A rapid start-up method for anaerobic ammonia oxidation treatment of incineration garbage leachate, and a treatment method and system for incineration garbage leachate

Abstract

This invention provides a rapid start-up method for anaerobic ammonia oxidation (AAO) treatment of landfill leachate, as well as a treatment method and system for landfill leachate, belonging to the field of anaerobic ammonia oxidation treatment technology. The rapid start-up method for anaerobic ammonia oxidation treatment of landfill leachate of this invention first involves inoculating the landfill leachate with anaerobic activated sludge for buffering; then anaerobic fermentation is carried out; subsequently, flocculation and sedimentation remove large particulate impurities and organic pollutants that have not been fully fermented; then ammoniation is performed to convert organic ammonia into inorganic ammonia; then, through anaerobic ammonia oxidation, a portion of the ammonia nitrogen is oxidized into nitrogen gas; then, short-cut nitrification is performed to provide nitrite for subsequent steps; then, short-cut denitrification is carried out through anaerobic processes to further increase the nitrite content; then, ultrafiltration is used to remove sludge and macromolecules; finally, activated carbon-coupled anaerobic ammonia oxidation is performed on the ultrafiltration permeate, ultimately converting the nitrogen in the landfill leachate into nitrogen gas, which is then discharged from the system.

Description

Technical Field

[0001] This invention belongs to the field of anaerobic ammonia oxidation treatment technology, and particularly relates to incineration leachate and systems with high organic matter concentration. Background Technology

[0002] Anaerobic ammonia oxidation (AAO) is a biological nitrogen removal process. Under anaerobic conditions, ammonia is oxidized into nitrogen gas using ammonia as the electron donor and nitrate or nitrite as the electron acceptor. This saves more than 60% of the oxygen required compared to full nitrification (ammonia oxidation to nitrate). Although AAO has opened up a new pathway for biological nitrogen removal from wastewater, its limited tolerance to environmental organic matter and the need for a stable nitrite supply make it difficult to apply in practical engineering for treating high-organic-matter-concentration incineration leachate. Furthermore, the long start-up time is a major obstacle to its engineering application. Summary of the Invention

[0003] The purpose of this invention is to provide a rapid start-up method for anaerobic ammonia oxidation treatment of incineration landfill leachate, as well as a treatment method and system for incineration landfill leachate. The treatment method of this invention can treat incineration landfill leachate with high organic matter concentration, and the process start-up time is short.

[0004] This invention provides a rapid start-up method for anaerobic ammonia oxidation treatment of landfill leachate, comprising the following steps: 1) Anaerobic activated sludge is inoculated into the leachate from incineration of landfills to buffer the leachate and obtain buffered leachate; 2) Inoculate the buffer leachate with anaerobic activated sludge and carry out anaerobic fermentation to obtain anaerobic fermentation products; 3) The anaerobic fermentation products are subjected to flocculation and precipitation to obtain the supernatant of the flocculated products; 4) Inoculate aerobic activated sludge into the supernatant of the flocculated product and perform ammoniation until the COD of the supernatant reaches a certain level. Cr ≤2500 mg / L, to obtain the supernatant of the amination product; 5) Inoculate anaerobic activated sludge into the supernatant of the ammonification product and carry out ammonia oxidation to obtain the supernatant of the ammonia oxidation product; 6) Inoculate the supernatant of the ammonia oxidation product with anaerobic ammonia oxidation activated sludge and denitrification sludge to carry out anaerobic ammonia oxidation and obtain the supernatant of the anaerobic ammonia oxidation product. 7) Inoculate aerobic activated sludge into the supernatant of the anaerobic ammonia oxidation product and carry out short-cut nitrification to obtain the supernatant of the short-cut nitrification product; 8) Inoculate aerobic activated sludge into the supernatant of the short-cut nitrification reaction products to carry out secondary short-cut nitrification or start short-cut denitrification until the COD of the supernatant reaches a certain level. Cr≤1000 mg / L, to obtain secondary short-cut nitrification supernatant or short-cut denitrification supernatant; perform secondary short-cut nitrification 30 days before start-up, and short-cut denitrification 30 days after start-up; 9) The supernatant from the secondary short-cut nitrification or the supernatant from the short-cut denitrification is subjected to ultrafiltration to obtain sludge and ultrafiltrate. 10) Inoculate the ultrafiltrate with anaerobic ammonia-oxidizing bacteria and activated carbon to perform activated carbon-coupled anaerobic ammonia oxidation until the COD of the supernatant is [value missing]. Cr Discharge shall be ≤100 mg / L and ammonia nitrogen ≤25 mg / L; In the initial feed solution for activated carbon coupled anaerobic ammonia oxidation, the mass concentration ratio of ammonia nitrogen to nitrite nitrogen is 2:1 to 3:1.

[0005] Preferably, in step 1), the COD of the incineration leachate is... Cr The ammonia nitrogen content of the incineration leachate is ≤25000 mg / L, and the buffer temperature is 1200~1800 mg / L; the buffer pH is 7~7.2; and the buffering time is 12~24 h. In step 2), the temperature of the anaerobic fermentation is 10~40℃, the pH value of the anaerobic fermentation is 7~7.2, and the time of the anaerobic fermentation is 10~36 h; In step 3), the flocculant used for flocculation and sedimentation includes at least one of polyaluminum chloride, iron salt, and polyacrylamide; the working concentration of the flocculant is 50~150 mg / L; and the flocculation and sedimentation time is 1~2 h. In step 4), during the ammoniation process, the dissolved oxygen concentration is greater than or equal to 0.1 mg / L; the hydraulic retention time for ammoniation is 1.5~10 h. After ammoniaation, the COD of the supernatant Cr When the concentration is greater than 2500 mg / L, reflux to step 2) for anaerobic fermentation.

[0006] Preferably, in step 5), the hydraulic residence time for ammonia oxidation is 15-48 h.

[0007] Preferably, in step 6), the volume ratio of the anaerobic ammonia oxidation activated sludge to the denitrification sludge is 3:2 to 1:1; the pH value of the anaerobic ammonia oxidation is 6.5 to 7.2; and the hydraulic retention time of the anaerobic ammonia oxidation is 20 to 48 h. In the initial feed solution of the anaerobic ammonia oxidation, COD Cr The mass concentration ratio of NH3 to NH3 is 5:2 to 25:7.

[0008] Preferably, in step 7), the dissolved oxygen content during the short-cut nitrification process is 0.08~0.42 mg / L; and the hydraulic retention time of the short-cut nitrification is 8~16 h.

[0009] Preferably, in step 8), the dissolved oxygen content during the secondary short-cut nitrification process is 0.08~0.1 mg / L; During the short-cut denitrification process, aeration is stopped and the hydraulic retention time is 5-16 hours. When the COD of the supernatant Cr When the concentration is greater than 1000 mg / L, reflux to step 5) for ammonia oxidation.

[0010] Preferably, in step 9), the intercepted sludge is returned to step 5) for ammonia oxidation.

[0011] Preferably, in step 10), the volume ratio of the anaerobic ammonia-oxidizing bacteria to activated carbon is 1:(5~12). When the COD of the supernatant Cr If the concentration is greater than 100 mg / L, reflux to step 8) for secondary short-cut nitrification or short-cut denitrification; When the supernatant from activated carbon coupled anaerobic ammonia oxidation is discharged, and the volume of the remaining sludge exceeds 1 / 2 of the reaction vessel volume, the remaining sludge is returned to step 5) for ammonia oxidation.

[0012] The present invention also provides a method for treating incineration landfill leachate, comprising the following steps: (1) Anaerobic fermentation of incineration leachate to obtain anaerobic fermentation products; (2) The anaerobic fermentation products are subjected to flocculation and precipitation to obtain the supernatant of the flocculated products; (3) The supernatant of the flocculation product is aminated to obtain the supernatant of the aminated reaction product; (4) The supernatant of the ammoniation reaction is subjected to ammonia oxidation to obtain an ammonia oxidation product supernatant; (5) Anaerobic ammonia oxidation is performed on the supernatant of the ammonia oxidation product to obtain an anaerobic ammonia oxidation product supernatant; (6) The supernatant of the anaerobic ammonia oxidation product is subjected to short-cut nitrification to obtain the supernatant of the short-cut nitrification reaction product; (7) The supernatant of the short-cut nitrification reaction product is subjected to short-cut denitrification to obtain the supernatant of the short-cut denitrification reaction product; (8) The supernatant of the short-cut denitrification reaction product is subjected to ultrafiltration to obtain ultrafiltrate; (9) The ultrafiltrate is subjected to activated carbon coupled anaerobic ammonia oxidation reaction until the supernatant of the activated carbon coupled anaerobic ammonia oxidation product meets the discharge standard and is then discharged.

[0013] The present invention also provides a system for anaerobic ammonia oxidation treatment of landfill leachate, including a buffer tank; An anaerobic fermentation tank connected to the outlet of the buffer tank; A flocculation sedimentation tank connected to the outlet of the anaerobic fermentation tank; A first aerobic tank connected to the outlet of the flocculation sedimentation tank; The first anaerobic tank is connected to the outlet of the first aerobic tank; A second anaerobic tank connected to the outlet of the first anaerobic tank; A second aerobic tank connected to the outlet of the second anaerobic tank; A third aerobic tank connected to the outlet of the second aerobic tank; An ultrafiltration device connected to the outlet of the third aerobic tank; An activated carbon tank connected to the outlet of the ultrafiltration device.

[0014] This invention provides a rapid start-up method for anaerobic ammonia oxidation treatment of incineration landfill leachate, comprising the following steps: 1) inoculating anaerobic activated sludge into the incineration landfill leachate for buffering, obtaining buffered leachate; 2) inoculating the buffered leachate with anaerobic activated sludge for anaerobic fermentation, obtaining anaerobic fermentation products; 3) flocculating and settling the anaerobic fermentation products to obtain a flocculated product supernatant; 4) inoculating the flocculated product supernatant with aerobic activated sludge for ammoniation, reducing the COD of the supernatant to a certain level. Cr 5) Inoculate the ammonification supernatant with ≤2500 mg / L to obtain ammonification product supernatant; 6) Inoculate the ammonification product supernatant with anaerobic activated sludge and denitrification sludge to obtain ammonium oxidation product supernatant; 7) Inoculate the ammonium oxidation product supernatant with aerobic activated sludge and denitrification sludge to obtain anaerobic ammonium oxidation product supernatant; 8) Inoculate the anaerobic ammonium oxidation product supernatant with aerobic activated sludge to obtain short-cut nitrification product supernatant; 9) Inoculate the short-cut nitrification product supernatant with aerobic activated sludge to obtain secondary short-cut nitrification or start short-cut denitrification until the COD of the supernatant is ≤2500 mg / L. Cr The concentration is ≤1000 mg / L, yielding secondary short-cut nitrification supernatant or short-cut denitrification supernatant; secondary short-cut nitrification is performed 30 days before start-up, and short-cut denitrification is performed 30 days after start-up; 9) The secondary short-cut nitrification supernatant or short-cut denitrification supernatant is subjected to ultrafiltration to obtain sludge and ultrafiltrate; 10) Anaerobic ammonia oxidizing bacteria and activated carbon are inoculated into the ultrafiltrate to perform activated carbon coupled anaerobic ammonia oxidation until the COD of the supernatant is reduced to a certain level. CrDischarge concentrations are ≤100 mg / L for ammonia nitrogen and ≤25 mg / L for anaerobic ammonium oxidation with activated carbon. The mass concentration ratio of ammonia nitrogen to nitrite nitrogen in the initial feed liquid is 2:1 to 3:1. The method of this invention first inoculates anaerobic activated sludge into the incineration leachate, then buffers it to delay its entry into the treatment system, improving the system's adaptability. Then, anaerobic fermentation is carried out, where a portion of the organic matter is converted into methane and carbon dioxide, along with a large amount of amino acids, proteins, unsaturated fatty acids, and fibers in an anaerobic environment. Next, flocculation and sedimentation remove large particulate impurities such as incompletely fermented fibers, reducing subsequent load. Then, ammoniation is performed, converting organic ammonia into inorganic ammonia. Driven by ammonifying bacteria in the aerobic sludge, extracellular enzymes secreted decompose organic matter, releasing ammonia nitrogen through a deammoniation reaction. The process begins with ammonia oxidation. Ammonia monooxygenase (AMO) catalyzes the formation of hydroxylamine from ammonia, which is then converted to nitrite by hydroxylamine reductase. Next, anaerobic ammonia oxidation occurs, where nitrite acts as an electron donor and reacts with hydroxylamine. The hydroxylamine oxidase released by anaerobic ammonia-oxidizing bacteria then generates hydrazine, which is oxidized to nitrogen gas. At this point, because some organic matter and ammonia in the solution have not completely reacted, the effluent does not meet the required standards. Therefore, anaerobic processes are insufficient, and appropriate aeration is necessary to oxidize and decompose recalcitrant organic matter and promote short-cut nitrification of ammonia by nitrifying microorganisms in the aerobic activated sludge, thus preparing the effluent for subsequent treatments. The activated carbon coupled anaerobic ammonium oxidation process provides nitrite; the raw water also contains some nitrate and a small amount of nitrate produced by aeration. At startup, the nitrifying bacteria in the previous aeration ammoniation and short-cut nitrification stages have not yet proliferated on a large scale, and the nitrate concentration in the system is low. Secondary short-cut nitrification is first performed using aerobic sludge to further produce nitrite nitrogen from ammonia. After a period of time, aeration is stopped in this stage, and the sludge gradually transforms into anaerobic activated sludge. The short-cut denitrifying bacteria in the sludge are activated, converting nitrate nitrogen in the water into nitrite nitrogen. At this point, short-cut denitrification is achieved through anaerobic processes, further providing stable nitrite nitrogen for subsequent reactions. Simultaneously, a portion of the treated liquid is recycled, primarily to provide stable nitrite for anaerobic ammonia oxidation. Then, ultrafiltration is used to retain sludge and large molecules in the water, such as proteins. This retained sludge is recycled to the ammonia oxidation stage, increasing the sludge content. The ultrafiltrate undergoes activated carbon-coupled anaerobic ammonia oxidation. In this stage, ammonia nitrogen, nitrite nitrogen, and anaerobic ammonia oxidizing bacteria in the liquid are easily adsorbed by activated carbon, increasing the reactant concentration, the probability of contact between the three, enhancing the anaerobic ammonia oxidation rate, and improving the system's nitrogen removal efficiency. Ultimately, the nitrogen in the incineration leachate is converted into nitrogen gas and discharged from the system.This invention achieves the application of cascade anaerobic ammonia oxidation in incineration leachate with a high C / N ratio. By using buffering, low aeration, and selective aeration for startup, and adding exogenous anaerobic ammonia oxidizing bacteria, the rapid startup method for anaerobic ammonia oxidation treatment of incineration leachate of this invention is highly stable and can be started up quickly, providing green and low-carbon treatment of incineration leachate containing high concentrations of pollutants. Attached Figure Description

[0015] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0016] Figure 1 This is a flowchart illustrating the process principle. Figure 2 This is a schematic diagram of the anaerobic ammonia oxidation system for treating incineration landfill leachate provided by the present invention. Figure 2 In the diagram, aerobic tank 1 corresponds to the first aerobic tank, aerobic tank 2 corresponds to the second aerobic tank, aerobic tank 3 corresponds to the third aerobic tank, anaerobic tank 1 corresponds to the first anaerobic tank, and anaerobic tank 2 corresponds to the second anaerobic tank. Detailed Implementation

[0017] This invention provides a rapid start-up method for anaerobic ammonia oxidation treatment of landfill leachate, comprising the following steps: 1) Anaerobic activated sludge is inoculated into the leachate from incineration of landfills to buffer the leachate and obtain buffered leachate; 2) Inoculate the buffer leachate with anaerobic activated sludge and carry out anaerobic fermentation to obtain anaerobic fermentation products; 3) The anaerobic fermentation products are subjected to flocculation and precipitation to obtain the supernatant of the flocculated products; 4) Inoculate aerobic activated sludge into the supernatant of the flocculated product and perform ammoniation until the COD of the supernatant reaches a certain level. Cr ≤2500 mg / L, to obtain the supernatant of the amination product; 5) Inoculate anaerobic activated sludge into the supernatant of the ammonification product and carry out ammonia oxidation to obtain the supernatant of the ammonia oxidation product; 6) Inoculate the supernatant of the ammonia oxidation product with anaerobic ammonia oxidation activated sludge and denitrification sludge to carry out anaerobic ammonia oxidation and obtain the supernatant of the anaerobic ammonia oxidation product. 7) Inoculate aerobic activated sludge into the supernatant of the anaerobic ammonia oxidation product and carry out short-cut nitrification to obtain the supernatant of the short-cut nitrification product; 8) Inoculate aerobic activated sludge into the supernatant of the short-cut nitrification products to perform secondary short-cut nitrification or start short-cut denitrification until the COD of the supernatant reaches a certain level. Cr ≤1000 mg / L, to obtain secondary short-cut nitrification supernatant or short-cut denitrification supernatant; perform secondary short-cut nitrification 30 days before start-up, and short-cut denitrification 30 days after start-up; 9) The supernatant from the secondary short-cut nitrification or the supernatant from the short-cut denitrification is subjected to ultrafiltration to obtain sludge and ultrafiltrate. 10) Inoculate the ultrafiltrate with anaerobic ammonia-oxidizing bacteria and activated carbon to perform activated carbon-coupled anaerobic ammonia oxidation until the COD of the supernatant is [value missing]. Cr Discharge shall be ≤100 mg / L and ammonia nitrogen ≤25 mg / L; In the initial feed solution for activated carbon coupled anaerobic ammonia oxidation, the mass concentration ratio of ammonia nitrogen to nitrite nitrogen is 2:1 to 3:1.

[0018] The present invention first inoculates anaerobic activated sludge into the leachate from incinerated landfills to buffer it, thereby obtaining buffered leachate.

[0019] As one implementation method, the COD of the incineration leachate is... Cr Preferably, the ammonia nitrogen content is ≤25000 mg / L; the preferred ammonia nitrogen content of the incineration leachate is 1200~1800 mg / L.

[0020] As one implementation method, the temperature of the buffer is 15~40℃, more preferably 15~25℃ or 16~28℃; the pH of the buffer is 7~7.2, more preferably 7.0; the buffering time is preferably 12~24 h; the buffering is carried out in a buffer tank; the volume ratio of the anaerobic activated sludge used in the buffering to the reaction volume is preferably 1:100. In this invention, the adaptability of the treatment system is improved by buffering. In the specific implementation of this invention, the degree of buffering is determined with reference to the following two conditions: (1) it is usually determined by the average annual leachate water quality, with fluctuations not exceeding 1%; (2) when the leachate production is particularly large, such as heavy rain or continuous rainfall, with a daily production ≥ 1.5 times the annual average and requiring large-scale treatment, it is based on the premise of preventing safety accidents. In this invention, when the sludge in the buffer tank is full, it is preferably discharged from the system.

[0021] After obtaining the buffer leachate, the present invention inoculates anaerobic activated sludge into the buffer leachate and carries out anaerobic fermentation to obtain anaerobic fermentation products.

[0022] In one implementation method, the anaerobic fermentation is preferably carried out in an anaerobic fermentation tank; the anaerobic activated sludge preferably includes anaerobic granular sludge; the anaerobic granular sludge accounts for 50-60% of the volume of the anaerobic reaction volume; the temperature of the anaerobic fermentation is 10-40℃, more preferably 14-27℃ or 16-28℃; the pH of the anaerobic fermentation is 7-7.2, more preferably 7.0; the hydraulic retention time of the anaerobic fermentation is preferably 10-36 h. In this invention, when the sludge in the anaerobic fermentation tank is full, it is preferably discharged from the system. In this invention, after anaerobic fermentation decomposes organic matter, a portion of the organic matter is converted into methane and carbon dioxide in an anaerobic environment.

[0023] After obtaining the anaerobic fermentation product, the present invention performs flocculation and precipitation on the anaerobic fermentation product to obtain the supernatant of the flocculated product.

[0024] In one embodiment, the flocculant used in the flocculation and sedimentation includes at least one of polyaluminum chloride (PAC), iron salt, and polyacrylamide (PAM); the working concentration of the polyaluminum chloride is 50-150 mg / L, more preferably 120 mg / L; the flocculation and sedimentation time is 1-2 hours; the flocculation and sedimentation is carried out in a flocculation and sedimentation tank. In this invention, the sludge in the flocculation and sedimentation tank is preferably discharged from the system when it is full. In this invention, after the anaerobic fermentation, the reaction system still contains a large amount of amino acids, proteins, unsaturated fatty acids, fibers, etc.; through flocculation and sedimentation, large particulate impurities such as incompletely fermented fibers are removed, reducing the subsequent load.

[0025] After obtaining the supernatant of the flocculated product, the present invention inoculates aerobic activated sludge into the supernatant of the flocculated product and performs ammoniation until the COD of the supernatant is reduced to a certain level. Cr ≤2500 mg / L, to obtain the supernatant of the amination product.

[0026] In one implementation method, during ammoniation, the dissolved oxygen concentration is preferably greater than or equal to 0.1 mg / L; the hydraulic retention time of ammoniation is preferably 1.5 to 10 h; the ammoniation is carried out in a first aerobic tank; and the aerobic activated sludge accounts for 10 to 30% of the reaction volume of the ammoniation, more preferably 20%. In this invention, organic ammonia is converted into inorganic ammonia through ammoniation. Driven by ammonia-oxidizing bacteria in the aerobic activated sludge, the secreted extracellular enzymes decompose organic matter, releasing ammonia nitrogen through a deammoniation reaction.

[0027] As one implementation method, this invention adjusts the concentration of aerobic activated sludge used in anaerobic fermentation, flocculation sedimentation, and ammoniation, as well as the hydraulic retention time and reflux measures during ammoniation. For example, it reduces the COD of the ammoniation effluent. CrThe concentration of COD in the ammonia-treated effluent should be controlled at ≤2500 mg / L, and the ammonia nitrogen content should be controlled at 700~800 mg / L. As one implementation method, when the COD of the ammonia-treated effluent... Cr If the values ​​are higher than the above range, it indicates that the anaerobic fermentation time needs to be increased or the amount of anaerobic fermentation sludge needs to be increased or the sludge needs to be returned to anaerobic fermentation. If the ammonia nitrogen content is lower than the above range, it indicates that the ammoniation time needs to be increased or the sludge strength needs to be increased. This is the key to successfully starting the anaerobic ammonia oxidation process in the second anaerobic tank.

[0028] After obtaining the supernatant of the ammoniation product, the present invention inoculates anaerobic activated sludge into the supernatant of the ammoniation product and performs ammonia oxidation to obtain the supernatant of the ammonia oxidation product.

[0029] In one embodiment, the hydraulic retention time of the ammonia oxidation is 15-48 h, more preferably 36 h; the ammonia oxidation is preferably carried out in a first anaerobic tank; the first anaerobic tank is kept in a static state; the anaerobic activated sludge accounts for 40-50% of the volume of the ammonia oxidation reaction volume. In this invention, the sludge in the first anaerobic tank is preferably discharged from the system when it is full. During the ammonia oxidation process, ammonia monooxygenase (AMO) catalyzes the formation of hydroxylamine from ammonia, and hydroxylamine reductase converts hydroxylamine into nitrite. In this invention, the anaerobic activated sludge comes from a denitrification tank. At this time, aerobic ammonification occurs before ammonia oxidation, and the supernatant of the ammonification product enters the ammonia oxidation process. The water still contains trace amounts of oxygen. This environment easily activates the nitrite-oxidizing bacteria in the ammonia-oxidizing bacteria of the anaerobic sludge, and AMO is released by the bacteria through a biochemical reaction.

[0030] After obtaining the supernatant of ammonia oxidation products, the present invention inoculates anaerobic ammonia oxidation activated sludge and denitrification sludge into the supernatant of ammonia oxidation products to carry out anaerobic ammonia oxidation and obtain anaerobic ammonia oxidation product supernatant.

[0031] As one implementation method, the volume ratio of the anammox activated sludge to the denitrification sludge used for anammox is 3:2 to 1:1; the pH value of the anammox is 6.5 to 7.2, and the hydraulic retention time is 20 to 48 h, more specifically 36 h; the initial feed liquid for the anammox contains COD... Cr The preferred mass concentration ratio of anaerobic sludge to NH3 is 5:2 to 25:7; the anaerobic ammonium oxidation is carried out in a second anaerobic tank; the second anaerobic tank remains static; the volume percentage of the anaerobic activated sludge and denitrifying sludge in the anaerobic ammonium oxidation reaction is 50-60%. In this invention, the sludge in the second anaerobic tank is preferably discharged from the system when it is full. In this invention, through anaerobic ammonium oxidation, nitrite reacts with hydroxylamine as an electron donor, and hydrazine is generated by hydroxylamine oxidase, which then oxidizes to nitrogen gas.

[0032] After obtaining the supernatant of the anaerobic ammonia oxidation product, the present invention inoculates aerobic activated sludge into the supernatant of the anaerobic ammonia oxidation product and performs short-cut nitrification to obtain the supernatant of the short-cut nitrification product.

[0033] In one implementation method, during the short-cut nitrification process, the dissolved oxygen content is 0.08~0.42 mg / L, further 0.1~0.15 mg / L; the dissolved oxygen content is achieved through aeration, with an aeration rate of 100~800 m³ / h; the aeration gas is air; the hydraulic retention time of the short-cut nitrification is 8~16 h; the short-cut nitrification is carried out in a second aerobic tank; the volume percentage of aerobic activated sludge in the short-cut nitrification reaction volume is 20~40%. In this invention, the sludge in the second aerobic tank is preferably discharged from the system when it is full. In this invention, because some organic matter and ammonia in the supernatant of the anaerobic ammonia oxidation product have not reacted completely and do not meet the effluent requirements, the anaerobic process is no longer sufficient to meet the requirements. Appropriate aeration is needed to achieve the oxidative decomposition of recalcitrant organic matter, promote the short-cut nitrification reaction of ammonia by nitrifying microorganisms, and provide nitrite for the subsequent activated carbon-coupled anaerobic ammonia oxidation process.

[0034] After obtaining the supernatant of the short-cut nitrification products, the present invention inoculates aerobic activated sludge into the supernatant to perform secondary short-cut nitrification or initiate short-cut denitrification until the COD of the supernatant reaches a certain level. Cr ≤1000 mg / L, to obtain secondary short-cut nitrification supernatant or short-cut denitrification supernatant; perform secondary short-cut nitrification 30 days before start-up, and short-cut denitrification 30 days after start-up.

[0035] In one implementation method, during the secondary short-cut nitrification process, the dissolved oxygen content is 0.08~0.1 mg / L; the dissolved oxygen is preferably obtained through aeration, the aeration rate is 100~200 m³ / h, and the aeration gas is preferably air; the hydraulic retention time of the secondary short-cut nitrification is 8 h; the volume percentage of the aerobic activated sludge in the reaction volume of the secondary short-cut nitrification or the initiation of short-cut denitrification is 10~45%, further 20% or 30%.

[0036] In one implementation method, during the short-cut denitrification process, aeration is stopped, and the hydraulic retention time is 5-16 hours.

[0037] In one implementation, the secondary short-cut nitrification or short-cut denitrification is carried out in a third aerobic tank. In this invention, after the sludge in the third aerobic tank is full, the sludge is preferably returned to ammonia oxidation.

[0038] As one implementation method, the COD in the effluent from secondary short-cut nitrification or short-cut denitrification is... CrFor concentrations greater than 1000 mg / L, reflux for ammonia oxidation.

[0039] After obtaining the secondary short-cut nitrification supernatant or the short-cut denitrification supernatant, the present invention performs ultrafiltration on the secondary short-cut nitrification supernatant or the short-cut denitrification supernatant to obtain retained sludge and ultrafiltrate.

[0040] In one implementation method, the retained sludge is returned for ammonia oxidation, and the return flow rate of the retained sludge is 200~400 m³ / h; the ultrafiltration is carried out using an external ultrafiltration membrane. In this invention, ultrafiltration not only retains the sludge but also large molecules in the water, such as proteins, amino acids, and sugars. The retained material is returned to the ammonia oxidation reaction stage to increase the ammonia oxidation sludge content.

[0041] After obtaining the ultrafiltrate, the present invention inoculates anaerobic ammonia-oxidizing bacteria and activated carbon into the ultrafiltrate to carry out an activated carbon-coupled anaerobic ammonia oxidation reaction until the COD of the supernatant is reduced. Cr Discharge shall be carried out with ammonia nitrogen concentration ≤100 mg / L and ammonia nitrogen concentration ≤25 mg / L; in the initial feed solution for activated carbon coupled anaerobic ammonia oxidation, the mass concentration ratio of ammonia nitrogen to nitrite nitrogen is 2:1~3:1.

[0042] In one embodiment, the volume ratio of the anaerobic ammonia-oxidizing bacteria to activated carbon is 1:(5~12); when the COD of the supernatant is... Cr If the concentration is greater than 100 mg / L, the sludge is refluxed for secondary short-cut nitrification or short-cut denitrification. When the supernatant of activated carbon coupled anaerobic ammonia oxidation is discharged and the volume of the remaining sludge accounts for more than 1 / 2 of the volume of the reaction vessel, the remaining sludge is refluxed to step 5) for ammonia oxidation.

[0043] As one implementation method, the present invention utilizes reaction conditions of ammoniation, short-cut nitrification, secondary short-cut nitrification / short-cut denitrification, and ultrafiltration to reduce the COD of the effluent from secondary short-cut nitrification / short-cut denitrification. Cr A concentration of less than 1000 mg / L and a mass concentration ratio of ammonia nitrogen to nitrite nitrogen of 2:1 to 3:1 are key to successfully starting the activated carbon coupled anaerobic ammonia oxidation reaction in the activated carbon tank.

[0044] In one embodiment, the activated carbon coupled anaerobic ammonia oxidation reaction is carried out in an activated carbon tank; the anaerobic ammonia oxidizing bacteria used in the activated carbon coupled anaerobic ammonia oxidation reaction are anaerobic ammonia oxidizing granular sludge; the present invention does not impose any special limitation on the effective viable number of the anaerobic ammonia oxidizing bacteria.

[0045] In this invention, anaerobic ammonia oxidizing bacteria and activated carbon occupy the reaction space of the activated carbon-coupled anaerobic ammonia oxidation reaction, forming an anaerobic environment that provides a favorable environment for the anaerobic ammonia oxidizing bacteria. When the ultrafiltrate enters the activated carbon-coupled anaerobic ammonia oxidation stage, ammonia nitrogen, nitrite nitrogen, and anaerobic ammonia oxidizing bacteria in the liquid are easily adsorbed by the activated carbon, increasing the reactant concentration, increasing the contact probability among the three, enhancing the anaerobic ammonia oxidation rate, and improving the system's nitrogen removal efficiency. Ultimately, the nitrogen in the landfill leachate is converted into nitrogen gas and discharged from the system.

[0046] As one implementation method, the sludge discharge time for the anaerobic fermentation tank (anaerobic fermentation), the first aerobic tank (ammoniation), and the first anaerobic tank (ammonia oxidation) is 5-7 days before the ammonia oxidation tank. The discharge time for the second anaerobic tank (anaerobic ammonia oxidation), the second aerobic tank (short-cut nitrification), the third aerobic tank (secondary short-cut nitrification in the early stage of start-up, and short-cut denitrification after aeration is stopped), and the activated carbon tank varies from 50 to 120 days. The flocculation sedimentation tank discharges sludge immediately according to the actual situation.

[0047] In one implementation, the method uses a batch reaction system.

[0048] The present invention also provides a method for treating incineration landfill leachate, comprising the following steps: (1) Anaerobic fermentation of incineration leachate to obtain anaerobic fermentation products; (2) The anaerobic fermentation products are subjected to flocculation and precipitation to obtain the supernatant of the flocculated products; (3) The supernatant of the flocculated product is ammonified to obtain the ammonified product supernatant; (4) The ammonification supernatant is subjected to ammonia oxidation to obtain an ammonia oxidation product supernatant; (5) Anaerobic ammonia oxidation is performed on the supernatant of the ammonia oxidation product to obtain an anaerobic ammonia oxidation product supernatant; (6) The supernatant of the anaerobic ammonia oxidation product is subjected to short-cut nitrification to obtain a short-cut nitrification product supernatant; (7) The supernatant of the short-cut nitrification product is subjected to short-cut denitrification to obtain the supernatant of the short-cut denitrification product; (8) The supernatant of the short-cut denitrification product is subjected to ultrafiltration to obtain ultrafiltrate; (9) The ultrafiltrate is subjected to activated carbon coupled anaerobic ammonia oxidation reaction until the supernatant of the activated carbon coupled anaerobic ammonia oxidation product meets the discharge standard and is then discharged.

[0049] In one implementation, the parameters of each step of the processing method are controlled according to the parameters of the fast start method described above.

[0050] Figure 2This is a schematic diagram of a system for anaerobic ammonia oxidation treatment of incineration landfill leachate provided by the present invention. The following is in conjunction with... Figure 2 The system of the present invention will be described.

[0051] The present invention also provides a system for anaerobic ammonia oxidation treatment of landfill leachate, including a buffer tank; An anaerobic fermentation tank connected to the outlet of the buffer tank; A flocculation sedimentation tank connected to the outlet of the anaerobic fermentation tank; A first aerobic tank (aerobic tank 1) is connected to the outlet of the flocculation sedimentation tank. The first anaerobic tank (anaerobic tank 1) is connected to the outlet of the first aerobic tank (aerobic tank 1). A second anaerobic tank (anaerobic tank 2) is connected to the outlet of the first anaerobic tank (anaerobic tank 1). The second aerobic tank (aerobic tank 2) is connected to the outlet of the second anaerobic tank (anaerobic tank 2). A third aerobic tank (aerobic tank 3) connected to the outlet of the second aerobic tank (aerobic tank 2); An ultrafiltration device connected to the outlet of the third aerobic tank (aerobic tank 3); An activated carbon tank connected to the outlet of the ultrafiltration device.

[0052] To further illustrate the present invention, the rapid start-up method for anaerobic ammonia oxidation treatment of incineration landfill leachate and the treatment method and system for incineration landfill leachate provided by the present invention will be described in detail below with reference to embodiments, but these should not be construed as limiting the scope of protection of the present invention.

[0053] In the embodiment, the aerobic activated sludge came from the nitrification tank of a landfill leachate treatment plant, the anaerobic activated sludge came from the denitrification tank of a landfill leachate treatment plant, and the anaerobic ammonia oxidizing bacteria were anaerobic ammonia oxidizing activated sludge from a landfill leachate treatment plant.

[0054] Example 1 See the process flow diagram. Figure 1 See system diagram. Figure 2 .

[0055] Influent COD Cr The concentration of leachate was 21240 mg / L, and the ammonia nitrogen content was 1538 mg / L. The reaction system was a batch reaction system; the reaction volume of the system was 5 L (5 L of leachate was treated each time); the test water came from the leachate collection pond of the incineration plant.

[0056] 1. After collecting the incineration leachate from the collection pond of the incineration plant, put it into a buffer tank for buffering, add 50 mL of anaerobic activated sludge, keep the temperature at room temperature with a fluctuation range of about 15~25℃, pH 7.0, and react for 24 h to obtain buffer leachate. 2. After the buffer leachate is extracted, it enters the anaerobic fermentation tank. The amount of anaerobic activated sludge inoculated into the anaerobic fermentation tank is 3L. The reaction temperature of anaerobic fermentation is room temperature, with a temperature fluctuation range of about 14~27℃, pH 7.0, and reaction time of 36 h to obtain anaerobic fermentation products. 3. After the anaerobic fermentation products are extracted, they are put into the flocculation sedimentation tank for flocculation and sedimentation. PAC is added at a concentration of 120 mg / L and the reaction is carried out for 1 h. The reaction solution undergoes flocculation and sedimentation to obtain the supernatant of flocculated products. 4. The supernatant of the flocculated product was extracted and introduced into aerobic tank 1 for ammoniation (aerobic ammoniation). 1L of aerobic activated sludge was inoculated, and dissolved oxygen was controlled at around 0.1 mg / L through aeration. The reaction was carried out for 8 hours, during which ammoniation and partial ammonia oxidation occurred, and COD was detected. Cr After reducing the concentration to 2500 mg / L, the ammonia nitrogen was extracted, and the concentration was controlled at approximately 740 mg / L with a pH of about 6.5, yielding a supernatant of the ammoniaation product. The COD of the supernatant was... Cr If the concentration is greater than 2500 mg / L, reflux for anaerobic fermentation; 5. The supernatant of the ammonification product is extracted and put into anaerobic tank 1, and 2 L of anaerobic activated sludge is inoculated. The reaction is carried out for 36 h, mainly ammonia oxidation, and the supernatant of ammonia oxidation product is obtained. 6. The supernatant of the ammonia oxidation product is extracted and put into anaerobic tank 2. The inoculated sludge is anaerobic ammonia oxidation activated sludge and denitrification sludge, of which 1.2 L of anaerobic ammonia oxidation activated sludge and 0.8 L of denitrification sludge are used. Anaerobic ammonia oxidation occurs and the reaction takes 36 h. The main reaction is anaerobic ammonia oxidation and some denitrification. The supernatant of the anaerobic ammonia oxidation product enters the next reaction. 7. The supernatant of the anaerobic ammonia oxidation product enters the next aerobic tank 2, and 2L of aerobic activated sludge is inoculated. The dissolved oxygen is controlled to be 0.15mg / L by aeration. The reaction takes 8 hours, during which nitrification and short-cut nitrification mainly occur. The supernatant of the short-cut nitrification product enters the next reaction. 8. The supernatant from the short-cut nitrification products enters aerobic tank 3, inoculated with 1.5 L of aerobic activated sludge. Secondary short-cut nitrification is performed for the first 30 days, followed by short-cut denitrification after 30 days. During the secondary short-cut nitrification, the dissolved oxygen content is 0.08 mg / L, and the hydraulic retention time is 8 h. During the short-cut denitrification, aeration is stopped, and the hydraulic retention time is 16 h. The COD of the supernatant is then measured. Cr If the concentration is less than 1000 mg / L, the supernatant proceeds to the next reaction; if the COD of the supernatant is... CrFor concentrations greater than or equal to 1000 mg / L, reflux for ammonia oxidation; 9. The supernatant from secondary short-cut nitrification or short-cut denitrification enters the ultrafiltration unit, and the retained sludge enters anaerobic tank 1. The total sludge return flow rate is 40 L (the retained sludge is circulated between anaerobic tank 1 and ultrafiltration); the COD of the ultrafiltrate is... Cr Once the concentration reaches approximately 850 mg / L, proceed to the next step. 10. The ultrafiltrate enters the activated carbon tank, which is inoculated with a mixture of anaerobic ammonia oxidizing bacteria and activated carbon (the volume ratio of anaerobic ammonia oxidizing bacteria to activated carbon is 1:5, and the inoculation amount of anaerobic ammonia oxidizing bacteria is 2L). The initial feed solution for activated carbon coupled anaerobic ammonia oxidation is controlled to have an ammonia nitrogen to nitrite nitrogen mass concentration ratio of 3:1. The reaction time is until the specified design standard is reached, and the COD of the supernatant is measured. Cr Discharge shall be carried out if COD of the supernatant is ≤100 mg / L and ammonia nitrogen is ≤25 mg / L; Cr If the concentration is greater than 100 mg / L, it is returned to step 8) for secondary short-cut nitrification or short-cut denitrification; when the supernatant of activated carbon coupled anaerobic ammonia oxidation is discharged, and the volume ratio of the remaining sludge to the volume of the reaction vessel exceeds 1:2, the remaining sludge is returned to anaerobic tank 1 for ammonia oxidation.

[0057] The overall reaction time of the entire system is 7-9 days. The system's nitrogen removal efficiency is 98.6% (influent (total nitrogen in influent - total nitrogen in effluent) / total nitrogen in influent, the same below), and no additional carbon source is required.

[0058] Example 2 Influent COD Cr The average concentration was 18413 mg / L, with an average ammonia nitrogen content of 744 mg / L and an average total nitrogen content of 937 mg / L. The influent flow rate was controlled at 5 mL / s. The test water came from the leachate collection pond of the incineration plant.

[0059] 1. After the incineration leachate is collected, it is placed in a buffer tank and anaerobic activated sludge at a volume ratio of 1% is added. The temperature is room temperature, with a fluctuation range of about 16~28℃, pH 7.0, and the reaction is carried out for 12 hours to buffer the leachate. When the sludge in the buffer tank is full, it is discharged into the sludge tank. 2. After the buffer tank is full, the sludge is transferred to the anaerobic fermentation tank. Anaerobic activated sludge is inoculated into the anaerobic fermentation tank at a rate of 50%. The reaction temperature is room temperature, with a fluctuation range of approximately 16~28℃, pH 7.0, and the reaction time is 10 hours for anaerobic fermentation. After the sludge in the anaerobic fermentation tank is full, it is discharged into the sludge tank. 3. After the anaerobic fermentation tank is full, it enters the next reactor, the flocculation sedimentation tank, for flocculation and sedimentation. PAC is added at a concentration of 50 mg / L, and the reaction is carried out for 2 hours. The reaction solution undergoes flocculation and sedimentation. After the sludge in the flocculation sedimentation tank is full, it is discharged into the sludge tank. 4. After the flocculation sedimentation tank is full, the sludge enters aerobic tank 1 for ammoniation (aerobic ammoniation). 10% aerobic activated sludge is inoculated, and dissolved oxygen is controlled at approximately 0.1 mg / L. The reaction lasts 1.5 hours, during which ammoniation and partial ammonia oxidation occur, and COD is detected. Cr After being reduced to 2500 mg / L, it flowed into anaerobic tank 1; COD Cr If the sludge does not meet the standards, it is returned to step 2 for anaerobic fermentation; once the sludge in aerobic tank 1 is full, it is discharged into the sludge tank. 5. After the reaction in aerobic tank 1 is completed, the sludge flows into anaerobic tank 1 and is inoculated with 40% anaerobic activated sludge. The reaction lasts for 36 hours, during which ammonia oxidation is the main reaction. When the sludge in anaerobic tank 1 is full, it is discharged into the sludge tank. 6. After anaerobic tank 1 is full, the sludge enters anaerobic tank 2. The sludge is a mixture of anaerobic ammonia oxidation sludge and denitrification sludge, with a volume ratio of anaerobic ammonia oxidation sludge to denitrification sludge of 3:2. The reaction takes 36 hours, during which anaerobic ammonia oxidation and partial denitrification mainly occur. After anaerobic tank 2 is full, the sludge is discharged into the sludge tank. 7. After the anaerobic tank 2 is full, it enters the next step, the aerobic tank 2, and is inoculated with 20% aerobic activated sludge with a dissolved oxygen content of 0.15 mg / L. The reaction takes 8 hours, during which nitrification and short-cut nitrification mainly occur. After the sludge in the aerobic tank 2 is full, it is discharged into the sludge tank. 8. After aerobic tank 2 is full, the sludge enters aerobic tank 3 and is inoculated with 20% aerobic activated sludge for secondary short-cut nitrification or short-cut denitrification (secondary short-cut nitrification is performed 30 days before startup, and short-cut denitrification is performed 30 days after startup). During secondary short-cut nitrification, the dissolved oxygen content is 0.08 mg / L, and the reaction time is 8 hours. During short-cut denitrification, aeration is stopped for 16 hours. After aerobic tank 3 is full, the sludge is returned to anaerobic tank 1. The total return flow rate is 1 / 6 of the influent flow rate, which ensures a thorough reaction, prevents bacterial death, and accelerates startup. 9. After the aerobic tank 3 is full, the sludge enters the ultrafiltration device to further retain the sludge. The retained sludge enters the anaerobic tank 1. The total sludge return ratio is 5:1. The ultrafiltrate enters the next step. 10. The ultrafiltrate enters the activated carbon tank, which is inoculated with a mixture of anaerobic ammonia-oxidizing bacteria and activated carbon (bacteria to activated carbon volume ratio of 1:12). The inoculation amount is sufficient to fill the entire reactor. The mass concentration ratio of ammonia nitrogen to nitrate nitrogen in the initial feed solution is controlled at 3:1. The reaction time continues until the COD and ammonia nitrogen of the leachate reach the design discharge standards (GB / T 31962-2015 or GB16889-2024). When the suspended solids (SS) of the excess sludge effluent from the activated carbon tank exceeds the design standard value, it is recycled to anaerobic tank 1.

[0060] The entire system has a reaction time of 15 days. The system has a nitrogen removal efficiency of 98.6% and requires no additional carbon source.

[0061] Comparative Example 1 Except for omitting ammoniation in aerobic tank 1 in step 4, the rest is the same as in Example 1, that is, the following process is adopted: Buffer + Anaerobic Fermentation + Flocculation and Sedimentation + Ammonia Oxidation + Anaerobic Ammonia Oxidation + Short-cut Nitrification + Short-cut Denitrification + Ultrafiltration + Activated Carbon Coupled with Anaerobic Ammonia Oxidation.

[0062] The results showed that the start-up failed because the process lacked the ammoniation reaction in aerobic tank 1, the COD concentration in the system filtrate was too high, and the required COD to ammonia nitrogen ratio was not met, resulting in excessive toxicity to anaerobic ammonia oxidizing bacteria and thus the start-up failure.

[0063] Comparative Example 2 Denitrification-zeolite aerated biological filter partial nitrification-anaerobic ammonia oxidation combined process (see [Chen Xiaozhen, Wang Xiaojun, Karasuta Chayangkun, et al. Denitrification-high-efficiency partial nitrification-anaerobic ammonia oxidation process for treating leachate from old landfills [J]. Environmental Science, 2020, 41(1): 345–352.]).

[0064] During the start-up phase, the influent to each reactor is simulated wastewater, NH4+. + -N is provided by NH4Cl, NO2 - -N was provided by NaNO2, and the carbon source was provided by glucose. The leachate from the aged waste used in the experiment was taken from a municipal solid waste landfill in Guangzhou. This landfill has been in operation for over 20 years, with a leachate production of approximately 400 m³. 3 ·d -1 .

[0065] The process start-up time is 130 days, the system denitrification efficiency is 97.2%, and an additional carbon source glucose is added at a dosage of 700 mg / L. This method is not suitable for incinerating landfill leachate. The nitrification process has problems such as low treatment efficiency, poor stability, and easy sludge bulking.

[0066] Comparative Example 3 A two-stage process of PN / ANAMMO + PD / ANAMMOX (see [Wang Z, Zhang L, Zhang F, et al. A continuous-flow combined process based on partial nitrification-anammox and partial denitrification-anammox (PN / A+PD / A) for enhanced nitrogen removal from mature landfill leachate[J]. Bioresource Technology, 2020, 297:122483.]).

[0067] A continuous flow combined process consisting of one continuous flow reactor and two UASB reactors was used for deep denitrification of leachate. The PN reactor was divided into eight units on average, including one anoxic zone and seven aerobic zones. Compressed air was injected into the remaining aerobic zones under the control of a gas flow meter. The landfill leachate was divided into a PN influent tank, an anaerobic ammonium oxidation reactor, and a partial denitrification-anaerobic ammonium oxidation reactor. The operating volumes of the A / O reactor, Anammox reactor, and PD-Anammox reactor were 10.5 L, 10 L, and 3.5 L, respectively. Polypropylene and sponge carriers were fixed together with fishing line, with a filling volume of 35%. The SRT of the A / O reactor, Anammox reactor, and PD-Anammox reactor were 25 d, 70 d, and 65 d, respectively. The HRT of the A / O reactor, Anammox reactor, and PD-Anammox reactor were 33.6 h, 26.7 h, and 21 h, respectively.

[0068] The process has a start-up time of 120 days, a denitrification efficiency of 98.8%, requires the addition of an additional carbon source, and has a maximum influent concentration of 2448 mg / L. It is not suitable for incinerating leachate with higher concentrations, and it also has a large footprint, poor stability, and a long start-up time.

[0069] Comparative Example 4 Denitrification-short-cut nitrification-anaerobic ammonium oxidation process (see [Wang Fan, Lu Mingyu, Yin Jiqiang, et al. Denitrification and carbon removal performance of denitrification-short-cut nitrification-anaerobic ammonium oxidation process for treating late-stage landfill leachate [J]. Environmental Science, 2018, 39(8): 3782–3788.]).

[0070] Leachate from late-stage landfills was treated using a combination of a UASB reactor and a PN-ANAMMOX integrated zoned reactor. Both reactors were constructed of plexiglass. The DN-UASB reactor had an effective volume of 1.8 L, while the PN-ANAMMOX integrated reactor had effective volumes of 10.25 L in the PN zone and 1.4 L in the ANAMMOX zone, with a sedimentation zone volume of 1.92 L. The entire reactor was placed in a shaded and insulated environment, with the temperature maintained at 31–34 °C using a temperature-controlled air bath. The landfill leachate was pumped into the bottom of the DN reactor by a peristaltic pump and flowed into the PN-ANAMMOX reactor from the top. Partial short-cut nitrification occurred in the PN zone before the leachate entered the ANAMMOX zone for the ANAMMOX reaction. A portion of the effluent was returned to the bottom of the DN reactor by a peristaltic pump to neutralize the NO3 produced by the ANAMMOX reaction. - -N and some organic matter in the leachate are removed through denitrification.

[0071] According to the data in the article, after approximately 85 days, the concentrations of ammonium nitrogen and nitrate nitrogen in the effluent stabilized, remaining at low levels with minimal fluctuations, suggesting a start-up time of approximately 85 days. The system's nitrogen removal efficiency was 98.6%. However, when treating high-concentration ammonia nitrogen wastewater, additional nitrates were generated. When treating low-concentration ammonia nitrogen wastewater, PN (nitric acid) was difficult to control, making start-up challenging, resulting in poor stability and a narrow range of applications.

[0072] Comparative Example 5 Short-cut denitrification / anammox combined process (see [Du R, Cao S, Peng Y, et al. Combined partial denitrification (PD)-anammox: a method for high nitrate wastewater treatment[J]. Environment International, 2019, 126: 707–716.]).

[0073] A simultaneous treatment experiment was conducted for over seven months on high-nitrate nitrogen wastewater and municipal sewage. The PD reactor operated in batch mode with a cycle time of 120 minutes. This included NO3. --N and municipal wastewater influent stages (8 min), external carbon source addition (2 min), stirring (15-20 min), settling (10 min), discharge (5 min), idling (75-80 min). SBR operation is controlled by a timer. Hydraulic retention time (HRT) of the PD reactor is 3.6 h for the first stage and 3.1 h for the second and third stages. The effluent rate of the anammox UASB reactor with continuous feed ranges from 1.4 L / h to 1.6 L / h. The HRT of anammox UASB varies between 2.3 and 2.0 h depending on the operating conditions of the PD reactor. Three different phase properties can be identified through denitrification. In the first stage (days 1-68), the PD-Anammox system was started up and the input of nitrate and municipal wastewater was optimized. Because the biological organic carbon source involved in municipal wastewater is insufficient to completely convert NO3. - -N; Sodium acetate was added to the PD reactor as an external carbon source. In the second stage (days 69-147), the recovery of anammox performance was explored after being inhibited by excess organic matter. In the third stage (days 148-215), the stability of the PD-Anammox process was investigated. To examine the nitrogen removal performance of PD and PD-Anammox processes, the PD temperature and anammox reactor were uncontrolled under actual conditions, with the temperature ranging from 14.8℃ to 28.2℃, operating at ambient temperature and varying with the seasons.

[0074] Based on the total nitrogen concentrations of the influent and effluent, and considering the proportion of anaerobic ammonia oxidation in the total nitrogen removal rate, it was determined that the system reached stable operation after approximately 210 days. Therefore, based on degradation data, the process start-up time was estimated to be approximately 210 days. The system's nitrogen removal efficiency is 95.6%, requiring the addition of sodium acetate at a dosage of 212.5 mg / L. It is not suitable for high-concentration incineration leachate, has numerous control parameters, presents significant practical challenges, exhibits poor stability, requires a segmented design, occupies a large area, and has a long start-up time.

[0075] Although the above embodiments have provided a detailed description of the present invention, they are only some embodiments of the present invention, and not all embodiments. People can obtain other embodiments based on these embodiments without creative effort, and these embodiments all fall within the protection scope of the present invention.

Claims

1. A rapid start-up method for anaerobic ammonia oxidation treatment of landfill leachate, characterized in that, Includes the following steps: 1) Anaerobic activated sludge is inoculated into the leachate from incineration of landfills to buffer the leachate and obtain buffered leachate; 2) Inoculate the buffer leachate with anaerobic activated sludge and carry out anaerobic fermentation to obtain anaerobic fermentation products; 3) The anaerobic fermentation products are subjected to flocculation and precipitation to obtain the supernatant of the flocculated products; 4) inoculating the flocculated product supernatant with aerobic activated sludge, ammoniating until the supernatant has a COD Cr ≤ 2500 mg / L, obtaining an ammoniated product supernatant; 5) Inoculate anaerobic activated sludge into the supernatant of the ammonification product and carry out ammonia oxidation to obtain the supernatant of the ammonia oxidation product; 6) Inoculate the supernatant of the ammonia oxidation product with anaerobic ammonia oxidation activated sludge and denitrification sludge to carry out anaerobic ammonia oxidation and obtain the supernatant of the anaerobic ammonia oxidation product. 7) Inoculate aerobic activated sludge into the supernatant of the anaerobic ammonia oxidation product and carry out short-cut nitrification to obtain the supernatant of the short-cut nitrification product; 8) Inoculate aerobic activated sludge into the supernatant of the short-cut nitrification products to perform secondary short-cut nitrification or start short-cut denitrification until the COD of the supernatant reaches a certain level. Cr With a concentration ≤1000 mg / L, a secondary short-cut nitrification supernatant or a short-cut denitrification supernatant is obtained; A second short-cut nitrification is carried out 30 days before startup, and a short-cut denitrification is carried out 30 days after startup. 9) The supernatant from the secondary short-cut nitrification or the supernatant from the short-cut denitrification is subjected to ultrafiltration to obtain sludge and ultrafiltrate. 10) Inoculate the ultrafiltrate with anaerobic ammonia-oxidizing bacteria and activated carbon to perform activated carbon-coupled anaerobic ammonia oxidation until the COD of the supernatant is [value missing]. Cr Discharge shall be ≤100mg / L and ammonia nitrogen ≤25mg / L; In the initial feed solution for activated carbon coupled anaerobic ammonia oxidation, the mass concentration ratio of ammonia nitrogen to nitrite nitrogen is 2:1 to 3:

1.

2. The fast startup method according to claim 1, characterized in that, In step 1), the COD of the incineration leachate is... Cr The ammonia nitrogen content of the incineration leachate is ≤25000mg / L, and the buffer temperature is 1200~1800mg / L; the buffer pH is 7~7.2; and the buffering time is 12~24h. In step 2), the temperature of the anaerobic fermentation is 10~40℃, the pH value of the anaerobic fermentation is 7~7.2, and the hydraulic retention time of the anaerobic fermentation is 10~36h. In step 3), the flocculant used for flocculation and sedimentation includes at least one of polyaluminum chloride, iron salt, and polyacrylamide; the working concentration of the polyaluminum chloride is 50~150 mg / L; and the flocculation and sedimentation time is 1~2 h. In step 4), during the ammoniation process, the dissolved oxygen concentration is greater than or equal to 0.1 mg / L; the hydraulic retention time for ammoniation is 1.5~10 h. After ammoniaation, the COD of the supernatant Cr When the concentration is greater than 2500 mg / L, reflux to step 2) for anaerobic fermentation.

3. The fast startup method according to claim 1, characterized in that, In step 5), the hydraulic residence time for ammonia oxidation is 15-48 hours.

4. The fast startup method according to claim 1, characterized in that, In step 6), the volume ratio of the anaerobic ammonia oxidation activated sludge to the denitrification sludge is 3:2 to 1:1; the pH value of the anaerobic ammonia oxidation is 6.5 to 7.2; and the hydraulic retention time of the anaerobic ammonia oxidation is 20 to 48 hours. In the initial feed solution of the anaerobic ammonia oxidation, COD Cr The mass concentration ratio of NH3 to NH3 is 5:2 to 25:

7.

5. The fast startup method according to claim 1, characterized in that, In step 7), the dissolved oxygen content during the short-cut nitrification process is 0.08~0.42 mg / L; the hydraulic retention time of the short-cut nitrification is 8~16 h.

6. The fast startup method according to claim 1, characterized in that, In step 8), during the secondary short-cut nitrification process, the dissolved oxygen content is 0.08~0.1 mg / L, and the hydraulic retention time is 8 h. During the short-cut denitrification process, aeration is stopped, and the hydraulic retention time is 5-16 hours. When the COD of the supernatant Cr When the concentration is greater than 1000 mg / L, reflux to step 5) for ammonia oxidation.

7. The fast startup method according to claim 1, characterized in that, In step 9), the intercepted sludge is returned to step 5) for ammonia oxidation.

8. The fast startup method according to claim 1, characterized in that, In step 10), the volume ratio of the anaerobic ammonia-oxidizing bacteria to activated carbon is 1:(5~12). When the COD of the supernatant Cr If the concentration is greater than 100 mg / L, reflux to step 8) for secondary short-cut nitrification or short-cut denitrification; When the supernatant from activated carbon coupled anaerobic ammonia oxidation is discharged, and the volume of the remaining sludge exceeds 1 / 2 of the volume of the reaction vessel, the remaining sludge is returned to step 5) for ammonia oxidation.

9. A method for treating landfill leachate, characterized in that, Includes the following steps: (1) Anaerobic fermentation of incineration leachate to obtain anaerobic fermentation products; (2) The anaerobic fermentation products are subjected to flocculation and precipitation to obtain the supernatant of the flocculated products; (3) The supernatant of the flocculation product is aminated to obtain the supernatant of the aminated reaction product; (4) The supernatant of the amination reaction product is subjected to ammonia oxidation to obtain the supernatant of the ammonia oxidation product; (5) Anaerobic ammonia oxidation is performed on the supernatant of the ammonia oxidation product to obtain an anaerobic ammonia oxidation product supernatant; (6) The supernatant of the anaerobic ammonia oxidation product is subjected to short-cut nitrification to obtain the supernatant of the short-cut nitrification reaction product; (7) The supernatant of the short-cut nitrification reaction product is subjected to short-cut denitrification to obtain the supernatant of the short-cut denitrification reaction product; (8) The supernatant of the short-cut denitrification reaction product is subjected to ultrafiltration to obtain ultrafiltrate; (9) The ultrafiltrate is subjected to activated carbon coupled anaerobic ammonia oxidation reaction until the supernatant of the activated carbon coupled anaerobic ammonia oxidation product meets the discharge standard and is then discharged.

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