CN112551829A - Minamide technical production wastewater treatment device and method - Google Patents
Minamide technical production wastewater treatment device and method Download PDFInfo
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- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
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- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
Abstract
The invention discloses a device and a method for treating production wastewater of an imidazole amide technical material, which relate to the technical field of sewage treatment, wherein the device comprises a high-salinity wastewater pretreatment system and a comprehensive biochemical treatment system, wherein the high-salinity wastewater pretreatment system comprises a primary sedimentation tank, an electric flocculation device, an evaporation device, a Fenton advanced oxidation device and a physicochemical treatment device which are sequentially connected in series; the comprehensive biochemical treatment system comprises an anaerobic treatment device, an anoxic treatment device, an aerobic treatment device and a secondary sedimentation tank which are sequentially connected in series; the method of classifying, performing targeted pretreatment and performing comprehensive treatment at last can effectively solve the problems of a series of treatments on the imidazole amide technical production wastewater such as high salt content, high organic matter content, poor biochemical property and the like, the whole process can adapt to the fluctuation of the quality and quantity of the incoming water, the sludge generated by the whole system is digested as much as possible, the sludge treatment cost is greatly reduced, the process can realize the standard discharge of the wastewater, and the method has the advantages of stable operation, low operation cost, simple operation and management and the like.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a device and a method for treating prochloraz technical production wastewater.
Background
The imidazole amide is a high-efficiency, low-toxicity and low-residue spectral imidazole bactericide. It has obvious control effect on diseases of various crops caused by ascomycetes and adelomycetes; can be mixed with most pesticides, and has effects of treating and eradicating various diseases on field crops, vegetables and flowers. The bactericide is popularized and used in China at the end of the 20 th century, is widely applied to China in the processes of production, storage, transportation and the like of agricultural and forestry products such as grains, vegetables, fruits, flowers and the like at present, has obvious control effect, and is a bactericide which is widely applied in recent years. Since the century, a plurality of enterprises develop and put into production in China, a certain scale is formed at present, the capacity exceeds ten thousand tons, and the actual annual output reaches about 6000 t.
The synthesis method of the imidamide has various methods, and mainly comprises a phenol route and a trichlorophenol route. Wherein trichlorophenol is divided into a dibromoethane method and a dichloroethane method. The process is roughly as follows: 2,4, 6-trichlorophenol is subjected to a series of melting, alkali adding pulping and oil-water separation to obtain propylamine, the propylamine is acidified by hydrochloric acid to obtain secondary amine salt, the secondary amine salt and trichloromethyl carbonate are heated and refluxed in toluene to generate acyl chlorination reaction to obtain formyl chloride, and finally the formyl chloride and imidazole are condensed in the presence of triethylamine, and then the imidazole amide raw drug is obtained by water washing, triethylamine salt removal and vacuum desolventization.
In view of the addition of the raw materials, high-organic-content and high-chloride-ion wastewater can be generated in the production process of the imamide technical product, the biochemical property is very poor, and the potential adverse factors of sterilization are also provided. The currently common treatment processes comprise materialization and biochemistry, wherein the materialization comprises Fenton oxidation, coagulating sedimentation, evaporation and other processes, and the biochemistry comprises anaerobic, anoxic and aerobic processes. However, any process can not be used for treating the waste water stably and reach the standard, but how to combine the conventional processes can treat the imidazole amide waste water pertinently, the imidazole amide waste water can be treated efficiently and discharged after reaching the standard, the imidazole amide waste water can adapt to the change of concentration and water quantity, and the stable operation all the year round becomes a difficult problem.
Disclosure of Invention
The invention aims to provide a device and a method for treating raw imidamide pharmaceutical production wastewater, which can be used for solving the problems in the prior art, can synchronously remove salt inorganic substances and COD, can effectively solve a series of treatment problems of raw imidamide pharmaceutical production wastewater such as high salt, high organic substances, poor biochemical property and the like, can adapt to the fluctuation of the quality and quantity of incoming water, can digest sludge generated by the whole system as far as possible internally, greatly reduces the sludge treatment cost, can realize standard wastewater discharge, and has the advantages of stable operation, low operation cost, simple operation management and the like.
In order to achieve the purpose, the invention provides the following scheme:
the invention provides a device and a method for treating raw imidyl amide production wastewater, which comprise a high-salinity wastewater pretreatment system and a comprehensive biochemical treatment system, wherein the high-salinity wastewater pretreatment system is used for pretreating high-salinity wastewater, the high-salinity wastewater enters the high-salinity wastewater pretreatment system after passing through a high-salinity wastewater adjusting tank, and the high-salinity wastewater pretreatment system comprises a primary sedimentation tank, an electric flocculation device, an evaporation device, a Fenton advanced oxidation device and a physicochemical treatment device which are sequentially connected in series; synthesize biochemical treatment system including anaerobic treatment device, oxygen deficiency processing apparatus, aerobic treatment device and the two ponds that establish ties in proper order, low salt waste water gets into through low salt waste water equalizing basin anaerobic treatment device washes waste water and domestic sewage and gets into through the domestic sewage equalizing basin anaerobic treatment device, the high salt waste water after high salt waste water pretreatment system preliminary treatment gets into anaerobic treatment device.
Preferably, high salt wastewater pretreatment of systems still including set up in the electroflocculation device with evaporation water distribution tank between the evaporation plant, the fragrant advanced oxidation unit includes fenton water distribution tank and fenton tower, the fenton water distribution tank with evaporation plant intercommunication, materialization processing apparatus is including the pond of taking off gas, reaction tank and the sedimentation tank that communicate in proper order, take off the gas pond set up in the fenton tower tail end, the sediment effluent in the sedimentation tank lets in anaerobic treatment device, mud in the sedimentation tank lets in the sludge impoundment through the sludge pump.
Preferably, the sediments in the primary sedimentation tank and the electric flocculation device are introduced into the sludge tank through a sludge pump.
Preferably, anaerobic treatment device includes anaerobism distributing reservoir, anaerobic tower and oxygen deficiency pond, good oxygen treatment device includes good oxygen pond, anaerobism distributing reservoir, anaerobic tower, oxygen deficiency pond, good oxygen pond and two sink ponds communicate through the pipeline in proper order, two sink ponds still through mud backwash pump intercommunication good oxygen pond with the oxygen deficiency pond, two sink ponds communicate through the sludge pump sludge impoundment, two tail ends that sink the pond still communicate reaction tank, materialization sedimentation tank, clean water basin and filtering ponds in proper order, materialization sedimentation tank passes through the sludge pump and connects sludge impoundment.
Preferably, the aerobic tank is also connected with the anoxic tank through a reflux pump.
Preferably, the tail end of the sludge tank is connected with a plate-and-frame filter press.
Preferably, the high-salinity wastewater regulating tank, the low-salinity wastewater regulating tank and the domestic sewage regulating tank are internally provided with aeration stirring systems in a matching way.
Based on the above device for treating the prochloraz original drug production wastewater, the invention also provides a method for treating the prochloraz original drug production wastewater, which comprises the following steps:
s1: the high-salinity wastewater enters a high-salinity wastewater adjusting tank to homogenize the quality of the wastewater; the low-salt wastewater enters a low-salt wastewater adjusting tank to homogenize the quality of the wastewater; the flushing wastewater and the domestic sewage enter a domestic sewage regulating tank to homogenize the quality of the wastewater;
s2: pumping the high-salinity wastewater into a primary sedimentation tank and an electric flocculation device for pretreatment before evaporation, removing large-particle impurities and suspended matters through the primary sedimentation tank, and adding chemicals into the electric flocculation device to further remove micro suspended matters, colloids and insoluble organic matters;
s3: the effluent of the electric flocculation sedimentation tank overflows to an evaporation distribution tank, and then the wastewater is pumped into an evaporation system for evaporation treatment of the wastewater, so that salt and part of organic matters are removed;
s4: temporarily storing the evaporated condensate water in a Fenton water distribution pool, and adjusting the pH value to be acidic;
s5: pumping the high-salinity wastewater in the Fenton water distribution tank into a Fenton tower, strongly oxidizing wastewater organic matters by using an advanced oxidation agent, and overflowing the effluent of the Fenton tower into a degassing tank to remove excessive hydrogen peroxide;
s6: the effluent of the degassing tank flows to a reaction tank automatically, alkali and PAM are added for coagulation reaction, the effluent treated by the reaction tank is discharged into a sedimentation tank for mud-water separation, the sedimentation effluent is discharged into an anaerobic distribution tank, and the generated sludge is pumped into a sludge tank;
s7: mixing the low-salt wastewater, the flushing wastewater, the domestic sewage and the high-salt wastewater after the pretreatment in an anaerobic distribution tank, homogenizing, and pumping into an anaerobic tower after adjusting the pH value of the wastewater;
s8: enabling the effluent of the anaerobic tower to automatically flow into an anoxic tank and then automatically flow into an aerobic tank for biochemical reaction; the effluent of the aerobic tank automatically flows into a secondary sedimentation tank for sludge-water separation, the clear water at the upper layer enters a reaction tank for advanced treatment, the sludge at the lower layer partially flows back to the anoxic tank and the aerobic tank, and part of the sludge is pumped into a sludge tank;
s9: adding a flocculating agent into the reaction tank to further carry out deep physicochemical treatment on organic matters and suspended matters in the wastewater; after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank for mud-water separation, clear water is discharged into a clear water tank, filtered by a filter tank and discharged out after reaching the standard, and precipitated sludge is discharged into a sludge tank;
s10: and carrying out filter pressing on the sludge in the sludge tank, and transporting and disposing the sludge cakes.
Preferably, PAC and PAM agents are added to the electroflocculation apparatus in step S2;
adding sulfuric acid into an acid adjusting tank in the step S4 to adjust the pH value to 4-5;
the advanced oxidizing agent in step S5 includes hydrogen peroxide and ferrous sulfate; in the step S5, the degassing tank adopts an aeration stirring system to carry out aeration to remove excessive hydrogen peroxide, and the aeration intensity is controlled to be 5-10 m3/(m2·h)；
Adding alkali and PAM in the coagulation reaction process in the step S6, and adjusting the pH value to 8-9;
in the step S7, the wastewater of the anaerobic distribution tank is low-salt wastewater, flushing wastewater, domestic sewage and pretreated high-salt wastewater, and acid/alkali is added into the comprehensive wastewater to control the pH value to be 7-7.5;
step S8, sequentially carrying out anaerobic treatment and anoxic treatment on the wastewater to be treated, adjusting the pH value of the effluent to be alkaline, then carrying out aerobic treatment, and refluxing the nitrified liquid into an anoxic tank; returning the sludge in the secondary sedimentation tank to an anaerobic tower, an anoxic tank and an aerobic tank through a sludge pump in the step S8, and performing filter-pressing concentration treatment on the residual sedimentation sludge;
adding PAC and PAM medicaments into the reaction tank in the step S9;
and in the step S10, after the sludge passes through a dewatering device, the water content is 70% -80%, and the filtrate flows back to the anaerobic water distribution tank for continuous treatment.
Preferably, before entering an aerobic tank for aerobic treatment, the pH value is adjusted to 7.5-8.5;
refluxing the sludge-water mixed solution subjected to the anoxic treatment in the anoxic tank to an anaerobic tower according to the reflux ratio of 150-300%; refluxing the nitrified liquid after aerobic treatment in the aerobic tank to the anoxic treatment process in the anoxic tank according to the reflux ratio of 330-450%; and refluxing the precipitated sludge in the secondary sedimentation tank to an anaerobic tower, an anoxic tank and an aerobic tank according to the reflux ratio of 150-300%.
Compared with the prior art, the invention has the following beneficial technical effects:
the invention provides a device and a method for treating prochloraz original drug production wastewater. Firstly, wastewater is divided into three types, namely high-salinity wastewater, low-salinity wastewater, flushing wastewater and domestic sewage. The high-salinity wastewater adopts a pre-process route of 'primary sedimentation, electric flocculation, evaporation, Fenton advanced oxidation and physical and chemical treatment', large-particle impurities and suspended matters in the wastewater are removed, partial COD (chemical oxygen demand) is degraded, salt is removed, the toxicity of the wastewater is reduced, and the biodegradability is improved; the pretreated high-salinity wastewater, the low-salinity wastewater, the flushing wastewater and the domestic sewage are uniformly mixed and then are comprehensively treated, and a treatment process mainly comprising anaerobic treatment, anoxic treatment, aerobic treatment, secondary sedimentation treatment, physicochemical advanced treatment and filtering is mainly adopted. After the wastewater is treated, COD can be degraded from 35000mg/L to 400mg/L, ammonia nitrogen is treated from 210mg/L to 30mg/L, and chloride ions are treated from 21000mg/L to obtain final effluent of 600 mg/L. Meets the standard discharge limit value of class B in the Standard of wastewater discharge to urban sewer Water quality (GB/T31962 and 2015). The method can remove salt inorganic substances and COD synchronously, can effectively solve a series of treatment problems of high salt, high organic substances, poor biochemical property and the like of the imidazole amide technical production wastewater, can adapt to the fluctuation of the quality and quantity of the incoming water, can digest the sludge generated by the whole system as much as possible, greatly reduces the sludge treatment cost, can realize the standard-reaching discharge of the wastewater, and has the advantages of stable operation, low operation cost, simple operation and management and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a device for treating imazamide technical production wastewater in the invention;
FIG. 2 is a system flow chart of the method for treating imazamide technical production wastewater in the present invention;
in the figure: 1-high-salinity wastewater adjusting tank, 2-primary settling tank, 3-electrocoagulation device, 4-evaporation water distribution tank, 5-evaporation device, 6-fenton water distribution tank, 7-fenton tower, 8-degassing tank, 9-reaction tank, 10-sedimentation tank, 11-low-salinity wastewater adjusting tank, 12-domestic sewage adjusting tank, 13-anaerobic water distribution tank, 14-anaerobic tower, 15-anoxic tank, 16-aerobic tank, 17-secondary settling tank, 18-reaction tank, 19-materialized sedimentation tank, 20-clear water tank, 21-filtering tank, 22-sludge tank and 23-plate-and-frame filter press.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention aims to provide a device and a method for treating prochloraz technical production wastewater, which are used for solving the problems in the prior art.
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in further detail below.
The device for treating the raw iminamide production wastewater in the embodiment comprises a high-salt wastewater pretreatment system and a comprehensive biochemical treatment system, as shown in fig. 1, wherein the high-salt wastewater pretreatment system is used for pretreating high-salt wastewater, the high-salt wastewater enters the high-salt wastewater pretreatment system after passing through a high-salt wastewater adjusting tank 1, and the high-salt wastewater pretreatment system comprises a primary sedimentation tank 2, an electric flocculation device 3, an evaporation device 5, a fenton advanced oxidation device and a physicochemical treatment device which are sequentially connected in series; synthesize biochemical treatment system including anaerobic treatment device, oxygen deficiency processing apparatus, aerobic treatment device and the secondary sedimentation tank 17 that establishes ties in proper order, low salt waste water gets into through low salt waste water equalizing basin 11 anaerobic treatment device washes waste water and domestic sewage and gets into through domestic sewage equalizing basin 12 anaerobic treatment device, the high salt waste water after high salt waste water pretreatment system preliminary treatment gets into anaerobic treatment device.
In this embodiment, the high-salinity wastewater pretreatment system further includes an evaporation distribution tank 4 disposed between the electrocoagulation device 3 and the evaporation device 5, the fenton advanced oxidation device includes a fenton distribution tank 6 and a fenton tower 7, the fenton distribution tank 6 is communicated with the evaporation device 5, the physicochemical treatment device includes a degassing tank 8, a reaction tank 9 and a sedimentation tank 10 which are sequentially communicated, the degassing tank 8 is disposed at the tail end of the fenton tower 7, the precipitated effluent in the sedimentation tank 10 is introduced into the anaerobic treatment device, and the sludge in the sedimentation tank 10 is introduced into a sludge tank 22 through a sludge pump; the sediments in the primary sedimentation tank 2 and the electric flocculation device 3 are pumped into the sludge tank 22 through a sludge pump.
In this embodiment, the anaerobic treatment device includes an anaerobic distribution tank 13, an anaerobic tower 14 and an anoxic tank 15, the aerobic treatment device includes an aerobic tank 16, the anaerobic distribution tank 13, the anaerobic tower 14, the anoxic tank 15, the aerobic tank 16 and the secondary sedimentation tank 17 are sequentially communicated through a pipeline, the secondary sedimentation tank 17 is further communicated with the aerobic tank 16 and the anoxic tank 15 through a sludge reflux pump, the secondary sedimentation tank 17 is communicated with the sludge tank 22 through a sludge pump, the tail end of the secondary sedimentation tank 17 is further sequentially communicated with a reaction tank 18, a materialized sedimentation tank 19, a clean water tank 20 and a filter tank 21, the materialized sedimentation tank 19 is connected with the sludge tank 22 through a sludge pump, and the tail end of the sludge tank 22 is connected with a plate-and frame filter press 23. The aerobic tank 16 is also connected with the anoxic tank 15 through a reflux pump.
In the embodiment, the aeration stirring systems are arranged in the high-salinity wastewater regulating tank 1, the low-salinity wastewater regulating tank 11 and the domestic sewage regulating tank 12 in a matching way. The evaporation device 5 is a multi-effect evaporator.
Based on above miamide former medicine waste water processing apparatus, this embodiment still provides a miamide former medicine waste water treatment method, combines fig. 2, includes the following step:
s1: the high-salinity wastewater enters a high-salinity wastewater adjusting tank 1 to homogenize the quality of the wastewater; the low-salt wastewater enters a low-salt wastewater adjusting tank 11 to homogenize the quality of the wastewater; the flushing wastewater and the domestic sewage enter a domestic sewage adjusting tank 12 to homogenize the quality of the wastewater;
s2: pumping the high-salinity wastewater into a primary sedimentation tank 2 and an electric flocculation device 3 for pretreatment before evaporation, removing large-particle impurities and suspended matters through the primary sedimentation tank 2, and adding medicines into the electric flocculation device 3 to further remove micro suspended matters, colloids and insoluble organic matters;
s3: the effluent of the electric flocculation sedimentation tank 10 overflows to an evaporation distribution tank 4, and then the wastewater is pumped into an evaporation system for evaporation treatment of the wastewater, so that salt and part of organic matters are removed;
s4: temporarily storing the evaporated condensate water in a Fenton water distribution tank 6, and adjusting the pH value to be acidic;
s5: pumping the high-salinity wastewater in the Fenton water distribution tank 6 into a Fenton tower 7, strongly oxidizing wastewater organic matters by using an advanced oxidation agent, and overflowing the effluent of the Fenton tower 7 to a degassing tank 8 to remove excessive hydrogen peroxide;
s6: the effluent of the degassing tank 8 automatically flows to a reaction tank 9, alkali and PAM are added for coagulation reaction, the effluent treated by the reaction tank 9 is discharged into a sedimentation tank 10 for mud-water separation, the sedimentation effluent is discharged into an anaerobic distribution tank 13, and the generated sludge is pumped into a sludge tank 22;
s7: mixing the low-salt wastewater, the flushing wastewater and the domestic sewage, and the pretreated high-salt wastewater in an anaerobic distribution tank 13, homogenizing, and pumping into an anaerobic tower 14 after adjusting the pH value of the wastewater;
s8: macromolecular pollutants in the wastewater in the anaerobic tower 14 become micromolecular pollutants, pollutants which are difficult to degrade become pollutants which are easy to degrade, the biodegradability of the sewage is improved, organic matters are removed in the anaerobic tower 14, and methane is generated. The temperature is reduced in winter, and the temperature of the anaerobic tower 14 is ensured to be between 35 and 38 ℃ by controlling the temperature of the anaerobic distribution tank 13;
s9: enabling the effluent of the anaerobic tower 14 to automatically flow into an anoxic tank 15 and then automatically flow into an aerobic tank 16 for biochemical reaction; removing total nitrogen of ammonia nitrogen and a small amount of phosphorus;
s10: the effluent of the aerobic tank 16 automatically flows into a secondary sedimentation tank 17 for mud-water separation, the clear water at the upper layer enters a reaction tank 18 for advanced treatment, the sludge at the lower layer partially flows back to the anoxic tank 15 and the aerobic tank 16, and part of the sludge is pumped into a sludge tank 22;
s11: adding a flocculating agent into the reaction tank 18 to further carry out deep physicochemical treatment on organic matters and suspended matters in the wastewater; after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank 19 for mud-water separation, clear water is discharged into a clear water tank 20 and is filtered by a filter tank 21 to be discharged out after reaching the standard, and precipitated sludge is discharged into a sludge tank 22;
s12: the sludge in the sludge tank 22 is subjected to pressure filtration, and the sludge cake is transported to the outside for disposal.
In this embodiment, the adjusting tanks in step S1 are all matched with aeration stirring systems, and the aeration intensity is 2-4 m3/(m2·h)。
In the step S2, PAC and PAM chemical are added to the electrocoagulation device 3, and the amount of PAC added is0.3 to 0.5kg/m3The addition amount of the PAM is 0.005-0.01 kg/m3And (4) waste water.
The evaporation device 5 used in the evaporation system in the step S3 is a multi-effect evaporator, and the flow passage component is made of 316L material.
Adding sulfuric acid into the acid regulating tank in the step S4 to regulate the pH value to 4-5; the strong oxidizing oxidant comprises hydrogen peroxide and ferrous sulfate; the addition amount of the hydrogen peroxide is 0.5-1 kg/m3The addition amount of the ferrous sulfate is 0.5-1 kg/m3Waste water; the degassing tank 8 adopts an aeration stirring system to carry out aeration and removal of excessive hydrogen peroxide, and the aeration intensity is controlled to be 5-10 m3/(m2·h)。
Adding alkali and PAM in the iron mud coagulation reaction process in the step S6; the addition amount of the PAM is 0.005-0.01 kg/m3Waste water; adjusting the pH value to 8-9 in the iron mud coagulation reaction process;
preferably, in the step S7, the wastewater of the anaerobic distribution tank 13 is low-salt wastewater, flushing wastewater, domestic sewage, and pretreated high-salt wastewater, acid/alkali is added into the comprehensive wastewater to control the pH to be about 7-7.5, and meanwhile, part of the anaerobic effluent can flow back to the distribution tank;
in the biochemical treatment process in the step S8, the wastewater to be treated is sequentially subjected to anaerobic treatment and anoxic treatment, the pH value of the effluent is adjusted to be alkaline and then aerobic treatment is performed, and the nitrified liquid flows back to the anoxic treatment process of the anoxic tank 15; and before the aerobic treatment, adjusting the pH value to 7.5-8.5. The type of the alkali reagent is not particularly limited, and the pH value can be ensured to be within a required range, specifically, the alkali reagent is a NaOH solution with the mass concentration of 20%.
In the anoxic and aerobic comprehensive treatment process, the dissolved oxygen of anoxic treatment is less than or equal to 0.2mg/L, and the carbon-nitrogen ratio is (4-5): 1, the aeration rate of the anoxic treatment is 0.5-1.0 m3/(m2H); the dissolved oxygen of the aerobic treatment is 3-5 mg/L, and the aeration rate of the aerobic treatment is 5-6 m3/(m2·h)。
And refluxing the sludge-water mixed solution subjected to the anoxic treatment in the anoxic tank 15 to the anaerobic treatment process of the anaerobic tower 14 according to the reflux ratio of 150-300%.
And refluxing the nitrified liquid after the aerobic treatment in the aerobic tank 16 to the anoxic treatment process in the anoxic tank 15 according to the reflux ratio of 330-450%. More preferably 350 to 400%. The invention preferably returns the nitrifying liquid to the anoxic treatment process under the condition of the reflux ratio, which is favorable for meeting the requirement of the denitrification of the heterotrophic bacteria on NO under the anoxic condition3-And is beneficial to reducing energy consumption. If the reflux ratio of the nitrifying liquid is too low or too high, the denitrification effect in the anoxic treatment stage is not fully ensured, so that the removal rate of nitrogen in the final effluent is low; moreover, the reflux ratio of the nitrified liquid is too high, so that the hydraulic retention time in the anoxic treatment stage is shortened, and the effluent quality is influenced.
After the biochemical treatment, the wastewater after the biochemical treatment is preferably subjected to precipitation treatment to obtain the wastewater after the precipitation treatment and the precipitated sludge. In the invention, the sedimentation treatment has the function of realizing sludge-water separation, so that the effluent is clearer and the sludge loss is avoided. The present invention is not particularly limited with respect to the specific operating conditions for the precipitation treatment, and those known to those skilled in the art may be used.
Preferably, the precipitated sludge in the secondary sedimentation tank 17 is refluxed to the anaerobic treatment, anoxic treatment and aerobic treatment processes according to the reflux ratio of 150-300%. Wherein the volume ratio of the precipitated sludge which flows back to the anaerobic treatment, the anoxic treatment and the aerobic treatment is 1: (0.9-1.1): (7.5 to 8.5), more preferably 1: 1: 8.
the surface load of the secondary sedimentation tank 17 is 0.6-0.8 m3/(m2·h)。
The hydraulic retention time of the anaerobic tower 14 is 1.5-2.5 d, and the organic load is 0.8-2 kgCOD/(m)3D); the residence time of the anoxic and aerobic tank 16 is 2-4 days, and the organic load is 0.8-1.2 kgCOD/(m)3·d)。
A submersible mixer is arranged in the anoxic pond 15, and the power configuration is 6-12 (W/m)3A tank body);
the sludge settlement ratio (SV30) of the anaerobic treatment is preferably 80-90%; the invention preferably controls the sludge sedimentation ratio of the anaerobic treatment within the range, and simultaneously cooperates with the sludge sedimentation ratio in the subsequent anoxic treatment and aerobic treatment processes, thereby being beneficial to ensuring that ammonia nitrogen and total nitrogen in the wastewater are fully removed, and if the sludge sedimentation ratio of the anaerobic treatment is too low, the ammonia nitrogen and/or the total nitrogen in the final effluent are easy to not reach the standard.
In the invention, the sludge sedimentation ratio (SV30) of the anoxic and aerobic comprehensive treatment is preferably 70-80%; the invention preferably controls the sludge sedimentation ratio of the anoxic and aerobic comprehensive treatment within the range and simultaneously matches the sludge sedimentation ratio in the anaerobic treatment, which is favorable for ensuring that ammonia nitrogen and total nitrogen in the wastewater are fully removed, and if the sludge sedimentation ratio of the anoxic and aerobic comprehensive treatment is too low, the ammonia nitrogen and/or the total nitrogen in the final effluent are not up to the standard.
In step S11, the pharmaceutical agent in the reaction tank 18 adopts polyaluminium chloride (PAC) flocculant and anionic Polyacrylamide (PAM) coagulant, wherein Al in the PAC flocculant is2O3The content is preferably 24%, and the molecular weight of the PAM coagulant is preferably 1200 ten thousand. The addition amount of the PAC is 0.1-0.3 kg/m3The addition amount of the PAM is 0.005-0.01 kg/m3And (4) waste water.
In the invention, the physicochemical precipitation treatment aims at realizing mud-water separation, enabling the effluent to be clearer and avoiding sludge loss. The specific operation conditions for the mud-water separation in the present invention are not particularly limited, and those well known to those skilled in the art may be used. After the physicochemical precipitation treatment, the obtained effluent reaches the discharge standard and can be directly discharged.
Preferably, the materialized precipitated sludge is obtained after the materialized precipitation treatment, and the materialized precipitated sludge is subjected to filter pressing concentration treatment.
Preferably, in the step S12, after the sludge passes through the dewatering equipment, the water content is 70% to 80%, and the filtrate flows back to the anaerobic distribution tank 13 for further treatment. The present invention is not particularly limited to the above-mentioned filter-pressing concentration treatment, and the method of filter-pressing concentration treatment of the precipitated sludge may be referred to.
The principle and the implementation mode of the invention are explained by applying specific examples, and the description of the above examples is only used for helping understanding the method and the core idea of the invention; meanwhile, for a person skilled in the art, according to the idea of the present invention, the specific embodiments and the application range may be changed. In summary, this summary should not be construed to limit the present invention.
Claims (10)
1. The utility model provides a miamide former medicine waste water processing apparatus which characterized in that: the system comprises a high-salinity wastewater pretreatment system and a comprehensive biochemical treatment system, wherein the high-salinity wastewater pretreatment system is used for pretreating high-salinity wastewater, the high-salinity wastewater enters the high-salinity wastewater pretreatment system after passing through a high-salinity wastewater adjusting tank, and the high-salinity wastewater pretreatment system comprises a primary sedimentation tank, an electric flocculation device, an evaporation device, a Fenton advanced oxidation device and a physicochemical treatment device which are sequentially connected in series; synthesize biochemical treatment system including anaerobic treatment device, oxygen deficiency processing apparatus, aerobic treatment device and the two ponds that establish ties in proper order, low salt waste water gets into through low salt waste water equalizing basin anaerobic treatment device washes waste water and domestic sewage and gets into through the domestic sewage equalizing basin anaerobic treatment device, the high salt waste water after high salt waste water pretreatment system preliminary treatment gets into anaerobic treatment device.
2. The prochloraz-containing raw material production wastewater treatment device according to claim 1, wherein: high salt pretreatment of water system still including set up in the electric flocculation device with evaporation distribution tank between the evaporation plant, the fragrant advanced oxidation device includes the fragrant pool and the fragrant tower of joining in marriage, the fragrant pool with evaporation plant intercommunication, the materialization processing apparatus is including the pond of taking off gas, reaction tank and the sedimentation tank that communicate in proper order, take off gas the pond set up in the fragrant tower tail end, the sediment effluent in the sedimentation tank lets in anaerobic treatment device, mud in the sedimentation tank lets in the sludge impoundment through the sludge pump.
3. The prochloraz-containing raw material production wastewater treatment device according to claim 2, wherein: and the sediments in the primary sedimentation tank and the electric flocculation device are introduced into the sludge tank through a sludge pump.
4. The prochloraz-containing raw material production wastewater treatment device according to claim 2, wherein: the anaerobic treatment device comprises an anaerobic distribution tank, an anaerobic tower and an anoxic tank, the aerobic treatment device comprises an aerobic tank, the anaerobic distribution tank, the anaerobic tower, the anoxic tank, the aerobic tank and the secondary sedimentation tank are sequentially communicated through pipelines, the secondary sedimentation tank is further communicated with the aerobic tank and the anoxic tank through a sludge reflux pump, the secondary sedimentation tank is communicated with the sludge tank through a sludge pump, the tail end of the secondary sedimentation tank is further sequentially communicated with a reaction tank, a materialized sedimentation tank, a clear water tank and a filtering tank, and the materialized sedimentation tank is connected with the sludge tank through a sludge pump.
5. The prochloraz-containing raw material production wastewater treatment device according to claim 1, wherein: the aerobic tank is also connected with the anoxic tank through a reflux pump.
6. The prochloraz-containing raw material production wastewater treatment device according to claim 1, wherein: the tail end of the sludge tank is connected with a plate-and-frame filter press.
7. The prochloraz-containing raw material production wastewater treatment device according to claim 1, wherein: and aeration stirring systems are arranged in the high-salinity wastewater regulating tank, the low-salinity wastewater regulating tank and the domestic sewage regulating tank in a matched manner.
8. A method for treating imazamide technical production wastewater based on the apparatus for treating imazamide technical production wastewater according to any one of claims 1 to 7, comprising the steps of:
s1: the high-salinity wastewater enters a high-salinity wastewater adjusting tank to homogenize the quality of the wastewater; the low-salt wastewater enters a low-salt wastewater adjusting tank to homogenize the quality of the wastewater; the flushing wastewater and the domestic sewage enter a domestic sewage regulating tank to homogenize the quality of the wastewater;
s2: pumping the high-salinity wastewater into a primary sedimentation tank and an electric flocculation device for pretreatment before evaporation, removing large-particle impurities and suspended matters through the primary sedimentation tank, and adding chemicals into the electric flocculation device to further remove micro suspended matters, colloids and insoluble organic matters;
s3: the effluent of the electric flocculation sedimentation tank overflows to an evaporation distribution tank, and then the wastewater is pumped into an evaporation system for evaporation treatment of the wastewater, so that salt and part of organic matters are removed;
s4: temporarily storing the evaporated condensate water in a Fenton water distribution pool, and adjusting the pH value to be acidic;
s5: pumping the high-salinity wastewater in the Fenton water distribution tank into a Fenton tower, strongly oxidizing wastewater organic matters by using an advanced oxidation agent, and overflowing the effluent of the Fenton tower into a degassing tank to remove excessive hydrogen peroxide;
s6: the effluent of the degassing tank flows to a reaction tank automatically, alkali and PAM are added for coagulation reaction, the effluent treated by the reaction tank is discharged into a sedimentation tank for mud-water separation, the sedimentation effluent is discharged into an anaerobic distribution tank, and the generated sludge is pumped into a sludge tank;
s7: mixing the low-salt wastewater, the flushing wastewater, the domestic sewage and the high-salt wastewater after the pretreatment in an anaerobic distribution tank, homogenizing, and pumping into an anaerobic tower after adjusting the pH value of the wastewater;
s8: enabling the effluent of the anaerobic tower to automatically flow into an anoxic tank and then automatically flow into an aerobic tank for biochemical reaction; the effluent of the aerobic tank automatically flows into a secondary sedimentation tank for sludge-water separation, the clear water at the upper layer enters a reaction tank for advanced treatment, the sludge at the lower layer partially flows back to the anoxic tank and the aerobic tank, and part of the sludge is pumped into a sludge tank;
s9: adding a flocculating agent into the reaction tank to further carry out deep physicochemical treatment on organic matters and suspended matters in the wastewater; after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank for mud-water separation, clear water is discharged into a clear water tank, filtered by a filter tank and discharged out after reaching the standard, and precipitated sludge is discharged into a sludge tank;
s10: and carrying out filter pressing on the sludge in the sludge tank, and transporting and disposing the sludge cakes.
9. The method for treating imazamide technical production wastewater according to claim 8, comprising the steps of:
adding PAC and PAM agents into the electric flocculation device in step S2;
adding sulfuric acid into an acid adjusting tank in the step S4 to adjust the pH value to 4-5;
the advanced oxidizing agent in step S5 includes hydrogen peroxide and ferrous sulfate; in the step S5, the degassing tank adopts an aeration stirring system to carry out aeration to remove excessive hydrogen peroxide, and the aeration intensity is controlled to be 5-10 m3/(m2·h)；
Adding alkali and PAM in the coagulation reaction process in the step S6, and adjusting the pH value to 8-9;
in the step S7, the wastewater of the anaerobic distribution tank is low-salt wastewater, flushing wastewater, domestic sewage and pretreated high-salt wastewater, and acid/alkali is added into the comprehensive wastewater to control the pH value to be 7-7.5;
step S8, sequentially carrying out anaerobic treatment and anoxic treatment on the wastewater to be treated, adjusting the pH value of the effluent to be alkaline, then carrying out aerobic treatment, and refluxing the nitrified liquid into an anoxic tank; returning the sludge in the secondary sedimentation tank to an anaerobic tower, an anoxic tank and an aerobic tank through a sludge pump in the step S8, and performing filter-pressing concentration treatment on the residual sedimentation sludge;
adding PAC and PAM medicaments into the reaction tank in the step S9;
and in the step S10, after the sludge passes through a dewatering device, the water content is 70% -80%, and the filtrate flows back to the anaerobic water distribution tank for continuous treatment.
10. The method for treating imazamide technical production wastewater according to claim 8, comprising the steps of:
before entering an aerobic tank for aerobic treatment, adjusting the pH value to 7.5-8.5;
refluxing the sludge-water mixed solution subjected to the anoxic treatment in the anoxic tank to an anaerobic tower according to the reflux ratio of 150-300%; refluxing the nitrified liquid after aerobic treatment in the aerobic tank to the anoxic treatment process in the anoxic tank according to the reflux ratio of 330-450%; and refluxing the precipitated sludge in the secondary sedimentation tank to an anaerobic tower, an anoxic tank and an aerobic tank according to the reflux ratio of 150-300%.
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