purified water obtained in all the above embodiments of the present application are shown in table 1.
TABLE 1
| Water quality parameter | COD(mg/L) | TN(mg/L) | Total hardness (mg/L) | Chloride ion concentration (mg/L) |
| Example 1 | 5 | 10 | 15 | 210 |
| Example 2 | 25 | 15 | 15 | 210 |
| Example 3 | 25 | 25 | 15 | 210 |
| Example 4 | 35 | 35 | 15 | 210 |
| Example 5 | 5 | 20 | 15 | 210 |
| Example 6 | - | - | - | - |
| Example 7 | 5 | 10 | 15 | 210 |
| Example 8 | 23 | 19 | 15 | 210 |
| Example 9 | 44 | 35 | 15 | 210 |
| Example 10 | 66 | 70 | 15 | 210 |
| Example 11 | 5 | 10 | 15 | 210 |
| Example 12 | - | - | - | - |
| Comparative example 1 | - | - | - | - |
| Comparative example 2 | - | - | - | - |
| Comparative example 3 | 5 | 10 | 15 | 110 |
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
comparative examples 1 to 3 show that the dissolved oxygen concentration includes but is not limited to the preferred range of the present application, and the limitation of the dissolved oxygen concentration within the preferred range of the present application is beneficial to reducing energy consumption, improving denitrification effect, meeting the treatment requirement of the leachate of the waste incineration plant, and improving the purification effect of the leachate.
Comparing example 1 with comparative example 1, it can be seen that, by performing multistage anaerobic treatment on the primary purified leachate, on the first hand, compared with single-stage anaerobic treatment, the organic matter in the leachate of a waste incineration plant can be further degraded by adopting a multistage anaerobic treatment process, so that the COD concentration is reduced in a targeted manner; in the second aspect, the multistage anaerobic treatment is beneficial to improving the yield of the biogas, the subsequent recycling and reutilization and improving the economic benefit by improving the removal rate of organic matters; in the third aspect, the multistage anaerobic treatment can remove organic matters to the maximum extent, and the subsequent process is prevented from being influenced by organic matter inhibition.
Comparing examples 1 to 3 and comparative example 2, it can be seen that under the preferred dissolved oxygen condition of the present application, performing biodegradation treatment (SNAD process treatment) under the coupling action of nitrosobacteria, anammox bacteria and heterotrophic denitrifying bacteria can effectively reduce the total nitrogen content in the leachate, and the process only performs a nitrosation process (without performing a nitrification process, saving about 25% of aeration) and requires a low dissolved oxygen content, a small aeration amount, which is beneficial to reducing energy consumption; the anaerobic ammonia oxidation process is an autotrophic nitrogen removal process, no additional carbon source is needed, and the operation cost is saved.
The external cross-flow type membrane bioreactor realizes material circulation cross flow by pressurizing through a circulating pump, and materials flow in a disordered manner inside the membrane to scour the surface of the membrane and relieve membrane pollution; submerged membrane bioreactors generally mitigate membrane fouling by aeration to scour the membrane surfaces. Comparing example 1 with comparative example 3, it can be seen that the SNAD process requires a small amount of aeration and cannot effectively flush the membrane surface of the membrane bioreactor, and the contaminants in the leachate are more likely to deposit on the tubular membrane, accelerating the membrane fouling, so that it is not suitable to use a built-in membrane bioreactor.
Comparing examples 1, 4 and 6, it is understood that the hydraulic retention time and treatment temperature during treatment of the SNAD process include, but are not limited to, the preferred ranges disclosed herein, and that limiting the same to the preferred ranges disclosed herein facilitates further reduction of the total nitrogen content in the leachate.
Comparing examples 1, 7 to 9, it can be seen that limiting the pore size and membrane flux of the tubular ceramic membrane to the preferred range of the present application has better retention effect than other ranges, which is beneficial to retain microorganisms with longer generation period in the membrane bioreactor without being carried away by liquid phase product, thereby improving the stability of the SNAD process.
Comparing examples 1, 11 to 12, it can be seen that the longer hydraulic retention time and higher temperature of the anaerobic process did not significantly improve the COD removal rate. However, under the same conditions, higher temperatures require more energy consumption in order to ensure longer hydraulic retention times requiring greater building volumes.
It is noted that the terms first, second and the like in the description and in the claims of the present application are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the terms so used are interchangeable under appropriate circumstances such that the embodiments of the application described herein are, for example, capable of operation in sequences other than those described or illustrated herein.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for treating leachate of a waste incineration plant is characterized by comprising the following steps:
s1, performing solid-liquid separation treatment on the leachate of the waste incineration plant to obtain primary purified leachate and a first solid-phase product;
s2, performing multistage anaerobic treatment on the primary purified percolate to obtain a gas-phase product, a first liquid-phase product and a second solid-phase product;
s3, performing biochemical degradation treatment on the first liquid-phase product under the condition that the dissolved oxygen amount is 0.2-0.8 mg/L to obtain nitrogen and a second liquid-phase product;
the biochemical degradation process is a simultaneous shortcut nitrification anaerobic ammonia oxidation denitrification process, the participating microorganisms comprise nitrosobacteria, anaerobic ammonia oxidation bacteria and heterotrophic denitrifying bacteria, and the biochemical degradation process comprises the nitrosobacteria nitrosation process, the anaerobic ammonia oxidation process and the heterotrophic denitrifying bacteria denitrification process.
2. The method for treating leachate of a waste incineration plant according to claim 1, wherein the biochemical degradation treatment process is performed in a membrane bioreactor, the hydraulic retention time in the membrane bioreactor is 2 to 5 days, and the treatment temperature is 30 to 35 ℃.
3. The method for treating leachate from a waste incineration plant of claim 2, wherein the membrane in the membrane bioreactor is a tubular ceramic membrane, the pore size of the tubular ceramic membrane is 0.1 to 0.8 μm, and the membrane flux is 18 to 20L/(m) 2 ·h)；
Preferably, the biochemical degradation treatment process is carried out in an external cross-flow membrane bioreactor.
4. The method for treating leachate of a waste incineration plant according to claim 1, wherein the dissolved oxygen is detected and regulated in real time by using a dissolved oxygen on-line monitoring device, so that the dissolved oxygen concentration in the biochemical degradation treatment process is 0.2-0.5 mg/L.
5. The method of any of claims 1 to 4, wherein the multistage anaerobic treatment comprises sequentially subjecting the primary purified leachate to a primary anaerobic treatment and a secondary anaerobic treatment, the primary anaerobic treatment being performed in a primary anaerobic reactor, the secondary anaerobic treatment being performed in a secondary anaerobic reactor, and the primary anaerobic reactor being arranged in series with the secondary anaerobic reactor;
wherein, in the first-stage anaerobic treatment process, the reaction temperature is 33-38 ℃, the hydraulic retention time is 5-10 days, and after the first-stage anaerobic treatment process is finished, the COD removal rate is measured to be 85-90%;
in the second-stage anaerobic treatment process, the reaction temperature is 33-38 ℃, the hydraulic retention time is 2-5 days, and after the second-stage anaerobic treatment process is finished, the COD removal rate is measured to be 65-85%.
6. The method for treating leachate of a waste incineration plant according to claim 5, wherein the COD concentration in the first liquid phase product is 800-1000 mg/L and the TN value is 1100-2600 mg/L.
7. The method for treating leachate of a waste incineration plant according to claim 1, wherein the solid-liquid separation treatment sequentially comprises:
s4, filtering the percolate of the waste incineration plant by using a filtering device to remove solid impurities and hair;
s5, carrying out sedimentation treatment by adopting a sedimentation tank to remove soil and sandstone;
and S6, homogenizing by using an adjusting tank to obtain the primary purification percolate and the first solid-phase product.
8. The method for treating leachate of a waste incineration plant according to claim 7, wherein the screening pore size of the filtering device is 2-4 mm; the surface load of the sedimentation tank is 0.35-0.85 m 3 /(m 2 H), the time of the sedimentation treatment is 1-2 h.
9. The method for treating leachate of a waste incineration plant according to any of the claims 1 to 8, wherein the method for treating leachate of a waste incineration plant further comprises:
nano-filtering the second liquid-phase product under a first operating pressure condition to obtain a nano-filtrate and a first concentrated solution;
under the condition of a second operating pressure, carrying out reverse osmosis treatment on the nano filtrate to obtain first purified water and second concentrated solution;
under the condition of a third operating pressure, disc-tube reverse osmosis concentrated solution reduction treatment is respectively carried out on the first concentrated solution and the second concentrated solution to obtain second purified water and a third concentrated solution;
in the nanofiltration treatment process, the pH of the second liquid-phase product is 6.5-6.8, the nanofiltration membrane adopted in the nanofiltration treatment is one or more of polyvinylidene fluoride membrane, polytetrafluoroethylene and ceramic, the cut-off molecular weight of the nanofiltration membrane is 200-1000 daltons, and the first operating pressure is 0.5-0.7 MPa; preferably, the molecular weight cut-off of the nanofiltration membrane is 150-300 daltons;
the reverse osmosis membrane adopted in the reverse osmosis treatment is one or more of polyamide, acetate fiber and polyamide, the reverse osmosis membrane can separate ions with the particle size of less than 1nm, and the second operating pressure is 1-3 MPa;
the third operating pressure is 3-6 MPa.
10. The method of claim 1, wherein the leachate from a waste incineration plant has a COD of 25000-75000 mg/L, a BOD5/COD value of 0.5-0.8, ammonia nitrogen of 1000-2500 mg/L, a total hardness of 6500-11000 mg/L, a chloride ion concentration of 3000-5000 mg/L, a suspended matter concentration of 5000-10000 mg/L, and a pH of 4-6.
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