CN113429087A - Method for treating perfume oil-containing wastewater by activated sludge-biofilm symbiotic system - Google Patents
Method for treating perfume oil-containing wastewater by activated sludge-biofilm symbiotic system Download PDFInfo
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Abstract
The invention provides a method for treating perfume oily wastewater by an activated sludge-biofilm symbiotic system, which sequentially comprises the following steps of: the method comprises the following steps of three-stage oil separation treatment, air floatation machine treatment, biochemical regulating tank treatment, comprehensive air floatation machine treatment, hydrolytic acidification treatment, primary sedimentation tank treatment, anaerobic distribution tank treatment, EGSB anaerobic reactor treatment, multi-stage A/O and sedimentation tank treatment and mixed sedimentation treatment, wherein the mixed sedimentation treatment is carried out and then the mixture sedimentation treatment enters a discharge tank for discharge; the domestic oily wastewater passes through a low-concentration wastewater tank, then goes through three-stage oil separation treatment and air flotation machine treatment, and directly enters a biochemical regulating tank for treatment; wherein, the hydrolytic acidification treatment adopts an activated sludge method, and organism fillers are not arranged in a tank body of the hydrolytic acidification treatment. The invention can avoid forming a biological membrane which can not be metabolized normally, eliminate the influence of dissolved oil in the wastewater, improve the whole biochemical reaction environment of the process and ensure the sewage treatment effect.
Description
Technical Field
The invention relates to the technical field of oily wastewater treatment, in particular to a method for treating perfume oily wastewater by an activated sludge-biofilm symbiotic system.
Background
In some industrial processes, oily wastewater, such as perfume oily wastewater, is produced, and the process oily wastewater is produced by the production operations of the production and management units. The environmental pollution of the water body can be influenced if the oily wastewater is directly discharged without being treated.
At present, the oily wastewater is treated mainly by an anaerobic hydrolysis tank and a contact oxidation tank, some treatment processes adopt a hydrolysis acidification tank, organism fillers are generally arranged in a tank body, the hydrolysis acidification tank mainly utilizes the difference of hydrolysis, acid production and methane bacteria growth speed by adjusting hydraulic retention time, and methane bacteria are difficult to breed in a reactor by utilizing the flow of water, so the hydraulic retention time is an important control condition for stable operation at the stage. The technical specification of the sewage treatment engineering of the hydrolytic acidification reactor (HJ 2047-; the biomembrane formed by the biological filler can continuously adsorb petroleum substances in water, and finally oil-coated mud is formed on the stationary phase, so that the growth of microorganisms is inhibited, the microorganisms in the biomembrane can not be metabolized normally, and the sewage treatment effect is not ensured.
Disclosure of Invention
In order to solve the technical problem, the invention provides a method for treating perfume oily wastewater by an activated sludge-biofilm symbiotic system, which comprises the following steps of:
the method comprises the following steps of three-stage oil separation treatment, air floatation machine treatment, biochemical regulating tank treatment, comprehensive air floatation machine treatment, hydrolytic acidification treatment, primary sedimentation tank treatment, anaerobic distribution tank treatment, EGSB anaerobic reactor treatment, multi-stage A/O and sedimentation tank treatment and mixed sedimentation treatment, wherein the mixed sedimentation treatment is carried out and then the mixture sedimentation treatment enters a discharge tank for discharge;
the domestic oily wastewater passes through a low-concentration wastewater tank, then goes through three-stage oil separation treatment and air flotation machine treatment, and directly enters a biochemical regulating tank for treatment;
wherein, the hydrolytic acidification treatment adopts an activated sludge method, and organism fillers are not arranged in a tank body of the hydrolytic acidification treatment.
Optionally, polyacrylamide and polyaluminum chloride are added in the air flotation machine treatment and the comprehensive air flotation machine treatment, or polyacrylamide and alkali are added;
and adding activated carbon and polyaluminium chloride or activated carbon and polyacrylamide in the mixing and precipitating treatment.
Optionally, the treatment residence time of the anaerobic distribution tank is designed to be 5 days, and the anaerobic tank adopts a parallel and serial operation mode.
Optionally, in the multi-stage a/O and sedimentation tank treatment, each stage is first subjected to a/O treatment, and then subjected to sedimentation tank treatment; wherein the A/O treatment comprises a front-section anoxic section A and a rear-section aerobic section O which are connected in series.
Optionally, the activated sludge hydrolysis acidification treatment method adopts a sludge reflux form treated by a last-stage sedimentation tank to supplement the sludge.
Optionally, the front-stage anoxic section a in the a/O treatment is in the form of a biological filler; the sludge in each stage of A/O treatment is supplemented from the same stage of sedimentation tank.
Optionally, the oil stain separated by the three-stage oil separation treatment is conveyed to an oil phase collection tank for temporary storage, and the oil phase collection tank is subjected to oil phase recovery or incineration at regular time; the sludge discharged after the treatment of the A/O and sedimentation tank enters a first sludge concentration tank; and the sludge discharged by the first sludge concentration tank, the air floatation machine treatment and the comprehensive air floatation machine treatment enters a second sludge concentration tank.
Optionally, a central rotating wheel in the comprehensive air flotation machine is adopted for treatment by the comprehensive air flotation machine, a plurality of wheel blades are uniformly arranged on the outer cylindrical side surface of the central rotating wheel in the circumferential direction, and the blade surfaces of the wheel blades are parallel to the axial direction of the central rotating wheel;
the vanes are provided with a first adjusting part and a second adjusting part, the first adjusting part and the second adjusting part are positioned at positions of the vanes far away from the central rotating wheel, and the first adjusting part is used for influencing the stirring function; the second adjusting part is used for influencing the bubble function;
the vane is also provided with a third adjusting part and a fourth adjusting part which are respectively arranged at the first adjusting part and the second adjusting part; the third regulating part is used for increasing the generation amount of bubbles; the fourth adjusting part is used for reducing load;
the third adjusting part comprises a plurality of through holes, the through holes are regular polygons or circles, and the through holes are arranged in staggered manner at intervals in a longitudinal and transverse direction;
the fourth adjusting part comprises a long through hole and a hinge, the size of the long through hole along the radial direction of the central rotating wheel is larger than the size of the long through hole along the parallel direction of the central rotating wheel shaft, the size of the hinge is not smaller than that of the long through hole, the hinge is hinged with the edge of the long through hole, and the hinge can cover and shield the long through hole when the hinge deflects to be parallel to the wheel blade.
Optionally, a temperature adjusting device is arranged in the EGSB anaerobic reactor treatment for temperature control, the temperature adjusting device comprises a temperature detection module, a heat exchange module, a heat source module, a conveying module and a main control module, and the heat exchange module is connected with the heat source module through the conveying module;
the temperature detection module is used for detecting the temperature of the EGSB anaerobic reactor during treatment;
the heat exchange module is used for exchanging heat with wastewater during the treatment of the EGSB anaerobic reactor;
the heat source module is provided with a heat source valve and is used for generating heat;
the conveying module comprises a medium, a medium pipeline and a circulating pump; the medium pipeline is respectively connected with the heat exchange module and the heat source module, and the medium is driven by the circulating pump to circularly flow in the medium pipeline;
the main control module is respectively electrically connected with the temperature detection module, the heat source valve and the circulating pump, and heat is conveyed to the heat exchange module to exchange heat with wastewater according to the treatment requirement of the EGSB anaerobic reactor.
Optionally, the heat source module comprises a solar heat collector, a heat storage tank and an electric heater, the solar heat collector is connected with the heat storage tank through a heat medium pipeline, the electric heater is arranged in the heat storage tank, and the electric heater is electrically connected with the main control module; the heat storage tank is connected with a heat source valve and a medium pipeline.
The method for treating the perfume oily wastewater by the activated sludge-biofilm symbiotic system comprises the steps of sequentially carrying out three-stage oil separation treatment, air floatation machine treatment, biochemical regulation tank treatment, comprehensive air floatation machine treatment, hydrolytic acidification treatment, primary sedimentation tank treatment, anaerobic distribution tank treatment, EGSB (expanded granular sludge bed) anaerobic reactor treatment, multi-stage A/O and sedimentation tank treatment and mixed sedimentation treatment on the process oily wastewater, and discharging the process oily wastewater in a discharge tank after the mixed sedimentation treatment; firstly, emulsified oil and dissolved oil exist in water, and if a film hanging mode is adopted, although high biomass can be ensured, a biological film can continuously adsorb petroleum substances in water, finally oil-coated mud is formed on a fixed phase, the growth of microorganisms is inhibited, the microorganisms in the biological film can not be metabolized normally, and the sewage treatment effect cannot be ensured; secondly, the biochemical property of the wastewater is high, the B/C is estimated to be more than 0.4, the sludge proliferation rate is high, and the sludge can be timely updated by adopting an activated sludge method with high fluidity; thirdly, the mud discharged from the primary settling tank can discharge the oil mud absorbing the oil in time, and the influence of the oil dissolved in the water is eliminated. The hydrolysis acidification tank can adopt active sludge refluxed at the rear section to supplement sludge, which is beneficial to improving the whole biochemical reaction environment and ensuring the stable operation of the system; and the domestic oily wastewater passes through the low-concentration wastewater tank, then passes through the three-stage oil separation treatment and the air floatation machine treatment, and directly enters the biochemical regulating tank for treatment.
Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended drawings.
The technical solution of the present invention is further described in detail by the accompanying drawings and embodiments.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a flow chart of a method for treating aromatic oily wastewater by an activated sludge-biofilm symbiotic system in an embodiment of the invention;
FIG. 2 is a flow chart of an example of A/O and sedimentation tank treatment adopted by the method for treating the perfume oily wastewater by using the activated sludge-biofilm symbiotic system;
FIG. 3 is a schematic view of an embodiment of a central rotating wheel of an integrated air flotation machine used for the integrated air flotation machine treatment in the method for treating the perfume oily wastewater by using the activated sludge-biofilm symbiotic system;
FIG. 4 is a schematic view of a vane in the embodiment of FIG. 3;
FIG. 5 is a flow chart of the method for treating the perfume oil-containing wastewater in a certain plant area by using the activated sludge-biofilm symbiotic system of the invention.
Detailed Description
The preferred embodiments of the present invention will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein for the purpose of illustration and explanation and not limitation.
As shown in fig. 1, the embodiment of the present invention provides a method for treating perfume oily wastewater by using an activated sludge-biofilm symbiotic system, which sequentially comprises the following steps:
three-stage oil separation treatment S1, air floatation machine treatment S2, biochemical regulation tank treatment S3, comprehensive air floatation machine treatment S4, hydrolytic acidification treatment S5, primary sedimentation tank treatment S6, anaerobic distribution tank treatment S7, EGSB anaerobic reactor treatment S8, multi-stage A/O and sedimentation tank treatment S9 and mixed sedimentation treatment S10, wherein mixed sedimentation treatment S10 is discharged into a discharge tank;
the domestic oily wastewater passes through a low-concentration wastewater tank, then goes through three-level oil separation treatment S1 and an air flotation machine treatment S2, and directly enters a biochemical regulating tank for treatment S3;
wherein the hydrolytic acidification S5 adopts an activated sludge method, and organism fillers are not arranged in the tank body of the hydrolytic acidification S5.
The working principle and the beneficial effects of the technical scheme are as follows: the technical scheme is that the oily wastewater of the process is subjected to three-level oil separation treatment, air floatation machine treatment, biochemical regulation tank treatment, comprehensive air floatation machine treatment, hydrolytic acidification treatment, primary sedimentation tank treatment, anaerobic distribution tank treatment, EGSB anaerobic reactor treatment, multi-level A/O and sedimentation tank treatment and mixed sedimentation treatment in sequence, and enters a discharge tank for discharge after mixed sedimentation treatment; firstly, emulsified oil and dissolved oil exist in water, and if a film hanging mode is adopted, although high biomass can be ensured, a biological film can continuously adsorb petroleum substances in water, finally oil-coated mud is formed on a fixed phase, the growth of microorganisms is inhibited, the microorganisms in the biological film can not be metabolized normally, and the sewage treatment effect cannot be ensured; secondly, the biochemical property of the wastewater is high, the B/C is estimated to be more than 0.4, the sludge proliferation rate is high, and the sludge can be timely updated by adopting an activated sludge method with high fluidity; thirdly, the mud discharged from the primary settling tank can discharge the oil mud absorbing the oil in time, and the influence of the oil dissolved in the water is eliminated. The hydrolysis acidification tank can adopt active sludge refluxed at the rear section to supplement sludge, which is beneficial to improving the whole biochemical reaction environment and ensuring the stable operation of the system; and the domestic oily wastewater passes through the low-concentration wastewater tank, then passes through the three-stage oil separation treatment and the air floatation machine treatment, and directly enters the biochemical regulating tank for treatment.
In one embodiment, polyacrylamide and polyaluminum chloride are added in the air flotation machine treatment and the comprehensive air flotation machine treatment, or polyacrylamide and alkali are added; and adding activated carbon and polyaluminium chloride or activated carbon and polyacrylamide in the mixing and precipitating treatment.
The working principle and the beneficial effects of the technical scheme are as follows: according to the scheme, by adding polyacrylamide PAM and polyaluminum chloride PAC or adding polyacrylamide PAM and alkali in the air flotation machine treatment and the comprehensive air flotation machine treatment, suspended matters in the sewage can be promoted to float to the surface of the wastewater, and the separation is facilitated; activated carbon and polyaluminium chloride PAC or activated carbon and polyacrylamide PAM are added in the mixing and settling treatment, so that the emission standard can be more finely controlled, and the emission error can be avoided.
In one embodiment, the anaerobic distribution tank treatment residence time is designed to be 5 days, and the anaerobic treatment adopts a parallel-series operation mode.
The working principle and the beneficial effects of the technical scheme are as follows: due to the fact that biodegradability of the wastewater is high, excessive hydrolysis acidification is easy to occur in too long retention time under the condition, so that the anaerobic methane production stage is difficult to play a role, and even the situations that an anaerobic tower has no removal rate and no methane is generated occur. Referring to the results of field experiments in a certain plant area, the retention time of anaerobic biological treatment is designed to be 5d, so that macromolecular organic matters in the wastewater can be removed, the retention time is continuously increased, the COD removal effect is not obviously changed, the sludge in the reactor is decomposed, and the phenomenon of emulsified oil aggregation is easily caused; the anaerobic treatment adopts a parallel and serial operation mode, so that the flexibility is enhanced, and the capability of coping with the impact of the change of water quality and water quantity can be improved.
In one embodiment, as shown in fig. 2, in the multi-stage a/O and sink tank processing S9, each stage is first subjected to a/O processing S91, and then subjected to sink tank processing S92; wherein the A/O treatment S91 comprises a front anoxic section A and a rear aerobic section O which are connected in series.
The working principle and the beneficial effects of the technical scheme are as follows: A/O is an abbreviation for antioxidant/Oxic, i.e., Anoxic/Oxic; the multi-stage A/O and sedimentation tank treatment is at least two-stage, the multi-stage A/O process is mainly based on the unsteady state theory, the characteristics of various strains (aerobic bacteria, facultative bacteria, anaerobic bacteria and the like) in the system are utilized, the strains are alternately in a 'rich nutrition-poor nutrition' state by periodically controlling the oxygen deficiency and the aerobic bacteria, so that various strains play respective roles in different stages, pollutants are excessively removed, and finally the sewage treatment reaches the standard. The multi-stage A/O process is widely applied to the field of pollutant removal, and can effectively perform nitrogen and phosphorus removal and the like. At present, the research at home and abroad aiming at the multi-stage A/O process is mainly to utilize the staged water inflow unsteady state theory to enhance the removal of pollutants. A sectional water inlet pipeline is reserved in the project scheme, the water inlet load is divided into 2 equal parts, and the 2 equal parts enter each stage of anoxic zones respectively to form a sectional water inlet A/O process. Compared with a single-stage A/O process, the segmented water inlet two-stage A/O process can reduce the influence of metabolites accumulated by the first stage A/O on subsequent biochemical treatment through dilution; on the other hand, the method can provide a carbon source for the second-stage A/O section reaction, make up for the defect of insufficient carbon source of a subsequent biochemical system caused by the consumption of a large amount of organic matters in the first-stage A/O, and improve the removal capacity of pollutants. The heterotrophic bacteria hydrolyze starch, fiber, carbohydrate and other suspended pollutants and soluble organic matters in the sewage into organic acid at the anoxic section, so that macromolecular organic matters are decomposed into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, and when products obtained through anoxic hydrolysis enter an aerobic tank for aerobic treatment, the biodegradability of the sewage is improved, and the oxygen efficiency is improved.
In one embodiment, the activated sludge process of hydrolytic acidification treatment adopts a sludge reflux form treated by a last-stage sedimentation tank to supplement sludge; the front-stage anoxic section A in the A/O treatment S91 adopts a biological filler form; the sludge in each stage of A/O treatment is supplemented from the same stage of sedimentation tank.
The working principle and the beneficial effects of the technical scheme are as follows: according to the scheme, the activated sludge method can prevent oil-in-oil sludge from being formed during hydrolytic acidification treatment, accelerate sludge proliferation and ensure normal metabolism, so that the sewage treatment effect is ensured; the section A in the section A/O adopts a biological filler form, sludge is supplemented from the sedimentation tank, the biological membrane is continuously updated, the consumption of organic matters is compensated, the defect of insufficient carbon source of a subsequent biochemical system is prevented, and the removal energy of pollutants is improved.
In one embodiment, the oil stain separated by the three-stage oil separation treatment is conveyed to an oil phase collecting tank for temporary storage, and the oil phase collecting tank is periodically subjected to oil phase recovery or incineration; the sludge discharged after the treatment of the A/O and sedimentation tank enters a first sludge concentration tank; and the sludge discharged by the first sludge concentration tank, the air floatation machine treatment and the comprehensive air floatation machine treatment enters a second sludge concentration tank.
The working principle and the beneficial effects of the technical scheme are as follows: according to the scheme, the separated oil stains are conveyed to the oil phase collecting tank to be temporarily stored, and the oil phase is periodically recovered or incinerated in the oil phase collecting tank, so that secondary pollution caused by improper treatment of the oil engine can be avoided; the sludge in the sedimentation tank enters a sludge concentration tank for concentration, so that the sludge discharge amount can be reduced, and the treatment capacity is improved.
In one embodiment, as shown in fig. 3 and 4, the integrated air-floating machine processes a central rotating wheel 1 in the integrated air-floating machine, a plurality of vanes 2 are uniformly arranged on the outer cylindrical side surface of the central rotating wheel 1 in the circumferential direction, and the vane surfaces of the vanes 2 are parallel to the axial direction of the central rotating wheel 1;
the vanes 2 are provided with a first adjusting part 3 and a second adjusting part 4, the first adjusting part 3 and the second adjusting part 4 are positioned at the positions of the vanes 2 far away from the central runner 1, and the first adjusting part 3 is used for influencing the stirring function; the second regulating part 4 is used for influencing the bubble function;
the vane 2 is further provided with a third adjusting part 5 and a fourth adjusting part 6, and the third adjusting part 5 and the fourth adjusting part 6 are respectively arranged at the first adjusting part 3 and the second adjusting part 4; the third regulating part 5 is used for increasing the amount of generated bubbles; the fourth adjustment part 6 is used for reducing the load;
the third adjusting part 5 comprises a plurality of through holes, the through holes are regular polygons or circles, and the through holes are arranged in staggered manner at intervals in a longitudinal and transverse direction;
the fourth adjusting part 6 comprises a long through hole and a hinge, the size of the long through hole along the radial direction of the central rotating wheel is larger than that of the long through hole along the parallel direction of the central rotating wheel shaft, the size of the hinge is not smaller than that of the long through hole, the hinge is hinged with the edge of the long through hole, and the hinge can cover and shield the long through hole when the hinge deflects to be parallel to the wheel blade.
The working principle and the beneficial effects of the technical scheme are as follows: according to the scheme, the central rotating wheel is arranged in the comprehensive air flotation machine adopted in the treatment of the comprehensive air flotation machine, the central rotating wheel is driven to rotate through a power mechanism, the waste water is stirred by the wheel blades connected with the central rotating wheel, and the design structure of the wheel blades is combined, so that on one hand, the bubble generation efficiency is improved, and the air flotation separation is accelerated; on the other hand, the rotating speed is controlled to influence the hinge deflection angle, so that the load is reduced, and the energy consumption is saved.
In one embodiment, a temperature adjusting device is arranged in the EGSB anaerobic reactor treatment for temperature control, the temperature adjusting device comprises a temperature detection module, a heat exchange module, a heat source module, a conveying module and a main control module, and the heat exchange module is connected with the heat source module through the conveying module;
the temperature detection module is used for detecting the temperature of the EGSB anaerobic reactor during treatment;
the heat exchange module is used for exchanging heat with wastewater during the treatment of the EGSB anaerobic reactor;
the heat source module is provided with a heat source valve and is used for generating heat;
the conveying module comprises a medium, a medium pipeline and a circulating pump; the medium pipeline is respectively connected with the heat exchange module and the heat source module, and the medium is driven by the circulating pump to circularly flow in the medium pipeline;
the main control module is respectively electrically connected with the temperature detection module, the heat source valve and the circulating pump, and heat is conveyed to the heat exchange module to exchange heat with wastewater according to the treatment requirement of the EGSB anaerobic reactor.
The working principle and the beneficial effects of the technical scheme are as follows: according to the scheme, the temperature adjusting device is arranged in the treatment of the EGSB anaerobic reactor for temperature control, so that the temperature in the treatment process of the EGSB anaerobic reactor is more suitable for anaerobic reaction, the reaction speed is accelerated, and the treatment efficiency is improved; the suitability for temperature control during reaction can also enhance the treatment effect; the cold source module can be connected with the heat source module in parallel through a medium pipeline, the cold source module is provided with a cold source valve, the cold source valve is connected with the main control module, and the cold source module and the cold source valve are opened when necessary to generate cold energy so as to prevent the process from being too high in temperature rise and exceeding the process temperature requirement.
In one embodiment, the heat source module comprises a solar heat collector, a heat storage pool and an electric heater, the solar heat collector is connected with the heat storage pool through a heat medium pipeline, the electric heater is arranged in the heat storage pool, and the electric heater is electrically connected with the main control module; the heat storage tank is connected with a heat source valve and a medium pipeline.
The working principle and the beneficial effects of the technical scheme are as follows: this scheme is through setting up solar thermal collector, heat-retaining pond and electric heater in the heat source module, when solar energy is sufficient, can make full use of solar energy, with the electric energy replenishment when solar energy is not enough, can reduce power consumption, increase the feature of environmental protection.
In one embodiment, the adding amount of the polyacrylamide is calculated and controlled by the following formula when the integrated air flotation machine is used for treatment:
in the above formula, Q represents the addition amount of polyacrylamide; k represents the set addition ratio of the polyacrylamide to the wastewater; q represents the weight of the wastewater treated by the comprehensive air flotation machine; e represents a natural constant; t is1Represents the temperature of the wastewater in kelvin; t is2Representing ambient temperature in kelvin.
The working principle and the beneficial effects of the technical scheme are as follows: the scheme can realize the accurate control of the adding amount of the polyacrylamide by the formula, the formula reflects the influence of the balance of the wastewater temperature and the environmental temperature on the air floatation treatment, the influence is adjusted by adjusting the adding amount of the polyacrylamide, the consistency of the wastewater treatment effect in the treatment process can be ensured,the fluctuation of the wastewater treatment effect is prevented, the subsequent treatment is not facilitated, and the final discharge is ensured to reach the standard; wherein the set addition ratio of polyacrylamide to the wastewater represented by k means a ratio at which the temperature of the wastewater coincides with the ambient temperature, i.e., when the temperature of the wastewater is equal to the ambient temperature (i.e., T1-T20), then Q is kq, and the addition amount only needs to be controlled according to the set addition ratio; the amount of the additive can be finely adjusted only when the temperature of the waste water is not equal to the ambient temperature.
Taking a certain factory project as an example, the flow is shown in fig. 5, the oily wastewater treatment capacity designed by the project is 150 t/day, and the effective volume of the three-stage oil separation collecting tank is 630 cubic meters; the effective volume of the low-concentration wastewater collecting tank is 300 cubic meters; the effective volume of the biochemical regulating tank is 600 cubic meters, and the biochemical regulating tank is divided into two grids which are alternately used; the effective volume of the hydrolysis acidification tank is 800 cubic meters; the effective volume of the anaerobic distribution tank is 160 cubic meters; the effective volume of the EGSB anaerobic reactor is 3000 cubic meters; the effective volume of the first-level A/O and the second-level A/O is 3000 cubic meters; the effective volume of the discharge pool is 200 cubic meters; wherein, the hydrolysis acidification process adopts an activated sludge method, organism fillers are not arranged in the tank body, and a primary sedimentation tank is arranged at the water outlet end of the hydrolysis acidification tank; the anaerobic treatment adopts a parallel and serial running mode to flexibly cope with the change impact of water quality and water quantity, the retention time of anaerobic biological treatment is designed to be 5d, the removal of macromolecular organic matters in the wastewater can be realized, the retention time is continuously increased, the COD removal effect has no obvious change, the sludge in the reactor is decomposed, and the phenomenon of emulsified oil aggregation is easily caused; treating by adopting two stages of A/O and sedimentation tanks, namely a first stage A/O, a primary sedimentation tank, a second stage A/O and a secondary sedimentation tank, wherein the section A in the section A/O adopts a biological filler form, mud is supplemented from the sedimentation tank, and a biological film is continuously updated; the method realizes removal of pollutants by utilizing the life activities of microorganisms in an anoxic-aerobic alternative environment, has the advantages of flexible operation and strong impact load resistance, and can maintain normal operation when the inlet water quality is greatly fluctuated or the pollutant concentration is high. The A-section anoxic contact operation is suitable for pretreatment of sewage with COD higher than 4000mg/L in anaerobic effluent, suspended pollutants and soluble organic matters in the sewage are hydrolyzed into organic acid by heterotrophic bacteria in the anoxic section, so that macromolecular organic matters are decomposed into micromolecular organic matters, and insoluble organic matters are converted into soluble organic matters. The hydrolysate remained in the water discharged from the section A is further biodegraded by aerobic sludge in the section O. In addition, certain substances are more susceptible to degradation under anoxic conditions than under aerobic conditions (such as azithromycin). The first-level section A can better adapt to high-load impact from anaerobic effluent, has good degradation effect on partial organic matters in the anaerobic effluent, and greatly reduces load impact on the section O. From the field test of the plant area, it can be known that according to a certain batch of experimental data of the plant area shown in the following table, the total removal amount of the organic matters by the primary O section (HRT2d) is basically stabilized at 1200-1500mg/L, no obvious organic matter degradation trend is continuously prolonged, the secondary A section is added, soluble organic matters and suspended organic matters can be further treated, the biodegradability of wastewater is provided, and the treatment of the secondary O section is facilitated. The A/O process is mainly based on an unsteady state theory, utilizes the characteristics of various strains (aerobic bacteria, facultative bacteria, anaerobic bacteria and other strains) in the system, and alternately stays in a 'eutrophic-poor nutrition' state by periodically controlling the oxygen deficiency and the aerobic bacteria, so that various strains play respective roles in different stages, pollutants are excessively removed, and finally the sewage treatment reaches the standard. The multi-stage A/O process is widely applied to the field of pollutant removal, and can effectively perform nitrogen and phosphorus removal and the like. At present, the research at home and abroad aiming at the multi-stage A/O process is mainly to utilize the staged water inflow unsteady state theory to enhance the removal of pollutants. A sectional water inlet pipeline is reserved in the project scheme, the water inlet load is divided into 2 equal parts, and the 2 equal parts enter each stage of anoxic zones respectively to form a sectional water inlet A/O process. Compared with a single-stage A/O process, the segmented water inlet two-stage A/O process can reduce the influence of metabolites accumulated by the first stage A/O on subsequent biochemical treatment through dilution; on the other hand, the method can provide a carbon source for the second-stage A/O section reaction, make up for the defect of insufficient carbon source of a subsequent biochemical system caused by the consumption of a large amount of organic matters in the first-stage A/O, and improve the removal capacity of pollutants.
The overlong hydraulic retention time can increase the investment and the operation cost, and simultaneously, the sludge age is easily over-long, and the sludge is aged due to over-oxidation, so that the operation of a sewage station is influenced, and the effluent stably reaches the standard. Under the condition of longer retention time, the content of biochemically degradable organic matters in the effluent of the first-stage A/O is low, and the B/C ratio of the effluent is lower, so that the second-stage A/O is difficult to achieve the expected treatment effect, the activity of microorganisms can be maintained by stage water inflow, and the additional operation cost (such as additional nutrient source) is not increased. Therefore, the hydraulic retention time in each stage of A/O process is set to be 2d +2d aiming at the design scale of the comprehensive sewage station 800t/d in the newly built plant area.
The plug flow and aeration functions are synchronously considered when the tank A is designed, so that the function of the biochemical tank can be flexibly adjusted by combining the water quality condition during later operation. When the biochemical aeration fan is selected, a plurality of fans are arranged by comprehensively considering each running state, and frequency conversion is matched so as to be suitable for each working condition of biochemical pool body function adjustment. On the arrangement of the aerators, the number, the spacing and other layouts of the aerators are adjusted by combining the oxygen demand of each unit, so that the effect of high front and low back of dissolved oxygen in the aerobic tank is achieved, and the influence of the backflow of the cell sap at the tail end on the microbial environment of the front-end tank A is reduced. The experimental data of a certain batch of the plant area are as follows:
data of a lot of experiments in a certain factory
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. A method for treating perfume oil-containing wastewater by an activated sludge-biofilm symbiotic system is characterized by sequentially carrying out the following steps on the process oil-containing wastewater:
the method comprises the following steps of three-stage oil separation treatment, air floatation machine treatment, biochemical regulating tank treatment, comprehensive air floatation machine treatment, hydrolytic acidification treatment, primary sedimentation tank treatment, anaerobic distribution tank treatment, EGSB anaerobic reactor treatment, multi-stage A/O and sedimentation tank treatment and mixed sedimentation treatment, wherein the mixed sedimentation treatment is carried out and then the mixture sedimentation treatment enters a discharge tank for discharge;
the domestic oily wastewater passes through a low-concentration wastewater tank, then goes through three-stage oil separation treatment and air flotation machine treatment, and directly enters a biochemical regulating tank for treatment;
wherein, the hydrolytic acidification treatment adopts an activated sludge method, and organism fillers are not arranged in a tank body of the hydrolytic acidification treatment.
2. The method for treating the perfume oily wastewater by using the activated sludge-biofilm symbiotic system according to claim 1, wherein polyacrylamide and polyaluminium chloride are added in the air flotation machine treatment and the comprehensive air flotation machine treatment, or polyacrylamide and alkali are added;
and adding activated carbon and polyaluminium chloride or activated carbon and polyacrylamide in the mixing and precipitating treatment.
3. The method for treating the aromatic oily wastewater by the activated sludge-biofilm symbiotic system according to claim 1, wherein the treatment residence time of the anaerobic distribution tank is designed to be 5 days, and the anaerobic treatment adopts a parallel-series operation mode.
4. The method for treating the aromatic oily wastewater by the activated sludge-biofilm symbiotic system according to claim 1, wherein in the multistage A/O and sedimentation tank treatment, the A/O treatment is firstly carried out on each stage, and then the sedimentation tank treatment is carried out; wherein the A/O treatment comprises a front-section anoxic section A and a rear-section aerobic section O which are connected in series.
5. The method for treating the aromatic oily wastewater by the activated sludge-biofilm symbiotic system according to claim 1, wherein the activated sludge process of hydrolytic acidification treatment adopts a sludge reflux form of last-stage sedimentation tank treatment to supplement sludge.
6. The method for treating the perfume-containing wastewater by the activated sludge-biofilm symbiotic system according to claim 4, wherein the front-stage anoxic section A in the A/O treatment is in the form of biological filler; the sludge in each stage of A/O treatment is supplemented from the same stage of sedimentation tank.
7. The method for treating the perfume oily wastewater by using the activated sludge-biofilm symbiotic system according to claim 1, wherein the oil stains separated by the three-stage oil separation treatment are conveyed to an oil phase collecting tank for temporary storage, and the oil phase collecting tank is periodically subjected to oil phase recovery or incineration; the sludge discharged after the treatment of the A/O and sedimentation tank enters a first sludge concentration tank; and the sludge discharged by the first sludge concentration tank, the air floatation machine treatment and the comprehensive air floatation machine treatment enters a second sludge concentration tank.
8. The method for treating the perfume oily wastewater by the activated sludge-biofilm symbiotic system according to claim 1, wherein the comprehensive air flotation machine is used for treating a central rotating wheel in the comprehensive air flotation machine, a plurality of blades are uniformly arranged on the outer cylindrical side surface of the central rotating wheel in the circumferential direction, and the blade surfaces of the blades are parallel to the axial direction of the central rotating wheel;
the vanes are provided with a first adjusting part and a second adjusting part, the first adjusting part and the second adjusting part are positioned at positions of the vanes far away from the central rotating wheel, and the first adjusting part is used for influencing the stirring function; the second adjusting part is used for influencing the bubble function;
the vane is also provided with a third adjusting part and a fourth adjusting part which are respectively arranged at the first adjusting part and the second adjusting part; the third regulating part is used for increasing the generation amount of bubbles; the fourth adjusting part is used for reducing load;
the third adjusting part comprises a plurality of through holes, the through holes are regular polygons or circles, and the through holes are arranged in staggered manner at intervals in a longitudinal and transverse direction;
the fourth adjusting part comprises a long through hole and a hinge, the size of the long through hole along the radial direction of the central rotating wheel is larger than the size of the long through hole along the parallel direction of the central rotating wheel shaft, the size of the hinge is not smaller than that of the long through hole, the hinge is hinged with the edge of the long through hole, and the hinge can cover and shield the long through hole when the hinge deflects to be parallel to the wheel blade.
9. The method for treating the aromatic oily wastewater by using the activated sludge-biofilm symbiotic system according to claim 1, wherein a temperature regulating device is arranged in the EGSB anaerobic reactor for temperature control, the temperature regulating device comprises a temperature detection module, a heat exchange module, a heat source module, a conveying module and a main control module, and the heat exchange module is connected with the heat source module through the conveying module;
the temperature detection module is used for detecting the temperature of the EGSB anaerobic reactor during treatment;
the heat exchange module is used for exchanging heat with wastewater during the treatment of the EGSB anaerobic reactor;
the heat source module is provided with a heat source valve and is used for generating heat;
the conveying module comprises a medium, a medium pipeline and a circulating pump; the medium pipeline is respectively connected with the heat exchange module and the heat source module, and the medium is driven by the circulating pump to circularly flow in the medium pipeline;
the main control module is respectively electrically connected with the temperature detection module, the heat source valve and the circulating pump, and heat is conveyed to the heat exchange module to exchange heat with wastewater according to the treatment requirement of the EGSB anaerobic reactor.
10. The method for treating the aromatic oily wastewater by the activated sludge-biofilm symbiotic system according to claim 9, wherein the heat source module comprises a solar heat collector, a heat storage tank and an electric heater, the solar heat collector is connected with the heat storage tank through a heat medium pipeline, the electric heater is arranged in the heat storage tank, and the electric heater is electrically connected with the main control module; the heat storage tank is connected with a heat source valve and a medium pipeline.
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