CN212246699U - Neomycin sulfate waste water treatment device - Google Patents
Neomycin sulfate waste water treatment device Download PDFInfo
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- CN212246699U CN212246699U CN202020993877.6U CN202020993877U CN212246699U CN 212246699 U CN212246699 U CN 212246699U CN 202020993877 U CN202020993877 U CN 202020993877U CN 212246699 U CN212246699 U CN 212246699U
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- PGBHMTALBVVCIT-VCIWKGPPSA-N framycetin Chemical compound N[C@@H]1[C@@H](O)[C@H](O)[C@H](CN)O[C@@H]1O[C@H]1[C@@H](O)[C@H](O[C@H]2[C@@H]([C@@H](N)C[C@@H](N)[C@@H]2O)O[C@@H]2[C@@H]([C@@H](O)[C@H](O)[C@@H](CN)O2)N)O[C@@H]1CO PGBHMTALBVVCIT-VCIWKGPPSA-N 0.000 title claims abstract description 20
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Abstract
A neomycin sulfate production wastewater treatment device comprises a preconditioning tank, an air flotation machine, a hydraulic plate-frame filter press, a comprehensive adjusting tank, an electrochemical reactor, an acid-producing phase reactor, a desulfurization tank, a methane-producing phase reactor, an ozone pre-oxidation tank, an ozone generator, an anaerobic tank, an anoxic tank, a contact oxidation tank, a secondary sedimentation tank, a flocculation sedimentation tank, a sludge tank and an anaerobic tank, wherein the preconditioning tank is communicated with the air flotation machine, the air flotation machine is communicated with the hydraulic plate-frame filter press, the hydraulic plate-frame filter press is communicated with the comprehensive adjusting tank, the air flotation machine is communicated with the electrochemical reactor, the electrochemical reactor is communicated with the acid-producing phase reactor, the acid-producing phase reactor is communicated with the desulfurization tank, the desulfurization tank is communicated with the methane-producing phase reactor, the methane-producing phase reactor is communicated with the comprehensive adjusting tank, the comprehensive adjusting tank is communicated with the ozone pre-oxidation tank, the ozone, the investment floor area and the operation cost are saved, and the method has good social and economic benefits.
Description
Technical Field
The utility model relates to a waste water treatment, in particular to a neomycin sulfate production waste water treatment device.
Background
The production of neomycin sulfate belongs to the fermentation pharmaceutical technology, and the wastewater is characterized by having two kinds of wastewater with high and low concentrations, wherein the high concentration wastewater is mainly extracted wastewater generated in the neomycin sulfate production process, COD (chemical oxygen demand) is up to 15000-20000mg/L, BOD (biological oxygen demand) is low, the content is 8000-10000mg/L, biodegradability is general, the ammonia nitrogen content is 1300-2000mg/L, TP (total phosphorus content) is 150-200mg/L, sulfate radical is 10000-15000mg/L, the content is higher, the water quality and water quantity with high concentration are greatly changed, and most of the wastewater contains difficultly biodegraded substances and microbial growth inhibitors. Because the raw water COD is higher, the anaerobic process is preferably adopted to reduce the raw water COD concentration, but the high sulfate radical concentration in the wastewater can generate SRB (sulfate reducing bacteria) to generate a substrate competition effect with anaerobic methanogens, so that the growth of the anaerobic reactor methanogens is inhibited, and even the paralysis of the anaerobic reactor is caused in severe cases. The conventional two-phase anaerobic process can only remove high sulfate radical and high COD wastewater, the extraction wastewater in the neomycin sulfate production process also has the characteristics of high SS, high P (phosphorus) and high ammonia nitrogen, the concentration of the extraction wastewater is far beyond the water inlet load of a conventional AAO biochemical system, if the high P high ammonia nitrogen wastewater directly enters the AAO biochemical system, the aeration amount of the conventional AAO process is obviously increased, serious foam, large sludge loss amount and other serious adverse effects are caused, therefore, the pretreatment of the wastewater must be enhanced, the biodegradability of the wastewater is improved, the high sulfate radical, most of ammonia nitrogen and TP in the water are removed, and the high P high ammonia nitrogen wastewater and TP are mixed with the low-concentration wastewater to enter a biochemical treatment facility.
SUMMERY OF THE UTILITY MODEL
To the above-mentioned condition, for overcoming prior art's defect, the utility model aims at providing a neomycin sulfate waste water treatment equipment, can effectively solve and improve neomycin sulfate waste water biodegradability, remove the high sulfate radical in the water, most ammonia nitrogen and TP to reduce the follow-up good oxygen biochemical technology stage and handle the degree of difficulty.
In order to realize the purpose, the utility model provides a technical scheme is, a neomycin sulfate production wastewater treatment device, including preconditioning tank, air supporting machine, comprehensive equalizing basin and anaerobism pond, the export of preconditioning tank be linked together through the import of pipeline with the air supporting machine, the fungus sediment export of air supporting machine is linked together through the import of pipeline with hydraulic pressure plate frame pressure filter, the liquid export of hydraulic pressure plate frame pressure filter is linked together through the import of pipeline with comprehensive equalizing basin, the waste water export of air supporting machine is linked together through the import of pipeline with electrochemical reactor, the export of electrochemical reactor is linked together through the import of pipeline with the acid-producing phase reactor, the export of the acid-producing phase reactor is linked together through the import of pipeline with the desulfurizing tank, the export of desulfurizing tank is linked together through the import of pipeline with the methane-producing phase reactor, the export of the methane-producing phase reactor is linked together through the import of pipeline with comprehensive equalizing basin, the outlet of the comprehensive adjusting tank is communicated with the inlet of the ozone pre-oxidation tank through a pipeline, the gas inlet of the ozone pre-oxidation tank is communicated with the gas outlet of an ozone generator, the outlet of the ozone pre-oxidation tank is communicated with the inlet of the anaerobic tank through a pipeline, the outlet of the anaerobic tank is communicated with the inlet of the anoxic tank through a pipeline, the outlet of the anoxic tank is communicated with the inlet of the contact oxidation tank through a pipeline, the backflow port of the contact oxidation tank is communicated with the inlet of the anoxic tank through a pipeline, the outlet of the contact oxidation tank is communicated with the inlet of the secondary sedimentation tank through a pipeline, the outlet of the secondary sedimentation tank is communicated with the inlet of the flocculation sedimentation tank through a pipeline, the sedimentation outlet of the secondary sedimentation tank is respectively communicated with the inlet of the sludge tank and the inlet pipeline of the anaerobic tank through a three-way pipe, and the outlet.
The utility model provides the high biodegradability of neomycin sulfate waste water gets rid of aquatic high sulfate radical, most ammonia nitrogen and TP, on full play anaerobic treatment advantage basis, save area, the working costs of investment and reduce the follow-up good oxygen biochemical technology stage and handle the degree of difficulty, have good society and economic benefits.
Drawings
Fig. 1 is a structural block diagram of the present invention.
Detailed Description
The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings.
The device comprises a preconditioning tank, an air flotation machine, a comprehensive adjusting tank and an anaerobic tank, wherein the outlet of the preconditioning tank 1 is communicated with the inlet of the air flotation machine 3 through a pipeline, the bacteria residue outlet of the air flotation machine 3 is communicated with the inlet of a hydraulic plate frame filter press 8 through a pipeline, the liquid outlet of the hydraulic plate frame filter press 8 is communicated with the inlet of the comprehensive adjusting tank 9 through a pipeline, the waste water outlet of the air flotation machine 3 is communicated with the inlet of an electrochemical reactor 4 through a pipeline, the outlet of the electrochemical reactor 4 is communicated with the inlet of an acid-producing phase reactor 5 through a pipeline, the outlet of the acid-producing phase reactor 5 is communicated with the inlet of a desulfurizing tank 6 through a pipeline, the outlet of the desulfurizing tank 6 is communicated with the inlet of a methane-producing phase reactor 7 through a pipeline, the outlet of the methane-producing phase reactor 7 is communicated with the inlet of the comprehensive adjusting tank 9 through a pipeline, the outlet of the comprehensive adjusting tank 9 is communicated with the inlet of an ozone pre-oxidation tank 10 through a pipeline, the gas inlet of the ozone pre-oxidation tank 10 is communicated with the gas outlet of an ozone generator 11, the outlet of the ozone pre-oxidation tank 10 is communicated with the inlet of an anaerobic tank 13 through a pipeline, the outlet of the anaerobic tank 13 is communicated with the inlet of an anoxic tank 14 through a pipeline, the outlet of the anoxic tank 14 is communicated with the inlet of a contact oxidation tank 15 through a pipeline, the return port of the contact oxidation tank 15 is communicated with the inlet of the anoxic tank 14 through a pipeline, the outlet of the contact oxidation tank 15 is communicated with the inlet of a secondary sedimentation tank 16 through a pipeline, the outlet of the secondary sedimentation tank 16 is communicated with the inlet of a flocculation sedimentation tank 17 through a pipeline, the sedimentation outlet of the secondary sedimentation tank 16 is respectively communicated with the inlet of a sludge tank 18 and the inlet pipeline of the anaerobic tank 13 through a three-way pipe 16-1, and the outlet of the.
In order to ensure better implementation effect, a first sewage lifting pump 2 is arranged on a pipeline between the pre-adjusting tank 1 and the air flotation machine 3, a second sewage lifting pump 6-1 is arranged on a pipeline between the desulfurization tank 6 and the methanogenic phase reactor 7, and a third sewage lifting pump 12 is arranged on a pipeline between the ozone pre-oxidation tank 10 and the anaerobic tank 13.
And the air inlets of the desulfurization tank 6, the comprehensive adjusting tank 9 and the contact oxidation tank 15 are respectively communicated with the air outlet of the air blower 21 through pipelines.
The pre-conditioning tank 1 is internally provided with a stirrer, and the power of the stirrer is 5-8W/m3 (a commercial product, a known technology).
The chemical feeding port of the air flotation machine 3 is communicated with the chemical outlet of the automatic chemical feeding device 3-1, and a sludge conditioning chemical feeding device 20 is arranged on a pipeline between the sludge tank 18 and the sludge dewatering machine 19.
The sludge dewatering machine 19 is a hydraulic plate frame dewatering machine or a stacked spiral sludge dewatering machine.
The volume ratio of the anaerobic tank 13 to the anoxic tank 14 to the contact oxidation tank 15 is 1: 3 or 1: 4.
the utility model discloses when concrete implementation, the particular case is as follows:
(1) adjusting the water quality and the water quantity: pharmaceutical production is mostly intermittent production, the fluctuation of water quantity and water quality is large, the purification function of the wastewater treatment equipment is not good, in order to improve the impact capacity of a sewage treatment facility on organic matter load and reduce the fluctuation of water quality, a preconditioning tank is arranged to regulate the water quantity and the water quality of raw water, high sulfate radical and high ammonia nitrogen extraction wastewater is treated by a grid well to remove larger suspended matters, floating matters, fiber substances and solid particle substances, thereby ensuring the normal operation of a subsequent treatment structure and reducing the treatment load of the subsequent treatment structure, the wastewater enters the preconditioning tank 1, a stirrer is arranged in the preconditioning tank 1, and the power is 5-8W/m3Adding H into the pre-adjusting tank 12SO4(sulfuric acid) and NaOH (sodium hydroxide), reacting the wastewater in a pre-adjusting tank 1 for 24-48h,the pH value is controlled to be 6-9 by an industrial pH meter, suitable reaction conditions are provided for the subsequent process, and a grid well is arranged at the inlet of the pre-adjusting tank 1 and is built with the pre-adjusting tank 1;
(2) and solid-liquid separation of wastewater: the wastewater in the preconditioning tank 1 is pumped into an air flotation machine 3 through a first sewage lifting pump 2 to carry out solid-liquid separation for 20-30min, scum separated by the air flotation machine is mainly used for extracting bacteria residues in the wastewater, SS (suspended solids) in the wastewater reaches ten thousand mg/L, 30-50mg/L of polyaluminium chloride with the mass fraction of 10-15 percent is added into the air flotation machine 3 through an automatic medicine adding device 3-1, and 1-2mg/L of polyacrylamide with the mass fraction of 1 per mill, so as to realize better solid-liquid separation effect, remove suspended substances and a small amount of COD in water, ensure that the SS removal rate can reach 80-90 percent, separate fungus residues into dangerous wastes, enter a hydraulic plate-and-frame filter press 8 for dewatering and squeezing, the wastewater is treated by a third party with the treatment qualification of hazardous waste, and the wastewater dehydrated by the hydraulic plate-frame filter press 8 enters a comprehensive regulating tank 9; (3) and electrochemical reaction: the wastewater treated by the air flotation machine 3 enters the electrochemical reactor 4 to react for 0.8h to 1.5h, and COD, ammonia nitrogen and TP in the wastewater are removed;
under the pulse flow impact and electrochemical action, organic matters in the wastewater continuously generate electrochemical oxidative degradation and reductive modification on the surface of an electrode and also generate electro-Fenton (Fenton) reaction, under the synergistic action of hydroxyl radicals, a pulse power supply matched with a soluble high-silicon ferrite bipolar electrode is adopted, and physicochemical separation reactions such as electro-flotation, electrocoagulation and the like are simultaneously carried out to react under the conditions of normal temperature and normal pressure; the system can control the process system by enduring the impact of water quality and water temperature fluctuation; no additional medicament is needed, no secondary pollution is caused, the CODcr (dichromate index) of the wastewater is reduced by 50-70%, the ratio of BOD5/CODcr is greatly improved, and the biodegradability of the wastewater is effectively improved;
during electrolysis, the anode mainly generates a dissolution reaction of iron, and the cathode mainly generates H2With a decrease in H +, NH3-NH4 +Equilibrium is disrupted, free ammonia (NH)3) Are increasing. The gas generated by the cathode takes out free ammonia from the wastewater, so that the concentration of total ammonia nitrogen in the wastewater is reduced, and OH at the moment-Increasing the pH value. When the pH value is increasedAfter adding a certain value, the OH in the wastewater-And dissolved Fe2+A flocculent precipitate forms, on the other hand OH-Electrons are lost and oxygen is released, the pH value increasing speed is slowed down by the electrons and the oxygen, when the reaction reaches the balance, the ammonia removal rate reaches the maximum, and a large amount of ammonia nitrogen is removed;
(4) removing sulfate: the wastewater treated by the electrochemical reactor 4 enters the acid-producing phase reactor 5 to react for 6 to 24 hours, the pH value in the electrochemical reactor (4) is 6.1 to 6.5, and the generated sulfide is mainly H2S, SRB (sulfate reducing bacteria) has a wide range of available substrates, most of sulfate in the wastewater is removed through the sulfate reducing bacteria, more methane precursors are generated, the methanogen is prevented from being poisoned after desulfurization, and a higher methane production rate is ensured; COD volume loading of acidogenic phase reactor 5: 2-5kgCOD/m3。
(5) And desulfurizing: the wastewater treated by the acidogenic phase reactor 5 enters a desulfurization tank 6, aeration is provided by an air blower 21, and H in the wastewater is oxidized by micro-aerobic aeration2S is oxidized into elemental sulfur, and flocculating settling is carried out for 1.5 to 2 hours by adding flocculating agent, the surface load of the settling is less than 0.1m/S, and the sulfur is removed from the wastewater;
(6) COD and BOD removal: the wastewater treated by the desulfurization tank 6 enters a methanogenic phase reactor 7 through a second sewage lift pump 6-1 to react for 1.5-8d, the pH value in the methanogenic phase reactor 7 is 6.8-7.2, and because high sulfate radicals and high ammonia nitrogen are removed in the pre-pretreatment step, organic matters in the wastewater are degraded into methane and carbon dioxide by methanogenic bacteria in the desulfurization tank 6, and COD and BOD in the wastewater are removed; the COD load of the desulfurization tank 6 is 4-15kgCOD/m3；
(7) Comprehensively adjusting water quality and water quantity: the waste water treated by the methanogenic phase reactor 7 and the neomycin sulfate regeneration waste water are treated by a grating well to remove larger suspended matters, floating matters, fiber substances and solid particle substances, then the waste water enters a comprehensive adjusting tank 9, acidic substances and alkaline substances are added into the comprehensive adjusting tank 9, the waste water in the comprehensive adjusting tank 9 is subjected to gas stirring by an air blower 21, organic matters are prevented from settling to the bottom of the tank and being acidified and corrupted, a part of COD and BOD can also be removed by pre-aeration of the air blower 21, the waste water reacts in the comprehensive adjusting tank 9 for 12-24h, and the pH value is controlled to be 6-9 by an industrial pH meter; the grid well is arranged at the inlet of the comprehensive adjusting tank 9;
(8) and (3) ozone oxidation: the wastewater treated by the comprehensive adjusting tank 9 enters an ozone pre-oxidation tank 10, ozone is provided by an ozone generator 11, and the wastewater reacts in the ozone pre-oxidation tank 10 for 1h to remove organic matters in the wastewater;
(9) and AAO process: the wastewater treated by the ozone pre-oxidation tank 10 is pumped into an anaerobic tank 13 by a third sewage lift pump 12, the wastewater reacts in the anaerobic tank 13, an anoxic tank 14 and a contact oxidation tank 15, TP in the wastewater is removed by phosphorus accumulating bacteria anaerobic phosphorus release and aerobic phosphorus absorption, ammonia nitrogen in the wastewater is converted into nitrogen by nitrification of nitrifying bacteria and denitrification of denitrifying bacteria, a combined filler made of plastic flower pieces is hung in the contact oxidation tank 15, the diameter of the combined filler is phi 150 and 180mm, and the volume load of the BOD filler is 1-1.2kgBOD/m3The wastewater reacts in the contact oxidation tank 15 for 12-20h, aeration is provided by the blower 21, uniform gas supply is realized by a microporous aeration disc phi 215mm with the diameter phi 215mm uniformly distributed at the bottom of the tank through aeration, the gas-water ratio is 15-20: 1, returning the reacted nitrified liquid to an anaerobic tank 13 through a pipeline, and feeding the reacted wastewater into a secondary sedimentation tank 16;
(10) and secondary precipitation: the wastewater enters a secondary sedimentation tank 16 and then is sedimentated for 0.5h-1h, sludge and clear water are separated, a part of the generated sludge flows back to an anaerobic tank 13, the rest sludge enters a sludge tank 18, and the separated clear water is discharged into a flocculation sedimentation tank 17 through a pipeline; (11) and sludge treatment: discharging sludge in the sludge pool 18 into a sludge dewatering machine 19, adding 1 per thousand polyacrylamide by mass percent through a sludge conditioning agent dosing device 20, adding 1-3kg of polyacrylamide into each ton of dry sludge, dewatering through the sludge dewatering machine 19, and conveying to a refuse landfill for harmless treatment;
(12) and flocculating and precipitating: the suspended matters remained in the effluent of the secondary sedimentation tank 16 are biological floccules with the particle size of 10 mu m to several millimeters and uncoagulated colloid particles, which are the main cause of the chromaticity of the pharmaceutical wastewater, 50 to 80 percent of the BOD value of the effluent of the secondary sedimentation tank 16 is derived from the particles, therefore, 10 percent of PAC and 0.1 percent of PAM are added into the flocculation sedimentation tank 12, the wastewater reacts in the flocculation sedimentation tank 12 for 0.5 to 1 hour, and the supernatant reaches the standard and is discharged through a water outlet of the flocculation sedimentation tank 12.
The utility model discloses through application and test implementation, very good beneficial effect has been obtained, and specific data is as follows:
note: in the tables, but not labeled, all units are in mg/L.
As can be seen from the above, the utility model discloses an extract waste water and strengthen preliminary treatment (wherein the filter-pressing is collected to the fungus sediment) -mix with regeneration waste water-ozone advanced pre-oxidation-AAO-flocculation and precipitation combined technology handles this waste water, compares with prior art, has following advantage:
(1) after the extracted wastewater is pretreated by combining physicochemical (air flotation), electrochemical (electro-flocculation, electro-Fenton) and two-phase anaerobic processes (step 4 and step 6), high sulfate radicals, COD, BOD, most of ammonia nitrogen and TP in the water are removed, and then the wastewater is mixed with the regenerated wastewater to enter a subsequent conventional biochemical treatment facility;
(2) by reasonable process design and model selection, an air floatation process and an electrochemical process are added before a two-phase anaerobic process, indexes such as SS, TP, ammonia nitrogen and the like are reduced to a conventional biochemical treatment range while COD and sulfate radicals are removed in a pretreatment stage, the subsequent biochemical treatment difficulty is reduced, and the standard-reaching stability of the treatment of the whole system is ensured;
(3) in the pretreatment, a great amount of H generated by the acid-producing phase anaerobic reactor is treated by a trace sulfur removal unit arranged in the middle of a two-phase anaerobic process and process technical means such as pH adjustment, trace aeration, dosing precipitation and the like2S is oxidized to remove toxic H2S, toxic action on a subsequent methanogenic phase anaerobic reactor is avoided, and normal growth and propagation of methanogens are guaranteed, so that normal treatment efficiency and daily operation of the anaerobic reactor are guaranteed. The desulfurization tank adopts air as a gas source, compared with the traditional method of using N2Or a methane blowing-off mode, simple economy, reliability and safety, the utility model improves the biodegradability of the neomycin sulfate production wastewaterThe method removes high sulfate radical, most ammonia nitrogen and TP in water, saves the investment floor area and the operation cost on the basis of fully exerting the advantages of anaerobic treatment, reduces the treatment difficulty of the subsequent aerobic biochemical process stage, and has good social and economic benefits.
Claims (7)
1. A neomycin sulfate production wastewater treatment device comprises a preconditioning tank, an air flotation machine, a comprehensive adjusting tank and an anaerobic tank, and is characterized in that an outlet of the preconditioning tank (1) is communicated with an inlet of the air flotation machine (3) through a pipeline, a bacteria residue outlet of the air flotation machine (3) is communicated with an inlet of a hydraulic plate frame filter press (8) through a pipeline, a liquid outlet of the hydraulic plate frame filter press (8) is communicated with an inlet of the comprehensive adjusting tank (9) through a pipeline, a wastewater outlet of the air flotation machine (3) is communicated with an inlet of an electrochemical reactor (4) through a pipeline, an outlet of the electrochemical reactor (4) is communicated with an inlet of an acid-producing phase reactor (5) through a pipeline, an outlet of the acid-producing phase reactor (5) is communicated with an inlet of a desulfurizing tank (6) through a pipeline, an outlet of the desulfurizing tank (6) is communicated with an inlet of a methane-producing phase reactor (7) through a pipeline, an outlet of the methanogenic phase reactor (7) is communicated with an inlet of a comprehensive adjusting tank (9) through a pipeline, an outlet of the comprehensive adjusting tank (9) is communicated with an inlet of an ozone pre-oxidation tank (10) through a pipeline, a gas inlet of the ozone pre-oxidation tank (10) is communicated with a gas outlet of an ozone generator (11), an outlet of the ozone pre-oxidation tank (10) is communicated with an inlet of an anaerobic tank (13) through a pipeline, an outlet of the anaerobic tank (13) is communicated with an inlet of an anoxic tank (14) through a pipeline, an outlet of the anoxic tank (14) is communicated with an inlet of a contact oxidation tank (15) through a pipeline, a reflux port of the contact oxidation tank (15) is communicated with an inlet of the anoxic tank (14) through a pipeline, an outlet of the contact oxidation tank (15) is communicated with an inlet of a secondary sedimentation tank (16) through a pipeline, an outlet of the secondary sedimentation tank (16) is communicated with an inlet of a flocculation sedimentation tank (17, the sedimentation outlet of the secondary sedimentation tank (16) is respectively communicated with the inlet of a sludge tank (18) and the inlet pipeline of the anaerobic tank (13) through a three-way pipe (16-1), and the outlet of the sludge tank (18) is communicated with the inlet of a sludge dewatering machine (19) through a pipeline.
2. The neomycin sulfate production wastewater treatment equipment according to claim 1, characterized in that a first wastewater lift pump (2) is installed on a pipeline between the preconditioning tank (1) and the air flotation machine (3), a second wastewater lift pump (6-1) is installed on a pipeline between the desulfurization tank (6) and the methanogenic phase reactor (7), and a third wastewater lift pump (12) is installed on a pipeline between the ozone pre-oxidation tank (10) and the anaerobic tank (13).
3. The neomycin sulfate production wastewater treatment equipment according to claim 1, characterized in that the air inlets of the desulfurization tank (6), the comprehensive regulation tank (9) and the contact oxidation tank (15) are respectively communicated with the air outlet of the blower (21) through pipelines.
4. The neomycin sulfate production wastewater treatment plant according to claim 1, characterized in that a stirrer is installed in the preconditioning tank (1), and the power of the stirrer is 5-8W/m for carrying out labor year up.
5. The neomycin sulfate production wastewater treatment equipment according to claim 1, wherein a drug adding port of the air flotation machine (3) is communicated with a drug outlet of the automatic drug adding device (3-1), and a sludge conditioning agent adding device (20) is installed on a pipeline between the sludge tank (18) and the sludge dewatering machine (19).
6. The neomycin sulfate production wastewater treatment plant according to claim 1, characterized in that the sludge dewatering machine (19) is a hydraulic plate-frame dewatering machine or a stacked-screw sludge dewatering machine.
7. The neomycin sulfate production wastewater treatment plant of claim 1, wherein the volume ratio of the anaerobic tank (13), the anoxic tank (14) and the contact oxidation tank (15) is 1: 3 or 1: 4.
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