CN114149146A - Anaerobic ammonia oxidation method for landfill leachate sewage - Google Patents
Anaerobic ammonia oxidation method for landfill leachate sewage Download PDFInfo
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- CN114149146A CN114149146A CN202111477864.9A CN202111477864A CN114149146A CN 114149146 A CN114149146 A CN 114149146A CN 202111477864 A CN202111477864 A CN 202111477864A CN 114149146 A CN114149146 A CN 114149146A
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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
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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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
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- 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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- 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
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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
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F7/00—Aeration of stretches of water
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Abstract
The invention discloses an anaerobic ammonia oxidation method for landfill leachate sewage, which comprises the following steps: s1, collecting garbage percolate, collecting the garbage percolate generated in a garbage landfill area through a collection pipeline, separating solid impurities from the collected garbage percolate through a stainless steel fine grid arranged at an inlet of an adjusting tank of a sewage treatment plant, then feeding the separated solid impurities into a percolate adjusting tank, heating the percolate in the adjusting tank to obtain uniform homogeneity, S2, heating the percolate, starting a garbage percolate heating device in the adjusting tank to heat, controlling a switch of a heater through a temperature controller, and enabling the temperature of the garbage percolate to reach 33-37 ℃ after the garbage percolate to be treated is heated and subjected to heat exchange.
Description
Technical Field
The invention discloses an anaerobic ammonium oxidation method for landfill leachate sewage, belonging to the technical field of landfill leachate treatment.
Background
In recent years, along with the increasing of the output of urban solid wastes, the landfill method gradually becomes the most widely applied treatment and disposal method in the world, the leachate generated by landfill can seriously pollute surface water or underground water if no effective measures are taken for control, the landfill leachate has the water quality characteristics of complex components, large change of water quality and water quantity, high concentration of organic matters and ammonia nitrogen, imbalance of microorganism nutrient elements and the like, so the treatment of the landfill leachate becomes one of the problems which are not solved in the international range, the serious shortage of organic carbon sources is a barrier which can not improve the denitrification efficiency of the leachate in the later period, and the additional organic carbon sources can greatly increase the cost of sewage denitrification, therefore, a more effective denitrification device and a more effective denitrification method need to be provided, the traditional sewage biological denitrification converts NH4+ -N into N03-N through nitrification, and then converts N03-N into nitrogen to escape from water through denitrification, in the denitrification stage, N03-N is used as an electron acceptor, organic matters are used as an electron donor, ammonia nitrogen is converted into nitrogen to complete biological denitrification, but for the denitrification of the late landfill leachate with high ammonia nitrogen and low organic matter concentration, the C/N ratio is usually lower than 4, and the traditional biological denitrification efficiency can only reach about 10% due to serious shortage of organic carbon sources.
The phenomenon of anammox is well noticed since 1995 report, because in the anammox process, anammox bacteria can convert ammonia nitrogen and nitrite nitrogen into nitrogen without oxygen participation, and the whole process completely belongs to an autotrophic process, compared with the traditional nitrification and denitrification process, the anammox process can save 50% of oxygen supply cost without additional carbon source, thereby greatly reducing the treatment cost and the capital construction cost of sewage treatment, however, garbage leachate contains a large amount of organic matters, most of the organic matters in the leachate are difficult to degrade, and some of the leachate have toxicity, can generate toxic action on anammox bacteria, and can generate adverse effect on anammox reaction.
Disclosure of Invention
The invention aims to solve the defects and provide an anaerobic ammonia oxidation method for landfill leachate sewage.
The anaerobic ammonia oxidation method for landfill leachate sewage comprises the following steps:
s1, collecting the garbage leachate generated in the garbage landfill area through a collection pipeline, separating solid impurities from the collected garbage leachate through a stainless steel fine grid arranged at the inlet of an adjusting tank of a sewage treatment plant, and then feeding the garbage leachate into a leachate adjusting tank, wherein the leachate is homogenized and equalized in the adjusting tank;
s2, heating the leachate, starting a landfill leachate heating device in the regulating tank to heat, and controlling the on-off of a heater through a temperature controller to ensure that the temperature of the landfill leachate reaches 33-37 ℃ after the landfill leachate to be treated is heated and subjected to heat exchange;
s3, acidifying the sewage, wherein the heated effluent of the regulating reservoir flows into a hydrolysis acidification pool, hydrolysis acidification bacteria in the hydrolysis acidification pool hydrolyze and acidify a long-chain high-molecular polymer into organic micromolecule alcohol or acid with stronger biodegradability, and part of heterocyclic organic matters which are not biochemical or have weaker biodegradability can be degraded into biochemical organic molecules, so that the BOD5/CODCr value of organic pollutants in the sewage is increased;
s4, anaerobic pretreatment, namely putting an activated anaerobic enhanced microbial inoculum and/or a composite denitrification microbial inoculum with a preset volume concentration into the acidified wastewater for anaerobic/anoxic reaction treatment for a preset time, wherein the volume concentration of the anaerobic enhanced microbial inoculum is 0.03-0.1%, and the anaerobic enhanced microbial inoculum is one or more of enterococcus, yeast and clostridium butyricum;
s5, aerating, introducing the wastewater into an aerating device after anaerobic effluent, adding an aerobic strengthening microbial inoculum and an autotrophic nitrifying microbial inoculum which are activated at a preset volume concentration, carrying out COD removal and ammonia nitrogen degradation treatment on the wastewater, and controlling the reaction time of the aeration treatment to regulate the proportion of COD, ammonia nitrogen and nitrite;
s6, performing enrichment treatment, namely allowing the aerated effluent to enter an enrichment device of a sewage treatment plant for standing reaction until red zoogloea appears, and completing the enrichment of anaerobic ammonium oxidation bacteria until the total nitrogen removal rate is stable;
s7, inoculating sewage containing anaerobic oxidizing bacteria into an anaerobic baffle plate reactor of a sewage plant under anaerobic conditions, introducing ammonia nitrogen and nitrite nitrogen with the concentration of 9-21 mg/L and the pH of 7.8-8.3 into the anaerobic baffle plate reactor through a water inlet storage bottle, controlling the water inflow by using a constant-current peristaltic pump positioned between the water inlet storage bottle and the anaerobic baffle plate reactor so as to control the hydraulic retention time to be 24-48 h, controlling the reaction temperature to be 25-30 ℃, discharging the treated wastewater from a water outlet, and discharging gas from an exhaust port until the anaerobic oxidizing bacteria in the anaerobic baffle plate reactor become dominant flora and the removal rate of the ammonia nitrogen and the nitrite nitrogen reaches 80% after 5 days;
s8, after the anaerobic baffle plate reactor is successfully started, adding short-cut nitrified sludge, anaerobic ammonium oxidation sludge, short-cut denitrifying anaerobic ammonium oxidation sludge and the sewage obtained in the step S7 into each anaerobic baffle plate reactor, and controlling the sludge concentration of mixed liquor of each reactor after adding to be respectively sludge concentration MLSS (6000 +/-300 mg/L), MLVSS (4500 +/-350 mg/L), and f (MLVSS/MLSS) to be 70%;
s9, making the percolate enter a two-stage A/O biochemical reaction tank after anaerobic treatment by an anaerobic baffle plate reactor, and fully removing organic matters and denitriding the percolate in the biochemical reaction tank;
s10, lifting the percolate subjected to biochemical treatment into an ultrafiltration system through a lifting pump, intercepting colloids, particles and substances with relatively high molecular weight in water under the action of pressure by using a pressure active membrane in the ultrafiltration system, and separating water and relatively small solute particles through the membrane;
s11, discharging the treated leachate, and closing the sewage treatment equipment.
Preferably, in the step S4, the volume concentration of the composite denitrification microbial inoculum is 0.01-0.1%; the composite denitrifying microbial agent is one or more of bacillus pumilus, bacillus cereus and bacillus thuringiensis.
Preferably, in the step S5, the aeration treatment reaction time is 11-95 h, the reaction conditions are controlled such that the effluent COD is less than 110mg/L, and the ratio of ammonia nitrogen to nitrite is 1: 1-1: 1.2.
Preferably, in the step S6, the number of water intakes per day of the enrichment device is 2-10, the reaction time of single standing is 2-6 h, and the enrichment time is 30-60 days.
Preferably, in the S7, the anaerobic baffled reactor is 40cm long, 14cm wide, 30cm high, 27.5cm effective height, 15.4L effective volume and 45 degrees of baffled corner.
Preferably, in step S8, in order to avoid excessive impact of the landfill leachate on the sludge, the system is stably operated for 30d in an artificial water distribution manner at the initial start-up stage, and then the proportion of the late-stage landfill leachate in the water distribution is increased by a concentration gradient of 20% every 10d, so that the sludge gradually adapts to the late-stage landfill leachate, and the reactor acclimates for 80 d; wherein each liter of water is composed of 997.5ml of tap water, 943mg of (NH4)2SO4, 1300mg of NaNO2, 8mg of KH2PO4, 4.48mg of CaCl 2. H2O, 240mg of MgSO4.7H2O, 1000mg of KHCO3, 1.25ml of trace element I and 1.25ml of trace element II; 1L of trace elements I comprises the following components: 6.369g EDTA, 9.14g FeSO4.7H2O, 1L microelement II component including 19.106g EDTA, 0.014g H3BO4, 0.99g MnCl2.4H2O, 0.25g CuSO4.5H2O, 0.43g ZnSO4.7H2O, 0.19g NiCl2.6H2O, 0.22g NaMoO 4.2H2O.
Preferably, in step S9, the anaerobic baffled reactor is provided with a heating system, and the volume of the two-stage a/O biochemical reaction tank is greater than 20.4L.
Preferably, in step S10, the pressure active membrane of the ultrafiltration system can filter particles with a molecular weight of 80-1000.
Compared with the prior art, the invention has the following beneficial effects:
according to the anaerobic ammonium oxidation method for landfill leachate sewage, the leachate waste water at different stages is treated by adding the microbial agent, so that on one hand, required enrichment culture conditions can be provided for anaerobic ammonium oxidation bacteria, and COD (chemical oxygen demand) and nitrite ammonia nitrogen in the effluent reach the requirements of enrichment strains; on the other hand, the method can improve the growth rate of the bacteria and the tolerance performance of the bacteria by performing the synergistic acclimation effect on the target strains in the enrichment process, simultaneously ensure that the reduction rate of the total nitrogen of the effluent reaches 95 percent, greatly improve the removal rate of the total nitrogen in the biological denitrification process, save 50 percent of oxygen supply cost compared with the traditional nitrification denitrification process, do not need additional carbon sources, greatly reduce the treatment cost and the infrastructure cost of sewage treatment, simultaneously have an ultrafiltration system, solve the defects that the sewage treated by a biochemical reaction tank in the prior art is directly treated by a disc tube type reverse osmosis membrane, ensure that the treatment load of the reverse osmosis membrane is higher and the service life is short, solve the problems that the nitrite nitrogen in the anaerobic ammonia oxidation reaction is difficult to stably generate and the total nitrogen is removed, reduce the toxic action, shorten the reaction flow and the reaction time in the biochemical denitrification process of the landfill leachate, the volume of the reaction tank and the aeration quantity of the aerobic tank are saved, the biological denitrification efficiency of the landfill leachate is improved, a large amount of residual sludge generated by the traditional biological denitrification is avoided, the treatment cost of the landfill leachate is reduced, and the method has important significance for the engineering of the related energy-saving and low-carbon high-efficiency denitrification technology.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The anaerobic ammonia oxidation method for landfill leachate sewage comprises the following steps:
s1, collecting the garbage leachate generated in the garbage landfill area through a collection pipeline, separating solid impurities from the collected garbage leachate through a stainless steel fine grid arranged at the inlet of an adjusting tank of a sewage treatment plant, and then feeding the garbage leachate into a leachate adjusting tank, wherein the leachate is homogenized and equalized in the adjusting tank;
s2, heating the leachate, turning on a landfill leachate heating device in the regulating tank to heat, and controlling the on-off of a heater through a temperature controller to ensure that the temperature of the landfill leachate to be treated reaches 33-37 ℃ after heating and heat exchange
S3, acidifying the sewage, wherein the heated effluent of the regulating reservoir flows into a hydrolysis acidification pool, hydrolysis acidification bacteria in the hydrolysis acidification pool hydrolyze and acidify a long-chain high-molecular polymer into organic micromolecule alcohol or acid with stronger biodegradability, and part of heterocyclic organic matters which are not biochemical or have weaker biodegradability can be degraded into biochemical organic molecules, so that the BOD5/CODCr value of organic pollutants in the sewage is increased;
s4, anaerobic pretreatment, namely putting an activated anaerobic enhanced microbial inoculum and/or a composite denitrification microbial inoculum with a preset volume concentration into the acidified wastewater for anaerobic/anoxic reaction treatment for a preset time, wherein the volume concentration of the anaerobic enhanced microbial inoculum is 0.03-0.1%, and the anaerobic enhanced microbial inoculum is one or more of enterococcus, yeast and clostridium butyricum;
s5, aerating, introducing the wastewater into an aerating device after anaerobic effluent, adding an aerobic strengthening microbial inoculum and an autotrophic nitrifying microbial inoculum which are activated at a preset volume concentration, carrying out COD removal and ammonia nitrogen degradation treatment on the wastewater, and controlling the reaction time of the aeration treatment to regulate the proportion of COD, ammonia nitrogen and nitrite;
s6, performing enrichment treatment, namely allowing the aerated effluent to enter an enrichment device of a sewage treatment plant for standing reaction until red zoogloea appears, and completing the enrichment of anaerobic ammonium oxidation bacteria until the total nitrogen removal rate is stable;
s7, inoculating sewage containing anaerobic oxidizing bacteria into an anaerobic baffle plate reactor of a sewage plant under anaerobic conditions, introducing ammonia nitrogen and nitrite nitrogen with the concentration of 9-21 mg/L and the pH of 7.8-8.3 into the anaerobic baffle plate reactor through a water inlet storage bottle, controlling the water inflow by using a constant-current peristaltic pump positioned between the water inlet storage bottle and the anaerobic baffle plate reactor so as to control the hydraulic retention time to be 24-48 h, controlling the reaction temperature to be 25-30 ℃, discharging the treated wastewater from a water outlet, and discharging gas from an exhaust port until the anaerobic oxidizing bacteria in the anaerobic baffle plate reactor become dominant flora and the removal rate of the ammonia nitrogen and the nitrite nitrogen reaches 80% after 5 days;
s8, after the anaerobic baffle plate reactor is successfully started, adding short-cut nitrified sludge, anaerobic ammonium oxidation sludge, short-cut denitrifying anaerobic ammonium oxidation sludge and the sewage obtained in the step S7 into each anaerobic baffle plate reactor, and controlling the sludge concentration of mixed liquor of each reactor after adding to be respectively sludge concentration MLSS (6000 +/-300 mg/L), MLVSS (4500 +/-350 mg/L), and f (MLVSS/MLSS) to be 70%;
s9, making the percolate enter a two-stage A/O biochemical reaction tank after anaerobic treatment by an anaerobic baffle plate reactor, and fully removing organic matters and denitriding the percolate in the biochemical reaction tank;
s10, lifting the percolate subjected to biochemical treatment into an ultrafiltration system through a lifting pump, intercepting colloids, particles and substances with relatively high molecular weight in water under the action of pressure by using a pressure active membrane in the ultrafiltration system, and separating water and relatively small solute particles through the membrane;
s11, discharging the treated leachate, and closing the sewage treatment equipment.
Preferably, in the step S4, the volume concentration of the composite denitrification microbial inoculum is 0.01-0.1%; the composite denitrifying microbial agent is one or more of bacillus pumilus, bacillus cereus and bacillus thuringiensis.
Preferably, in the step S5, the aeration treatment reaction time is 11-95 h, the reaction conditions are controlled such that the effluent COD is less than 110mg/L, and the ratio of ammonia nitrogen to nitrite is 1: 1-1: 1.2.
Preferably, in the step S6, the number of water intakes per day of the enrichment device is 2-10, the reaction time of single standing is 2-6 h, and the enrichment time is 30-60 days.
Preferably, in the S7, the anaerobic baffled reactor is 40cm long, 14cm wide, 30cm high, 27.5cm effective height, 15.4L effective volume and 45 degrees of baffled corner.
Preferably, in step S8, in order to avoid excessive impact of the landfill leachate on the sludge, the system is stably operated for 30d in an artificial water distribution manner at the initial start-up stage, and then the proportion of the late-stage landfill leachate in the water distribution is increased by a concentration gradient of 20% every 10d, so that the sludge gradually adapts to the late-stage landfill leachate, and the reactor acclimates for 80 d; wherein each liter of water is composed of 997.5ml of tap water, 943mg of (NH4)2SO4, 1300mg of NaNO2, 8mg of KH2PO4, 4.48mg of CaCl 2. H2O, 240mg of MgSO4.7H2O, 1000mg of KHCO3, 1.25ml of trace element I and 1.25ml of trace element II; 1L of trace elements I comprises the following components: 6.369g EDTA, 9.14g FeSO4.7H2O, 1L microelement II component including 19.106g EDTA, 0.014g H3BO4, 0.99g MnCl2.4H2O, 0.25g CuSO4.5H2O, 0.43g ZnSO4.7H2O, 0.19g NiCl2.6H2O, 0.22g NaMoO 4.2H2O.
Preferably, in step S9, the anaerobic baffled reactor is provided with a heating system, and the volume of the two-stage a/O biochemical reaction tank is greater than 20.4L.
Preferably, in step S10, the pressure active membrane of the ultrafiltration system can filter particles with a molecular weight of 80-1000.
The first embodiment is as follows:
the anaerobic ammonia oxidation method for landfill leachate sewage comprises the following steps:
s1, collecting the garbage leachate generated in the garbage landfill area through a collection pipeline, separating solid impurities from the collected garbage leachate through a stainless steel fine grid arranged at the inlet of an adjusting tank of a sewage treatment plant, and then feeding the garbage leachate into a leachate adjusting tank, wherein the leachate is homogenized and equalized in the adjusting tank;
s2, heating the leachate, turning on a landfill leachate heating device in the regulating tank to heat, and controlling the on-off of a heater through a temperature controller to ensure that the temperature of the landfill leachate to be treated reaches 33-37 ℃ after heating and heat exchange
S3, acidifying the sewage, wherein the heated effluent of the regulating reservoir flows into a hydrolysis acidification pool, hydrolysis acidification bacteria in the hydrolysis acidification pool hydrolyze and acidify a long-chain high-molecular polymer into organic micromolecule alcohol or acid with stronger biodegradability, and part of heterocyclic organic matters which are not biochemical or have weaker biodegradability can be degraded into biochemical organic molecules, so that the BOD5/CODCr value of organic pollutants in the sewage is increased;
s4, anaerobic pretreatment, namely putting an activated anaerobic enhanced microbial inoculum and/or a composite denitrification microbial inoculum with a preset volume concentration into the acidified wastewater for anaerobic/anoxic reaction treatment for a preset time, wherein the volume concentration of the anaerobic enhanced microbial inoculum is 0.03-0.1%, and the anaerobic enhanced microbial inoculum is one or more of enterococcus, yeast and clostridium butyricum;
s5, aerating, introducing the wastewater into an aerating device after anaerobic effluent, adding an aerobic strengthening microbial inoculum and an autotrophic nitrifying microbial inoculum which are activated at a preset volume concentration, carrying out COD removal and ammonia nitrogen degradation treatment on the wastewater, and controlling the reaction time of the aeration treatment to regulate the proportion of COD, ammonia nitrogen and nitrite;
s6, performing enrichment treatment, namely allowing the aerated effluent to enter an enrichment device of a sewage treatment plant for standing reaction until red zoogloea appears, and completing the enrichment of anaerobic ammonium oxidation bacteria until the total nitrogen removal rate is stable;
s7, inoculating sewage containing anaerobic oxidizing bacteria into an anaerobic baffle plate reactor of a sewage plant under anaerobic conditions, introducing ammonia nitrogen and nitrite nitrogen with the concentration of 9-21 mg/L and the pH of 7.8-8.3 into the anaerobic baffle plate reactor through a water inlet storage bottle, controlling the water inflow by using a constant-current peristaltic pump positioned between the water inlet storage bottle and the anaerobic baffle plate reactor so as to control the hydraulic retention time to be 24-48 h, controlling the reaction temperature to be 25-30 ℃, discharging the treated wastewater from a water outlet, and discharging gas from an exhaust port until the anaerobic oxidizing bacteria in the anaerobic baffle plate reactor become dominant flora and the removal rate of the ammonia nitrogen and the nitrite nitrogen reaches 80% after 5 days;
s8, after the anaerobic baffle plate reactor is successfully started, adding short-cut nitrified sludge, anaerobic ammonium oxidation sludge, short-cut denitrifying anaerobic ammonium oxidation sludge and the sewage obtained in the step S7 into each anaerobic baffle plate reactor, and controlling the sludge concentration of mixed liquor of each reactor after adding to be respectively sludge concentration MLSS (6000 +/-300 mg/L), MLVSS (4500 +/-350 mg/L), and f (MLVSS/MLSS) to be 70%;
s9, making the percolate enter a two-stage A/O biochemical reaction tank after anaerobic treatment by an anaerobic baffle plate reactor, and fully removing organic matters and denitriding the percolate in the biochemical reaction tank;
s10, lifting the percolate subjected to biochemical treatment into an ultrafiltration system through a lifting pump, intercepting colloids, particles and substances with relatively high molecular weight in water under the action of pressure by using a pressure active membrane in the ultrafiltration system, and separating water and relatively small solute particles through the membrane;
s11, discharging the treated leachate, and closing the sewage treatment equipment.
In this embodiment, in the step S4, the volume concentration of the composite denitrification microbial inoculum is 0.01-0.1%; the composite denitrifying microbial agent is one or more of bacillus pumilus, bacillus cereus and bacillus thuringiensis.
In this embodiment, in the step S5, the aeration treatment reaction time is 11-95 h, the reaction conditions are controlled such that the effluent COD is less than 110mg/L, and the ratio of ammonia nitrogen to nitrite is 1: 1-1: 1.2.
In this embodiment, in the step S6, the number of water intakes per day of the enrichment apparatus is 2-10, the reaction time of single standing is 2-6 h, and the enrichment time is 30-60 days.
In the present embodiment, in the S7, the anaerobic baffled reactor is 40cm long, 14cm wide, 30cm high, 27.5cm effective height, 15.4L effective volume and 45 degrees of baffled corner.
In this embodiment, in step S8, in order to avoid excessive impact of the landfill leachate on the sludge, the system is stably operated for 30d in an artificial water distribution manner at the initial start-up stage, and then the proportion of the late-stage landfill leachate in the water distribution is increased by a concentration gradient of 20% every 10d, so that the sludge gradually adapts to the late-stage landfill leachate, and the reactor acclimates for 80 d; wherein each liter of water is composed of 997.5ml of tap water, 943mg of (NH4)2SO4, 1300mg of NaNO2, 8mg of KH2PO4, 4.48mg of CaCl 2. H2O, 240mg of MgSO4.7H2O, 1000mg of KHCO3, 1.25ml of trace element I and 1.25ml of trace element II; 1L of trace elements I comprises the following components: 6.369g EDTA, 9.14g FeSO4.7H2O, 1L microelement II component including 19.106g EDTA, 0.014g H3BO4, 0.99g MnCl2.4H2O, 0.25g CuSO4.5H2O, 0.43g ZnSO4.7H2O, 0.19g NiCl2.6H2O, 0.22g NaMoO 4.2H2O.
In this embodiment, in step S9, the anaerobic baffled reactor is provided with a heating system, and the volume of the two-stage a/O biochemical reaction tank is greater than 20.4L.
In this embodiment, in step S10, the pressure active membrane of the ultrafiltration system can filter particles with a molecular weight of 80-1000, and the micro-pores on the membrane surface can screen substances with a molecular weight of 3x10000-1x10000, while the particles, macromolecules and the like larger than the pores of the membrane are retained by sieving, so that most of the colloidal silica is removed, and a large amount of organic substances and the like can be removed.
According to the anaerobic ammonium oxidation method for landfill leachate sewage, the leachate waste water at different stages is treated by adding the microbial agent, so that on one hand, required enrichment culture conditions can be provided for anaerobic ammonium oxidation bacteria, and COD (chemical oxygen demand) and nitrite ammonia nitrogen in the effluent reach the requirements of enrichment strains; on the other hand, the method can improve the growth rate of the bacteria and the tolerance performance of the bacteria by performing the synergistic acclimation effect on the target strains in the enrichment process, simultaneously ensure that the reduction rate of the total nitrogen of the effluent reaches 95 percent, greatly improve the removal rate of the total nitrogen in the biological denitrification process, save 50 percent of oxygen supply cost compared with the traditional nitrification denitrification process, do not need additional carbon sources, greatly reduce the treatment cost and the infrastructure cost of sewage treatment, simultaneously have an ultrafiltration system, solve the defects that the sewage treated by a biochemical reaction tank in the prior art is directly treated by a disc tube type reverse osmosis membrane, ensure that the treatment load of the reverse osmosis membrane is higher and the service life is short, solve the problems that the nitrite nitrogen in the anaerobic ammonia oxidation reaction is difficult to stably generate and the total nitrogen is removed, reduce the toxic action, shorten the reaction flow and the reaction time in the biochemical denitrification process of the landfill leachate, the volume of the reaction tank and the aeration quantity of the aerobic tank are saved, the biological denitrification efficiency of the landfill leachate is improved, a large amount of residual sludge generated by the traditional biological denitrification is avoided, the treatment cost of the landfill leachate is reduced, and the method has important significance for the engineering of the related energy-saving and low-carbon high-efficiency denitrification technology.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (8)
1. The anaerobic ammonia oxidation method for landfill leachate sewage is characterized by comprising the following steps: the method comprises the following steps:
s1, collecting the garbage leachate generated in the garbage landfill area through a collection pipeline, separating solid impurities from the collected garbage leachate through a stainless steel fine grid arranged at the inlet of an adjusting tank of a sewage treatment plant, and then feeding the garbage leachate into a leachate adjusting tank, wherein the leachate is homogenized and equalized in the adjusting tank;
s2, heating the leachate, turning on a landfill leachate heating device in the regulating tank to heat, and controlling the on-off of a heater through a temperature controller to ensure that the temperature of the landfill leachate to be treated reaches 33-37 ℃ after heating and heat exchange
S3, acidifying the sewage, wherein the heated effluent of the regulating reservoir flows into a hydrolysis acidification pool, hydrolysis acidification bacteria in the hydrolysis acidification pool hydrolyze and acidify a long-chain high-molecular polymer into organic micromolecule alcohol or acid with stronger biodegradability, and part of heterocyclic organic matters which are not biochemical or have weaker biodegradability can be degraded into biochemical organic molecules, so that the BOD5/CODCr value of organic pollutants in the sewage is increased;
s4, anaerobic pretreatment, namely putting an activated anaerobic enhanced microbial inoculum and/or a composite denitrification microbial inoculum with a preset volume concentration into the acidified wastewater for anaerobic/anoxic reaction treatment for a preset time, wherein the volume concentration of the anaerobic enhanced microbial inoculum is 0.03-0.1%, and the anaerobic enhanced microbial inoculum is one or more of enterococcus, yeast and clostridium butyricum;
s5, aerating, introducing the wastewater into an aerating device after anaerobic effluent, adding an aerobic strengthening microbial inoculum and an autotrophic nitrifying microbial inoculum which are activated at a preset volume concentration, carrying out COD removal and ammonia nitrogen degradation treatment on the wastewater, and controlling the reaction time of the aeration treatment to regulate the proportion of COD, ammonia nitrogen and nitrite;
s6, performing enrichment treatment, namely allowing the aerated effluent to enter an enrichment device of a sewage treatment plant for standing reaction until red zoogloea appears, and completing the enrichment of anaerobic ammonium oxidation bacteria until the total nitrogen removal rate is stable;
s7, inoculating sewage containing anaerobic oxidizing bacteria into an anaerobic baffle plate reactor of a sewage plant under anaerobic conditions, introducing ammonia nitrogen and nitrite nitrogen with the concentration of 9-21 mg/L and the pH of 7.8-8.3 into the anaerobic baffle plate reactor through a water inlet storage bottle, controlling the water inflow by using a constant-current peristaltic pump positioned between the water inlet storage bottle and the anaerobic baffle plate reactor so as to control the hydraulic retention time to be 24-48 h, controlling the reaction temperature to be 25-30 ℃, discharging the treated wastewater from a water outlet, and discharging gas from an exhaust port until the anaerobic oxidizing bacteria in the anaerobic baffle plate reactor become dominant flora and the removal rate of the ammonia nitrogen and the nitrite nitrogen reaches 80% after 5 days;
s8, after the anaerobic baffle plate reactor is successfully started, adding short-cut nitrified sludge, anaerobic ammonium oxidation sludge, short-cut denitrifying anaerobic ammonium oxidation sludge and the sewage obtained in the step S7 into each anaerobic baffle plate reactor, and controlling the sludge concentration of mixed liquor of each reactor after adding to be respectively sludge concentration MLSS (6000 +/-300 mg/L), MLVSS (4500 +/-350 mg/L), and f (MLVSS/MLSS) to be 70%;
s9, making the percolate enter a two-stage A/O biochemical reaction tank after anaerobic treatment by an anaerobic baffle plate reactor, and fully removing organic matters and denitriding the percolate in the biochemical reaction tank;
s10, lifting the percolate subjected to biochemical treatment into an ultrafiltration system through a lifting pump, intercepting colloids, particles and substances with relatively high molecular weight in water under the action of pressure by using a pressure active membrane in the ultrafiltration system, and separating water and relatively small solute particles through the membrane;
s11, discharging the treated leachate, and closing the sewage treatment equipment.
2. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 1, wherein: in the step S4, the volume concentration of the composite denitrification microbial inoculum is 0.01-0.1%; the composite denitrifying microbial agent is one or more of bacillus pumilus, bacillus cereus and bacillus thuringiensis.
3. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 1, wherein: in the step S5, the aeration treatment reaction time is 11-95 h, the reaction conditions are controlled such that the COD of the effluent is less than 110mg/L, and the ratio of the ammonia nitrogen to the nitrite is 1: 1-1: 1.2.
4. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 3, wherein: in the step S6, the water feeding frequency of the enrichment device per day is 2-10, the single standing reaction time is 2-6 h, and the enrichment time is 30-60 days.
5. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 1, wherein: in the S7, the anaerobic baffled reactor is 40cm long, 14cm wide, 30cm high, 27.5cm effective height, 15.4L effective volume and 45 degrees at the baffled corner.
6. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 1, wherein: in the step S8, in order to avoid excessive impact of the landfill leachate on the sludge, the system is stably operated for 30d in an artificial water distribution manner at the initial starting stage, and then the proportion of the late-stage landfill leachate in the water distribution is increased by a concentration gradient of 20% every 10d, so that the sludge is gradually adapted to the late-stage landfill leachate, and the reactor acclimates for 80 d; wherein each liter of water is composed of 997.5ml of tap water, 943mg of (NH4)2SO4, 1300mg of NaNO2, 8mg of KH2PO4, 4.48mg of CaCl 2. H2O, 240mg of MgSO 4. 7H2O, 1000mg of KHCO3, 1.25ml of trace element I and 1.25ml of trace element II; 1L of trace elements I comprises the following components: 6.369g EDTA, 9.14g FeSO 4.7H 2O, 1L microelement II component including 19.106g EDTA, 0.014g H3BO4, 0.99g MnCl 2.4H2O, 0.25g CuSO 4.5H2O, 0.43g ZnSO 4.7H 2O, 0.19g NiCl 2.6H2O, 0.22g NaMoO 4.2H2O.
7. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 1, wherein: in the step S9, the anaerobic baffled reactor is provided with a heating system, and the volume of the two-stage A/O biochemical reaction tank is more than 20.4L.
8. The anaerobic ammonia oxidation method for landfill leachate sewage of claim 1, wherein: in step S10, the pressure active membrane of the ultrafiltration system may filter particles having a molecular weight of 80-1000.
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