CN111592103B - Treatment method of livestock and poultry breeding wastewater - Google Patents

Treatment method of livestock and poultry breeding wastewater Download PDF

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CN111592103B
CN111592103B CN202010355689.5A CN202010355689A CN111592103B CN 111592103 B CN111592103 B CN 111592103B CN 202010355689 A CN202010355689 A CN 202010355689A CN 111592103 B CN111592103 B CN 111592103B
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tank
treatment
wastewater
sludge
strengthening
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CN111592103A (en
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汤江武
李园成
孙宏
沈琦
姚晓红
王新
吴逸飞
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Zhejiang Academy of Agricultural Sciences
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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
    • 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
    • C02F2101/20—Heavy metals or heavy metal compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/16—Total nitrogen (tkN-N)
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/18—PO4-P

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  • Activated Sludge Processes (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

The invention provides a treatment method of livestock and poultry breeding wastewater, which belongs to the technical field of wastewater treatment, and the livestock and poultry breeding wastewater enters a water collecting tank after solid-liquid separation; the pretreated wastewater is treated by an improved A/O process to achieve qualified effluent. The improved A/O process comprises the steps of enabling the wastewater to sequentially enter a primary strengthening tank, an A/O treatment tank, a secondary sedimentation tank, a secondary strengthening tank and a dosing flocculation tank, wherein activated sludge and/or functional microorganisms are respectively inoculated in the primary strengthening tank, the A/O treatment tank and the secondary strengthening tank; the A/O treatment tank comprises an anoxic tank and an aerobic tank, two-stage backflow is set in the improved A/O treatment stage, nitrification liquid backflow and sludge backflow are set, the nitrification liquid backflow is mixed liquid at the tail end of the aerobic tank and flows back to the anoxic tank, and the sludge backflow is partial residual sludge of the secondary sedimentation tank and flows back to the primary strengthening tank and/or the anoxic tank. The improved A/O process has the advantages of wide trial range, strong load resistance, low energy consumption, excellent operation effect and good effluent quality.

Description

Treatment method of livestock and poultry breeding wastewater
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a treatment method of livestock and poultry breeding wastewater.
Background
Livestock and poultry breeding is the backbone industry of agriculture in China, and plays an important role in maintaining stable supply of livestock products, activating rural economy and improving the living standard of people. However, with the continuous development of livestock and poultry breeding industry, the pollution problem of the livestock and poultry breeding industry is increasingly prominent, COD, total nitrogen and total phosphorus in the livestock and poultry breeding wastewater respectively account for 95.78%, 37.89% and 56.30% of non-point source pollution, and the pollution of the livestock and poultry breeding wastewater becomes one of three pollution sources which are parallel to industrial wastewater and domestic wastewater. The pollution generated by livestock and poultry breeding becomes a main surface pollution source in rural areas in China, and the pollution caused by a plurality of important water source areas, rivers and lakes cannot be ignored.
Compared with domestic wastewater, the livestock and poultry breeding wastewater contains high-concentration pollutants such as COD, nitrogen, phosphorus, suspended matters (SS) and the like, and the pollution load is very high. At present, the common treatment methods of the biogas slurry in the pig farm include two main methods: firstly, natural treatment is carried out, and a biological pond method and an artificial wetland method are common; the other is an industrial treatment technology, which is commonly referred to as UASB process, SBR process, A/O process and the like. However, the existing domestic and foreign livestock and poultry breeding wastewater treatment process generally has the problems of poor effluent stability, low denitrification efficiency and the like. In the fierce market economic competition, the breeding industry with small profit is difficult to invest a large amount of funds to treat the discharged wastewater, so that the overall treatment level and treatment rate of the Chinese livestock and poultry breeding wastewater are low, the livestock and poultry breeding wastewater is discharged when not reaching the standard, and the environment is seriously polluted. Therefore, aiming at the water quality characteristics of livestock and poultry breeding wastewater in China, a harmless livestock and poultry breeding wastewater treatment technology with high treatment efficiency, strong stability, low cost and the like needs to be developed urgently to effectively treat the pollution problem of the livestock and poultry breeding wastewater.
Disclosure of Invention
The invention aims to provide a method for treating livestock and poultry breeding wastewater, which has the advantages of low energy consumption, low sludge yield, high load, stable water discharge, good water quality of discharged water and stable operation in winter.
The technical scheme adopted by the invention for realizing the purpose is as follows:
an improved A/O process comprises the steps that wastewater enters an improved A/O treatment system, the improved A/O treatment system comprises a primary strengthening pool, an A/O treatment pool, a secondary sedimentation pool, a secondary strengthening pool and a dosing flocculation pool which are sequentially connected in the water flow direction, and the wastewater sequentially enters the primary strengthening pool, the A/O treatment pool, the secondary sedimentation pool, the secondary strengthening pool and the dosing flocculation pool to achieve qualified effluent;
wherein, the first-stage strengthening pool, the A/O treatment pool and the second-stage strengthening pool are respectively inoculated with activated sludge and/or functional microorganisms;
the A/O treatment tank comprises an anoxic tank and an aerobic tank, two-stage backflow is set in the improved A/O treatment stage, nitrification liquid backflow and sludge backflow are set, the nitrification liquid backflow is mixed liquid at the tail end of the aerobic tank and flows back to the anoxic tank, and the sludge backflow is partial residual sludge of the secondary sedimentation tank and flows back to the primary strengthening tank and/or the anoxic tank. The invention adopts the activated sludge to pre-treat the wastewater before the A/O treatment, can reduce the pollutant load and reduce the biochemical treatment difficulty of the wastewater in the A/O treatment stage, thereby improving the operation stability of the improved A/O treatment system and achieving the effect of stabilizing the effluent; according to the invention, the wastewater is treated by adopting the activated sludge and/or the functional microorganisms after the A/O treatment, so that pollutants in the water can be further removed, the sewage treatment efficiency is efficiently improved, and the water is stably discharged. The improved A/O treatment process is stable and reliable, realizes the high-efficiency treatment of carbon, nitrogen and phosphorus and the reduction of tetracycline and heavy metal resistance genes in water, has great advantages in the aspects of energy consumption, investment, treatment cost and treatment effect, and has higher popularization and application values; in addition, the improved A/O treatment process is less influenced by external temperature, can stably run in winter, can better solve the problem of low-temperature nitrification efficiency of the activated sludge, has good denitrification and dephosphorization effects and good effluent quality.
According to one embodiment of the invention, the aerobic tank is divided into 1-8 sections. Preferably, the aerobic tank is divided into 3-6 sections. The aerobic tank is divided into a plurality of tanks which can distribute the aquaculture wastewater load, reduce the impact of the concentration change of the influent pollutants caused by various reasons on the improved A/O treatment system, and strengthen the impact load resistance of the system, thereby improving the operation stability of the improved A/O treatment system and achieving the effect of stabilizing effluent.
According to one embodiment of the invention, the reflux ratio of the nitrifying liquid is 1:2-10, and the reflux ratio of the sludge is 1: 0.5-2.
According to one embodiment of the invention, the sludge settling ratio is 30-80% after the treatment system enters a full load stable operation state.
According to one embodiment of the invention, the HRT of the primary strengthening pool is 1-2d, the HRT of the A/O stage is 6-10d, and the HRT of the secondary strengthening pool is 0.5-1 d.
The invention also aims to provide application of the improved A/O process in treating high ammonia nitrogen wastewater, wherein the high ammonia nitrogen wastewater is livestock and poultry breeding wastewater, slaughter wastewater, kitchen wastewater, municipal wastewater, monosodium glutamate production wastewater or sludge digestion liquid.
It is still another object of the present invention to provide the use of the improved a/O process treatment in treating livestock and poultry farming wastewater.
According to an embodiment of the present invention, treating the livestock and poultry farming wastewater includes treating in winter.
The invention also aims to provide a method for treating livestock and poultry breeding wastewater, which comprises the following steps:
in the pretreatment stage, the livestock and poultry breeding wastewater is subjected to effective solid-liquid separation by a grid and a hydraulic vibrating screen or an air floatation device, most of the manure in the wastewater is removed, so that the generation amount of sediment and scum in the subsequent treatment link is reduced, the concentration of pollutants in the wastewater is reduced, solid matters can be conveyed to a composting workshop, and squeezed raw water enters a subsequent treatment system.
In the improved A/O treatment stage, indexes such as COD, ammonia nitrogen and TP in the pretreated wastewater are effectively removed by using the improved A/O process, so that qualified effluent is obtained.
The invention adopts an improved A/O process to treat the pig farm breeding wastewater, the index of the treated wastewater is superior to the requirement of livestock and poultry breeding pollutant discharge standard (GB 18596-.
According to one embodiment of the invention, the treatment method has a COD removal rate of more than 99.0%, an ammonia nitrogen removal rate of more than 99.5%, a TP removal rate of more than 99.0%, a tetracycline antibiotic removal rate of more than 86%, and a part of heavy metal removal rate of more than 90%.
Compared with the prior art, the invention has the beneficial effects that: according to the invention, the culture wastewater is pretreated by adopting the activated sludge and/or functional microorganisms before the A/O treatment, so that the pollutant load can be reduced, the impact of the concentration change of the influent pollutants on the A/O treatment system is reduced, the impact load resistance of the system is enhanced, the biochemical treatment difficulty of the sewage in the A/O treatment stage is reduced, the running stability of the A/O treatment system is improved, and the effect of stabilizing effluent is achieved; according to the invention, the wastewater is treated by adopting the activated sludge and/or the functional microorganisms after the A/O treatment, so that pollutants in the water can be further removed, the sewage treatment efficiency is efficiently improved, and the effluent is stabilized; simultaneously at terminal flocculation sedimentation tank, select for use high-efficient compound water purification agent (this high-efficient compound water purification agent provides in the patent document that patent application number is 201710305839X, its composition and preparation process are like this patent, this application is no longer repeated) and PAM combined action, get rid of suspended solid, colourity and total phosphorus in the waste water, reach qualified effluent. The improved A/O treatment process is stable and reliable, realizes the high-efficiency removal of carbon, nitrogen and phosphorus and the reduction of tetracycline antibiotics and partial heavy metal resistance genes in water, has great advantages in the aspects of energy consumption, investment, treatment cost and treatment effect, has higher popularization and application values, and can be used for treating livestock and poultry breeding wastewater, slaughter wastewater, kitchen wastewater, urban domestic wastewater, monosodium glutamate production wastewater or sludge digestive juice and the like; in addition, the improved A/O treatment process is less influenced by the external temperature due to longer hydraulic retention time, higher sludge concentration and more appropriate process parameters, so that the system can stably run in winter, the problem of low-temperature nitrification efficiency of the activated sludge is solved, and the effluent effect is good.
The invention adopts the technical scheme to provide the method for treating the livestock and poultry breeding wastewater, overcomes the defects of the prior art, and has reasonable design and convenient operation.
Drawings
FIG. 1 is a flow chart of the treatment of wastewater from pig farming in example 2 of the present invention;
FIG. 2 shows tetracycline antibiotic resistance genes for water inlet and outlet in example 2 of the present invention;
FIG. 3 shows heavy metal resistance genes of the water inlet and outlet portions in example 2 of the present invention;
FIG. 4 shows changes in the dehydrogenase activity of the activated sludge mixed liquid and the electron transport system activity in the aerobic tank in test example 1 of the present invention;
FIG. 5 shows the change of extracellular polymeric substance in the aerobic tank in test example 1 of the present invention;
FIG. 6 shows the sludge sedimentation ratio of the activated sludge in the aerobic tank in test example 1 of the present invention.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings, which illustrate embodiments of the present invention. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used in the description of the invention herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.
The invention provides an improved A/O process, which comprises the steps that wastewater enters an improved A/O treatment system, wherein the improved A/O treatment system comprises a primary strengthening pool, an A/O treatment pool, a secondary sedimentation pool, a secondary strengthening pool and a dosing flocculation pool which are sequentially connected in the water flow direction, so that the wastewater sequentially enters the primary strengthening pool, the A/O treatment pool, the secondary sedimentation pool, the secondary strengthening pool and the dosing flocculation pool to achieve qualified effluent;
wherein, the first-stage strengthening pool, the A/O treatment pool and the second-stage strengthening pool are respectively inoculated with activated sludge and/or functional microorganisms;
the A/O treatment tank comprises an anoxic tank and an aerobic tank, two-stage backflow is set in the improved A/O treatment stage, nitrification liquid backflow and sludge backflow are set, the nitrification liquid backflow is mixed liquid at the tail end of the aerobic tank and flows back to the anoxic tank, and the sludge backflow is partial residual sludge of the secondary sedimentation tank and flows back to the primary strengthening tank and/or the anoxic tank. According to the embodiment, the wastewater is pretreated by adopting the activated sludge and/or the functional microorganisms before the A/O treatment, so that the pollutant load can be reduced, the biochemical treatment difficulty of the wastewater in the A/O treatment stage can be reduced, and the influence on an A/O biochemical system caused by the water quality fluctuation of the wastewater in a pig farm can be reduced, so that the running stability of the A/O treatment system is improved, and the effect of stabilizing the effluent is achieved; according to the embodiment, the wastewater is treated by adopting the activated sludge and/or the functional microorganisms after the A/O treatment, so that pollutants in the water can be further removed, the sewage treatment efficiency is efficiently improved, and the effluent is stabilized; the embodiment improves the A/O treatment process, is stable and reliable, realizes the high-efficiency treatment of carbon, nitrogen and phosphorus and the reduction of tetracycline antibiotics and part of heavy metal resistance genes in the water body, has great advantages in the aspects of energy consumption, investment, treatment cost and treatment effect, and has higher popularization and application values; in addition, the improved A/O treatment process can stably run in winter, can better solve the problem of low-temperature nitrification efficiency of the activated sludge, and has good denitrification and dephosphorization effects and good water outlet effects.
In one embodiment of the invention, the aerobic tank is divided into 1-8 sections. Preferably, the aerobic tank is divided into 3-6 sections. The aerobic tank is divided into a plurality of tanks which can distribute the aquaculture wastewater load, reduce the impact of the concentration change of the influent pollutants caused by various reasons on the improved A/O treatment system, and strengthen the impact load resistance of the system, thereby improving the operation stability of the improved A/O treatment system and achieving the effect of stabilizing effluent.
In one embodiment of the invention, the reflux ratio of the nitrifying liquid is 1:2-10, and the reflux ratio of the sludge is 1: 0.5-2.
In one embodiment of the present invention, the sludge settling ratio is 30-80% after the treatment system enters a full load stable operation state.
In one embodiment of the present invention, the HRT of the primary strengthening tank is 1-2d, the HRT of the A/O stage is 6-10d, and the HRT of the secondary strengthening tank is 0.5-1 d.
In one embodiment of the present invention, the improved A/O process specifically comprises the following steps:
and in the primary strengthening treatment stage, the wastewater enters a primary strengthening tank and is subjected to primary strengthening treatment by activated sludge and/or functional microorganisms, so that the pollutant load can be reduced, the impact of the concentration change of the influent pollutants on an A/O treatment system is reduced, and the biochemical treatment difficulty of the wastewater in the A/O treatment stage is reduced.
In the A/O treatment stage, the wastewater after the primary strengthening treatment is sent to an anoxic tank, denitrifying bacteria in the anoxic tank degrade macromolecular organic matters into micromolecular organic matters, and the biodegradability of the wastewater during rear-end aerobic treatment is improved; the ammonia nitrogen is converted into nitrate in the aerobic nitrification process of the rear-section aerobic tank, and the nitrate is returned to the anoxic tank through reflux to perform denitrification so as to complete denitrification circulation; meanwhile, the metabolism of aerobic microorganisms is utilized to decompose organic matters in the wastewater into carbon dioxide and water; in a word, the A/O pool finally converts ammonia nitrogen, organic matters and the like in the wastewater into substances such as nitrogen, carbon dioxide, water and the like respectively for removal under the action of denitrifying bacteria, nitrifying bacteria and aerobic microorganisms.
A secondary strengthening treatment stage, namely precipitating the wastewater after the A/O treatment in a secondary sedimentation tank, and enabling supernatant to flow into a secondary strengthening tank for secondary strengthening treatment; whether activated sludge and/or functional microorganisms are inoculated or not can be selected according to the water quality of the supernatant, if the water quality is good, the activated sludge and/or the functional microorganisms are not inoculated for direct aeration, and if the water quality is not good, the activated sludge and/or the functional microorganisms are inoculated, so that pollutants in water are further removed, the wastewater treatment efficiency is efficiently improved, the water outlet is stabilized, and the water outlet index is far superior to the strictest discharge standard.
And in the flocculation treatment stage, the wastewater after the secondary strengthening treatment is further treated by a dosing flocculation tank to achieve qualified effluent. The high-efficiency composite water purifying agent and the flocculating agent in the dosing flocculation sedimentation tank act together, so that suspended matters, chromaticity and total phosphorus in the wastewater can be removed, and qualified effluent is obtained; and (3) pumping the residual sludge in the secondary sedimentation tank and the dosing flocculation sedimentation sludge to a sludge concentration tank through a water pump for storage, carrying out mechanical dehydration, transporting a mud cake outwards or carrying out fermentation treatment, and refluxing dehydration filtrate to the system.
The low temperature can inhibit the growth of nitrifying bacteria, denitrifying bacteria and phosphorus removing bacteria in the system to different degrees, thereby further influencing the removal effect of COD, ammonia nitrogen and TP in the improved A/O process. Therefore, in order to achieve the biological nitrogen and phosphorus removal effect at low temperature, especially at room temperature of 0-8 ℃, some countermeasures need to be taken, and the inventionIn one embodiment, the ultrafine particle ferric citrate and the zinc gluconate are added into the aerobic tank, and the addition of the particle ferric citrate and the zinc gluconate strengthens an electron transfer system and enzymatic reaction activity in a microorganism body, improves the nitrification capability of nitrifying bacteria, and can enhance the low-temperature nitrification resistance of activated sludge; the mutual matching of the ferric citrate and the zinc gluconate can promote microorganisms in the activated sludge to generate more extracellular polymers with larger volumes, reduce protein components in the extracellular polymers, improve polysaccharide components in the extracellular polymers and improve the sedimentation performance of the activated sludge. In addition, the mutual matching of the ferric citrate and the zinc gluconate can ensure that the phosphorus removing bacteria have higher biological activity, thereby having stronger aerobic phosphorus absorption capacity and Fe3+Can be combined with PO4 3-Insoluble salt is generated by reaction, and phosphorus is further removed. In a word, the problem of low-temperature nitrification efficiency of the activated sludge can be better solved by adding the ultrafine ferric citrate and the zinc gluconate into the aerobic tank, the nitrogen and phosphorus removal effect of the activated sludge is effectively improved under the low-temperature condition, the dosage of the medicament in the dosing flocculation tank is reduced, and the prices of the ferric citrate and the zinc gluconate are lower. Preferably, the concentrations of the ultra-micro ferric citrate and the zinc gluconate are respectively 1-5mg/L and 0.1-2 mg/L. Further, after the treatment system enters a full-load stable operation state, the removal rate of COD (chemical oxygen demand) of the treatment system is at least 99.0%, the removal rate of ammonia nitrogen is at least 99.5%, and the removal rate of TP (total phosphorus) is at least 99%.
In one embodiment of the invention, the high ammonia nitrogen wastewater is livestock and poultry breeding wastewater, kitchen wastewater, municipal wastewater, monosodium glutamate production wastewater or sludge digestive juice.
The embodiment of the invention also provides application of the improved A/O process treatment in treating livestock and poultry breeding wastewater.
In one embodiment of the present invention, treating the livestock and poultry farming wastewater comprises treating in winter.
The embodiment of the invention also provides a treatment method of livestock and poultry breeding wastewater, which comprises the following steps:
in the pretreatment stage, the livestock and poultry breeding wastewater enters a water collecting tank after solid-liquid separation; the waste water enters a septic tank for storage (grids can be added at the front end for treating large-particle floating objects such as plastic bags, injectors and the like), then the dry and clear excrement is effectively separated from solid and liquid by using a vibrating screen and/or a squeezing system and/or an air floatation device, most of excrement residues in the waste water are removed, the generation amount of sediment and scum in the subsequent treatment link is reduced, the concentration of pollutants in the waste water is reduced, solid matters can be conveyed to a composting workshop, and the waste water enters a subsequent treatment system;
in the improved A/O treatment stage, indexes such as COD, ammonia nitrogen and TP in the pretreated wastewater are effectively removed by using the improved A/O process, so that qualified effluent is obtained. The embodiment adopts an improved A/O process to treat the pig farm breeding wastewater, and the treated wastewater has indexes superior to the requirements of livestock and poultry breeding pollutant discharge standard (GB 18596-.
In one embodiment of the present invention, the removal rate of COD is at least 99.0%, the removal rate of ammonia nitrogen is at least 99.5%, the removal rate of TP is at least 99.0%, the removal rate of tetracycline antibiotics is above 86%, and the removal rate of part of heavy metals is above 90%.
The invention is further illustrated by the following examples. It should be understood that the examples are for illustrative purposes only and are not intended to limit the scope and spirit of the present invention.
Example 1:
an improved A/O process, the improved A/O treatment system comprises a primary strengthening tank, an A/O treatment tank, a secondary sedimentation tank, a secondary strengthening tank and a dosing flocculation tank which are sequentially connected in the water flow direction, the A/O treatment tank comprises an anoxic tank and an aerobic tank, and the aerobic tank is divided into 6 sections; respectively inoculating activated sludge in the primary strengthening tank, the A/O treatment tank and the secondary strengthening tank; and two-stage backflow is set in the improved A/O treatment stage, nitrification liquid backflow and sludge backflow are set, the nitrification liquid backflow is that mixed liquor at the tail end of the aerobic tank flows back to the anoxic tank, the sludge backflow is that partial residual sludge in the secondary sedimentation tank flows back to the primary strengthening tank and/or the anoxic tank, the nitrification liquid backflow ratio is 1:6, and the sludge backflow ratio is 1: 1.5. The improved A/O process specifically comprises the following steps:
a first-stage strengthening treatment stage, wherein the wastewater enters a first-stage strengthening tank and is subjected to first-stage strengthening treatment by activated sludge;
in the A/O treatment stage, the wastewater after the primary strengthening treatment is sent to an anoxic tank, denitrifying bacteria in the anoxic tank degrade macromolecular organic matters into micromolecular organic matters, and the biodegradability of the wastewater during rear-end aerobic treatment is improved; the ammonia nitrogen is converted into nitrate in the aerobic nitrification process of the rear-section aerobic tank, and the nitrate is returned to the anoxic tank through reflux to perform denitrification so as to complete denitrification circulation; meanwhile, the metabolism of aerobic microorganisms is utilized to decompose organic matters in the wastewater into carbon dioxide and water;
a secondary strengthening treatment stage, namely precipitating the wastewater after the A/O treatment in a secondary sedimentation tank, and enabling supernatant to flow into a secondary strengthening tank for secondary strengthening treatment; whether activated sludge and/or functional microorganisms are inoculated or not can be selected according to the water quality of the supernatant, if the water quality is good, the sludge and/or the functional microorganisms are not inoculated for direct aeration, and if the water quality is not good, the activated sludge and/or the functional microorganisms are inoculated;
in the flocculation treatment stage, the wastewater after the secondary strengthening treatment is further treated by a dosing flocculation basin, and the dosing flocculation sedimentation basin contains a high-efficiency composite water purifying agent and a flocculating agent to achieve qualified effluent; and (3) pumping the residual sludge in the secondary sedimentation tank and the dosing flocculation sedimentation sludge to a sludge concentration tank through a water pump for storage, carrying out mechanical dehydration, transporting a mud cake outwards or carrying out fermentation treatment, and refluxing dehydration filtrate to the system.
Example 2:
the difference from the embodiment 1 is that the ultrafine ferric citrate and the zinc gluconate are added into the aerobic pool, and the concentrations of the ultrafine ferric citrate and the ultrafine zinc gluconate are respectively 2mg/L and 1 mg/L.
Example 3:
treatment engineering of pig breeding wastewater
1 general overview of the engineering
The engineering is located in a certain scale pig farm which adopts a dry manure cleaning mode, and the main source of the wastewaterThe pig house is flushed with water, pig urine and a small amount of domestic sewage. Finally determining the engineering design throughput to be 150m according to the data provided by the owner and the on-site monitoring3Per hour, 24 hours per day, about 6.25m3H, the variation coefficient in design is 1.25, and the maximum design load of pretreatment is 7.8m3/h。
1.1 quality of wastewater
The wastewater of the base is sampled and measured for one week continuously, and the water quality detection result and the designed discharge standard are shown in table 1.
TABLE 1 Water quality and discharge Standard
Item CODcr/(mg/L) NH3-N/(mg/L) TP/(mg/L) pH
Pig farm wastewater 5000-13000 600-1800 70-120 7.2-7.6
Emission standard ≤150 ≤45 ≤7 6.0-9.0
1.2 Process flow
Aiming at the characteristics and the discharge requirements of the wastewater of the pig farm, the improved A/O treatment process of the embodiment 1 is adopted to carry out centralized treatment on the wastewater treatment method of the pig farm, and the process flow is shown in figure 1.
After large-particle floating objects in the wastewater of the pig farm are removed by the grating, the wastewater enters the septic tank, the wastewater is lifted to the vibrating screen by the water pump for solid-liquid separation, and the liquid enters the catch basin. Then lifted to a first-stage strengthening tank by a water pump, and biochemical treatment is carried out step by step. The mixed liquid in the aerobic tank and the residual sludge in the secondary sedimentation tank return to the primary strengthening tank and the anoxic tank; the supernatant fluid flows into a secondary strengthening tank and is further biochemically treated by immobilized microorganisms in the tank; follow-up through high-efficient compound water purification agent (this high-efficient compound water purification agent provides in the patent application number is 201710305839X, its composition and preparation process are like this patent, this application is no longer repeated) and PAM combined action, get rid of suspended solid, colourity and total phosphorus in the waste water, reach qualified effluent.
And (3) pumping the residual sludge in the secondary sedimentation tank and the dosing flocculation sedimentation sludge to a sludge concentration tank through a water pump for storage, carrying out mechanical dehydration, transporting a mud cake outwards or carrying out fermentation treatment, and refluxing dehydration filtrate to the system.
2 Main Structure and Unit
2.1 first-level strengthening pool
1 seat, semi-underground reinforced concrete structure, effective volume 250m3Biological fillers are arranged in the aeration device, and the lifting type aeration device 1 set is matched.
2.2A/O reaction tank
Semi-underground reinforced concrete structure, A pool effective volume 450m3Effective volume of O tank is 900m3The biological filler is arranged in the device, 2 stirring machines are matched, 2 aerators are used (one is used for the other), 1 lifting type aerator is arranged, and 2 nitrification reflux pumps are arranged.
2.3 Secondary sedimentation tank
Semi-underground reinforced concrete structure, 1 seat, surface load of 0.4m3/(m2H), 2 matched sludge pumps.
2.4 Secondary strengthening pool
1 seat, semi-underground reinforced concrete structure, effective volume 75m3Biological filler is arranged in the aeration device, and the aeration device can be lifted by 1 set.
2.5 Add medicine flocculation and sink
1 seat, a semi-underground reinforced concrete structure, 2 sets of matched dosing systems and 2 sludge pumps.
3 engineering debugging and operation results
3.1 engineering debugging
The engineering is debugged at the room temperature of 10-15 ℃, the time is about 30 days, the inoculated sludge comes from peripheral municipal sewage treatment plants, the sludge is black, the settleability is good, the activity is higher, 10t of sludge is inoculated in a primary strengthening tank, 30t of sludge is inoculated in an aerobic tank, then clear water and piggery wastewater are added, the water level is controlled to be 2.5m according to a certain proportion, and the aeration is started.
After aeration for 2d, wastewater is added according to 10% of the total amount of the mixed liquor every day until the primary strengthening tank, the anoxic tank and the aerobic tank are communicated (the mixed liquor of the anoxic tank comes from the aerobic tank), water flows into the secondary sedimentation tank, nitrification liquid reflux and sludge reflux are started, the nitrification liquid reflux ratio is 1:6, the sludge reflux ratio is 1:1.5, meanwhile, the water inlet mode is changed into a continuous water inlet mode, the water is respectively added into the primary strengthening tank and the anoxic tank, and the water inlet flow is gradually increased to meet the design requirements.
After debugging, the activated sludge in the system is dark brown, the mud-water interface is clear, the supernatant is clear, the sludge settlement ratio is about 45 percent, and the water quality of each treatment unit is stable.
3.2 results of engineering runs
After the engineering is debugged for 30 days, the system enters a full-load stable running state, the mean value of the water quality indexes of the water outlets of all units is shown in table 2, the COD (chemical oxygen demand) of effluent treated by the process is 81mg/L, ammonia nitrogen is 0.3mg/L, TP (total phosphorus removal) is 1.0mg/L, and the removal rates are 99.1%, 99.9% and 99.1% respectively.
TABLE 2 Water quality index at water outlet of each unit
Processing unit COD(mg/L) Ammonia nitrogen (mg/L) TP(mg/L)
Inflow water 9120 1150 114.7
First-level strengthening pool 614 85.5 78.3
A/O pool 225 0.8 41.7
Secondary strengthening pool 172 0.6 40.3
Dosing flocculation tank 85 0.5 1.1
Discharging water 81 0.3 1.0
4 determination of Water-in and Water-out resistance Gene
After the system runs stably, water inflow and water outflow are collected, and resistance genes in the water body are detected, and the results are shown in fig. 2 and fig. 3, the tetracycline and part of heavy metal resistance genes in the water body of the outflow water are obviously reduced, which shows that the treatment engineering of the pig breeding wastewater has good degradation effect on the tetracycline and part of heavy metal resistance genes in the water body.
Engineering economic analysis
In the project, the total installed capacity is 95.57kW, the operating power is 46.07kW, and the electric charge is calculated according to 0.68 yuan/kW.h, so that the electric charge for treating each ton of wastewater is 5.01 yuan. The process has the advantages of higher automation degree, simple and convenient operation and low labor intensity, 1 piggery can play a role simultaneously, 1000 yuan is subsidized every month, and the labor cost for treating each ton of wastewater is 0.22 yuan. The process needs to add the high-efficiency composite water purifying agent and PAM to carry out flocculation treatment on the wastewater, the adding amount and the cost are shown in the table 3, and the cost of the agent is 1.11 yuan/ton. The direct cost of operation of the wastewater treatment system is shown in Table 4.
TABLE 3 wastewater chemical dosage calculation chart
Name of medicine Amount of addition Monovalent per unit per kg Ton addition cost/yuan
High-efficiency composite water purifying agent 0.9kg/t 1.20 1.08
PAM 1.2g/t 25 0.03
Total up to 1.11
TABLE 4 direct cost summary of runs
Serial number Item Cost (Yuan/ton)
1 Electric charge 5.01
2 Cost of medicament 1.11
3 Personnel fee 0.22
4 Total up to 6.34
As can be seen from Table 4, the running cost is 6.34 yuan per ton of wastewater.
Conclusion 6
The improved A/O process is adopted to treat the pig farm breeding wastewater, and the operation result shows that after the treatment of the combined process, the removal rates of COD, ammonia nitrogen and TP are respectively 99.1%, 99.9% and 99.1%, and the effluent index is far superior to the design requirement standard. The treatment process is stable and reliable, realizes the high-efficiency treatment of carbon, nitrogen and phosphorus, and has higher popularization and application values.
Example 4:
treatment engineering of pig breeding wastewater
The difference from the embodiment 3 lies in that the engineering is debugged under the condition that the room temperature is 0-8 ℃, the mean value of the water quality indexes of the water outlets of all units is shown in table 5, and it can be seen that the water outlets of the A/O tank are 427mg/L of COD, 10.9mg/L of ammonia nitrogen and 66.8mg/L of TP, the removal rates are 60.7%, 88.6% and 26.1% respectively, and the water outlet indexes are far different from those of the water outlets of the A/O tank in the embodiment 3, because the lower water temperature can inhibit the growth of nitrifying bacteria, denitrifying bacteria and phosphorus removing bacteria in the system, thereby affecting the removal effect of COD, ammonia nitrogen and TP in the improved A/O process. After the treatment by the process, the COD (chemical oxygen demand) of the effluent is 246mg/L, the ammonia nitrogen is 3.2mg/L, the TP is 2.3mg/L, the removal rates are respectively 98.5%, 99.7% and 97.9%, and the effluent indexes are superior to the requirements of discharge standards of pollutants for livestock and poultry breeding (GB18596-2001), so that the effluent indexes of the irrigation of farmlands can be achieved, and the requirements of the irrigation of the farmlands are met.
Table 5 Water quality index of each unit water outlet
Processing unit COD(mg/L) Ammonia nitrogen (mg/L) TP(mg/L)
Inflow water 8700 1200 112.6
First-level strengthening pool 830 95.8 89.8
A/O pool 326 10.9 66.8
Secondary strengthening pool 245 6.2 65.7
Dosing flocculation tank 134 3.5 2.3
Discharging water 131 3.4 2.3
Example 5:
treatment engineering of pig breeding wastewater
The difference from the embodiment 4 is that after the engineering enters a full load stable operation state, the ultrafine ferric citrate and the ultrafine zinc gluconate are added into the aerobic pool, and the concentrations of the ultrafine ferric citrate and the ultrafine zinc gluconate are respectively 2mg/L and 1 mg/L. The mean values of the water quality indexes of the water outlets of the units are shown in Table 6, and it can be seen that the water outlet indexes of the A/O pool water outlet COD 181mg/L, ammonia nitrogen 0.6mg/L and TP 32.4mg/L are 65.4%, 99.1% and 69.5% respectively, and the water outlet indexes are far better than those of the water outlet of the A/O pool in example 4, because the lower water temperature can inhibit the growth of nitrifying, denitrifying and dephosphorizing bacteria in the system, thereby affecting the removal effect of COD, ammonia nitrogen and TP in the improved A/O process, and the addition of the particulate ferric citrate and the zinc gluconate strengthens the electron transfer system and the enzymatic reaction activity in the microorganism, improves the nitrifying capacity of the nitrifying bacteria, thereby enhancing the low-temperature nitrification resistance of the activated sludge, and simultaneously enabling the dephosphorizing bacteria to have higher biological activity, thereby having stronger aerobic phosphorus uptake capacity, and further achieving better COD, Ammonia nitrogen and TP removal effect. After the treatment by the process, the COD (chemical oxygen demand) of the effluent is 51mg/L, the ammonia nitrogen is 0.2mg/L, the TP is 0.5mg/L, the removal rates are respectively 99.4%, 99.98% and 99.6%, and the effluent indexes are superior to the requirements of discharge standards of pollutants for livestock and poultry breeding (GB18596 plus 2001), so that the effluent indexes of the irrigation of farmlands can be achieved, the requirements of the irrigation of farmlands are met, and the effluent discharge standards above class A of Integrated wastewater discharge standards can also be achieved.
Table 6 water quality index of each unit water outlet
Processing unit COD(mg/L) Ammonia nitrogen (mg/L) TP(mg/L)
Inflow water 8700 1200 112.6
First-level strengthening pool 523 65.7 89.8
A/O pool 181 0.6 27.4
Secondary strengthening pool 137 0.2 26.1
Dosing flocculation tank 53 0.3 0.5
Discharging water 51 0.2 0.5
Test example 1:
the treatment engineering of the pig breeding wastewater of the embodiment 2, the embodiment 3, the comparative example 1 and the comparative example 2 is operated in a low temperature range of 0-8 ℃, the system enters a full-load stable operation state, the activity of the activated sludge mixed liquid dehydrogenase and the activity of the electron transfer system in the aerobic tank are detected, and the sedimentation performance of the activated sludge is analyzed.
1. Method for measuring dehydrogenase activity
Preparing TTC solutions with different concentrations: 1mL, 2mL, 3mL, 4mL, 5mL, and 6mL of the TTC standard solution was aspirated into a set of 50mL volumetric flasks, and the volume was adjusted to 50mL with ultrapure water, and 2mL of Tris-HCl buffer was added to the volumetric flasks at the same time, wherein the TTC concentration in the flasks was 20. mu.g/mL, 40. mu.g/mL, 60. mu.g/mL, 80. mu.g/mL, 100. mu.g/mL, and 120. mu.g/mL in this order. During the determination, 1mL of TTC working solution with different concentrations is taken, and 10% Na is added2Shaking the S solution evenly, and standing for 20min (the control tube is not added with TTC) to ensure that the TTC is completely reduced to generate red TF; after the reaction is completed, 5mL of toluene is added into each tube, the tubes are shaken and kept stand for 10-20min after being mixed completely, supernatant liquid is absorbed, the absorbance is measured at 492nm (stabilized in a cuvette for 2min) by a spectrophotometer, and a standard curve is drawn. Solving a linear curve regression equation of the TTC-deaminase content standard as follows: y is 0.0049x +0.0371, R2＝0.9990。
Taking 15mL of sludge mixed solution into a conical flask, adding glass beads to shake the sludge to break the sludge, centrifuging the sludge for 10min at 4000r/min, removing supernatant, supplementing the sludge with distilled water, stirring and washing the mixture for 3 times respectively, supplementing the mixture to the original volume with distilled water, taking 2mL of the mixture into a test tube with a plug, adding 1.5mL of Tris-HCl buffer solution, 0.5mL of glucose solution, 0.5mL of 0.4% TTC solution and 0.5mL of 0.36% Na solution2SO3The solution was then incubated for 2h in a 37 ℃ thermostated waterbath shaker, removed and quenched by the addition of 0.5mL of formaldehydeAnd (3) reacting, adding 5mL of acetone, performing oscillation extraction at 37 ℃ for 10min, centrifuging at 4000r/min for 10min, taking the upper organic solvent, measuring the absorbance on a spectrophotometer under the condition of 492nm of wavelength, measuring the absorbance of the extract and calculating. Under the above conditions, the amount of production of μ g of triphenylformazan in 1 hour was considered as one unit of enzyme activity.
2. Method for measuring activity of electron transfer system
Taking 15mL of sludge mixed liquor in a conical flask, adding glass beads to shake to break the sludge, centrifuging for 10min at 4000r/min, discarding the supernatant, then adding distilled water to complement, stirring and washing for 3 times respectively, then adding distilled water to complement the original volume, then taking 1mL out of the conical flask, adding 0.5mL of 0.2% INT solution and 2mL of 0.1mol/L glucose solution, then culturing for 4h in a constant-temperature water bath shaking instrument at 37 ℃, taking out and adding 1mL of 37% formaldehyde to stop the reaction, centrifuging for 10min at 4000r/min, discarding the supernatant, then adding 5mL of methanol, shaking and extracting for 10min at 37 ℃ in the dark, then centrifuging for 10min at 4000r/min, taking the upper organic solvent, and measuring the absorbance on a spectrophotometer at the wavelength of 485 nm. The centrifuged excess sludge was dried at 100 ℃ for 1h and the weight of the dried sludge was measured. The electron transport system activity is calculated by the following formula: electron transport system activity [ μ g/(mg · h) ], value (absorbance × extractant volume)/(slope of standard curve × dry sludge weight × incubation time).
3. Determination of extracellular polymers
Centrifuging 50mL of sludge sample at a rotation speed of 5000r/min for l0min, pouring out supernatant, adding buffer solution into the residual sludge after centrifugation to make up 50mL, pouring into a beaker, and adding 8% H into the beaker2SO450mL, extracting for 1h in a stirrer at 300r/min, centrifuging again at the rotating speed of 5000r/min for 20min, and finally filtering with a 0.45-micron microporous filter membrane to obtain the extracellular polymer extract solution. The protein in the extracellular polymeric substance is measured by a modified Folin-Lowry method, and the standard substances are bovine serum albumin and fulvic acid respectively. The polysaccharide assay adopts anthrapyridone-sulfuric acid method, and the standard substance is glucose. Protein and polypeptide are measured by an ultraviolet-visible spectrophotometerThe sugar absorbs at 260nm and 280nm, 620nm, respectively. The concentration of the protein was calculated by the following formula: protein concentration of 1.45 × A280nm-0.74×A260mnThe method can eliminate the interference of nucleic acid in the sample to the measured value.
4. Sludge sedimentation ratio and sludge volume index of activated sludge
The sludge-water mixed liquor is put into a l00mL container, and after 30min, the volume of the precipitated sludge accounts for the volume percentage of the original mixed liquor, namely the sludge settlement ratio, which is generally used for representing the sludge settlement performance, and the lower the sludge settlement ratio, the better the settlement performance of the activated sludge.
FIG. 4 shows the changes of the activity of the activated sludge mixed liquor dehydrogenase and the activity of the electron transport system in the aerobic tank, and it can be seen that, in the low temperature range of 0-10 ℃, the activity of the activated sludge mixed liquor dehydrogenase and the activity of the electron transport system in the aerobic tank in example 3 are respectively 26.71 μ g/(mg.h) and 52.37 μ g/(mg.h), and the activity of the activated sludge mixed liquor dehydrogenase and the activity of the electron transport system in the aerobic tank in example 4 are respectively 76.33 μ g/(mg.h) and 80.02 μ g/(mg.h), compared with example 3, the activity of the activated sludge mixed liquor dehydrogenase and the activity of the electron transport system in the aerobic tank in example 4 are respectively 185.77% and 52.80%; the activity of the activated sludge mixed liquor dehydrogenase in the aerobic tank and the activity of an electron transfer system in the comparative example 1 are superior to those of the example 3 and inferior to those of the example 4, and the activity of the activated sludge mixed liquor dehydrogenase in the aerobic tank and the activity of the electron transfer system in the comparative example 2 are equivalent to those of the example 3 and inferior to those of the example 4; the results show that the adding of the ultrafine ferric citrate particles and the zinc gluconate particles into the aerobic tank strengthens an electron transfer system and enzymatic reaction activity in a microorganism body, improves the nitrification capability of nitrifying bacteria, and can enhance the low-temperature nitrification resistance of activated sludge.
FIG. 5 is a change of exopolymers in the aerobic tank, and it can be seen that, compared with example 3, in the low temperature range of 0-10 ℃, the contents of exopolymers, proteins in the exopolymers and polysaccharides in the exopolymers in the aerobic tank are increased in example 4 and comparative example 1, and the increase of example 4 is larger, while the content of exopolymers, proteins in the exopolymers and polysaccharides in the exopolymers in the aerobic tank is not changed significantly in comparative example 2; meanwhile, the ratio of the protein in the exopolymer to the polysaccharide in the exopolymer in the aerobic tank of example 3 is about 4.87, the ratio of the protein in the exopolymer to the polysaccharide in the exopolymer in the aerobic tank of example 4 is about 2.75, the ratio of the protein in the exopolymer to the polysaccharide in the exopolymer in the aerobic tank of comparative example 1 is about 4.56, and the ratio of the protein in the exopolymer to the polysaccharide in the exopolymer in the aerobic tank of comparative example 2 is about 4.77; the results show that the cooperation of the ferric citrate and the zinc gluconate can promote the microorganisms in the activated sludge to generate more extracellular polymeric substances, reduce the protein component in the extracellular polymeric substances and improve the polysaccharide component in the extracellular polymeric substances, thereby improving the sedimentation performance of the activated sludge.
FIG. 6 is a graph showing the sludge sedimentation ratio of activated sludge in an aerobic tank, and it can be seen that compared with example 3, the sludge sedimentation ratio of activated sludge in the aerobic tank is low in example 4 and comparative example 1, and is lower in example 4, and the sludge sedimentation ratio of activated sludge in the aerobic tank of comparative example 2 is not significantly changed; this shows that the mutual cooperation of ferric citrate and zinc gluconate can reduce the sludge sedimentation ratio of the activated sludge in the aerobic tank, thereby improving the sedimentation performance of the activated sludge, which is consistent with the above results, and further beneficial to the adsorption and degradation of pollutants.
Conventional techniques in the above embodiments are known to those skilled in the art, and therefore, will not be described in detail herein.
The above embodiments are merely illustrative, and not restrictive, and those skilled in the art can make various changes and modifications without departing from the spirit and scope of the invention. Therefore, all equivalent technical solutions also belong to the scope of the present invention, and the protection scope of the present invention should be defined by the claims.

Claims (6)

1. A treatment method of livestock and poultry breeding wastewater comprises the following steps:
in the pretreatment stage, the livestock and poultry breeding wastewater is subjected to effective solid-liquid separation by a grid and a hydraulic vibrating screen or an air floatation device to remove most of the manure in the wastewater so as to reduce the generation amount of sediment and scum in the subsequent treatment link and reduce the concentration of pollutants in the wastewater, solid matters are conveyed to a composting workshop, and squeezed raw water enters a subsequent treatment system;
an improved A/O treatment stage, wherein the pretreated wastewater is treated by an improved A/O system to achieve qualified effluent;
the improved A/O treatment system comprises a primary strengthening tank, an A/O treatment tank, a secondary sedimentation tank, a secondary strengthening tank and a dosing flocculation tank which are sequentially connected in the water flow direction, so that the wastewater sequentially enters the primary strengthening tank, the A/O treatment tank, the secondary sedimentation tank, the secondary strengthening tank and the dosing flocculation tank, and finally qualified effluent is obtained;
wherein the first-stage strengthening tank, the A/O treatment tank and the second-stage strengthening tank are respectively inoculated with activated sludge and/or functional microorganisms;
the A/O treatment tank comprises an anoxic tank and an aerobic tank, two-stage backflow, nitrification liquid backflow and sludge backflow are set in the improved A/O treatment stage, the nitrification liquid backflow is that mixed liquid at the tail end of the aerobic tank flows back to the anoxic tank, and the sludge backflow is that partial residual sludge in the secondary sedimentation tank flows back to the primary strengthening tank and/or the anoxic tank; the aerobic tank is divided into 3-6 sections; the reflux ratio of the nitrifying liquid is 1:2-10, and the reflux ratio of the sludge is 1: 0.5-2; after the treatment system enters a full-load stable operation state, the sludge settlement ratio is 30-80%; adding ultrafine ferric citrate particles and zinc gluconate into the aerobic pool;
the treatment method has the COD removal rate of more than 99.0 percent, the ammonia nitrogen removal rate of more than 99.50 percent, the TP removal rate of more than 99.0 percent, the tetracycline antibiotic removal rate of more than 86 percent and the heavy metal removal rate of more than 90 percent.
2. The method for treating livestock and poultry breeding wastewater according to claim 1, which is characterized in that: the HRT of the first-stage strengthening pool is 1-2d, the HRT of the A/O stage is 6-10d, and the HRT of the second-stage strengthening pool is 0.5-1 d.
3. The method for treating livestock and poultry breeding wastewater according to claim 1, which is characterized in that: the concentrations of the ultra-micro ferric citrate and the zinc gluconate are respectively 1-5mg/L and 0.1-2 mg/L.
4. The method for treating livestock and poultry breeding wastewater according to claim 1, which is characterized in that: the treatment method comprises treatment in winter.
5. The method for treating livestock and poultry breeding wastewater according to claim 1, which is characterized in that: the treatment method degrades tetracycline resistance genes and heavy metal resistance genes in water.
6. Use of the treatment method according to claim 1 for the treatment of high ammonia nitrogen wastewater in winter.
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