CN114084955A - Response surface method-based method for optimizing denitrification performance of anaerobic ammonia oxidation membrane bioreactor and denitrification method - Google Patents
Response surface method-based method for optimizing denitrification performance of anaerobic ammonia oxidation membrane bioreactor and denitrification method Download PDFInfo
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
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- C02F2101/16—Nitrogen compounds, e.g. ammonia
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Abstract
The invention belongs to the technical field of sewage treatment, and particularly relates to a method for optimizing denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method and a denitrification method. According to the invention, the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor is optimized by adopting the response curved surface method, the problem that the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor is influenced by the combined action of three factors, namely the inorganic carbon source concentration of sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor in actual engineering is solved, and more reasonable denitrification parameters can be quickly and effectively determined in actual engineering application, so that the anaerobic ammonia oxidation membrane bioreactor has high total nitrogen removal rate of sewage.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a method for optimizing denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method and a denitrification method.
Background
A Membrane Bioreactor (MBR) process is a novel high-efficiency sewage treatment technology organically combining a high-efficiency separation technology and traditional activated sludge biological treatment, and is concerned in the fields of various municipal sewage reclaimed water reuse, biological nitrogen and phosphorus removal, low carbon-nitrogen ratio municipal sewage, high-concentration ammonia nitrogen organic wastewater treatment and the like in recent years. Compared with the traditional nitrification and denitrification biological nitrogen removal method, in the MBR process, the biological membrane is used as a carrier for the attachment and growth of microorganisms, can intercept substances such as activated sludge, suspended matters and the like in a biochemical reaction tank, and has the characteristics of good effluent quality, compact system, high pollutant degradation rate and the like.
At present, membrane components in the MBR process mostly adopt hollow fiber membranes, composite membranes, flat membranes and the like, wherein the hollow fiber membranes are widely used as the main components. MBR-based denitrification processes are also constantly being updated, anaerobic ammonia oxidation (Anammox), short-cut denitrification, and,A series of processes such as synchronous nitrification and denitrification, aerobic denitrification and the like are in the future. Wherein the Anammox process can realize NH under the action of anaerobic ammonium oxidation bacteria in an anaerobic environment4 +-N and NO2 -Redox reaction of N to N2Thereby achieving nitrogen removal. The Anammox process has the characteristics of autotrophic nitrogen removal, no aerobic and external carbon source, 60% saving of aeration amount compared with the traditional nitrogen removal process, low sludge yield and the like. Compared with a Sequencing Batch Reactor (SBR) process, the starting time of the MBR process is shorter, higher nitrogen removal efficiency can be obtained, and the Anammox-MBR can quickly enrich and retain complete biomass of anaerobic ammonia oxidation microorganisms growing slowly, so that more uniform substrate and biomass distribution is realized, the activity of anaerobic activated sludge is maintained, and the problem of activity reduction of the anaerobic activated sludge in the Anammox process is ingeniously solved.
However, in the actual operation process of the Anammox-MBR process, the Anammox bacteria have the problems of long culture doubling time, strict requirements on growth environment, and susceptibility to the influence of conditions such as temperature, inorganic carbon source concentration and Hydraulic Retention Time (HRT) in the denitrification process, so that the efficiency of Anammox denitrification is reduced, and the large-scale application of the Anammox bacteria in urban sewage treatment is limited.
Disclosure of Invention
In view of the above, the invention aims to provide a method for optimizing the denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method and a denitrification method.
In order to achieve the purpose, the invention provides the following technical scheme:
the invention provides a method for optimizing denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method, which comprises the following steps:
adopting a single factor variable method to obtain each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor corresponding to the condition that the total nitrogen removal rate of the sewage is more than or equal to 80 percent; the single factors comprise the concentration of an inorganic carbon source of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor;
and (3) carrying out a response surface optimization test by taking the single factor values as independent variables and the total nitrogen removal rate of the sewage as response values, and carrying out multiple regression fitting on the data of the obtained multiple groups of response surface optimization tests to obtain a regression equation of the total nitrogen removal rate of the sewage:
and respectively solving a first-order partial derivative of the temperature of the membrane bioreactor, the concentration of the inorganic carbon source of the sewage and the hydraulic retention time of the membrane bioreactor through the regression equation to obtain a ternary linear equation set, and solving the equation set to obtain the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment.
Preferably, in the single-factor variable method, the concentration of the inorganic carbon source in the sewage ranges from 0.5mg/L to 1.5mg/L, the temperature of the anaerobic ammonia oxidation membrane bioreactor ranges from 30 ℃ to 36 ℃, and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor ranges from 8h to 12 h.
Preferably, the values of the independent variables are end values and middle values of the value ranges of the single factors.
Preferably, the Design of the response surface optimization experiment and the multiple regression fitting are carried out by Design Expert 8.0.6 software.
Preferably, the concentration of the inorganic carbon source in the sewage in the denitrification parameters is 0.85-0.95 mg/L, the temperature of the anaerobic ammonia oxidation membrane bioreactor is 33.5-36 ℃, and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor is 9.95-10.07 h.
Preferably, the membrane component of the anaerobic ammonia oxidation membrane bioreactor is a hollow fiber membrane; the hollow fiber membrane is made of polyvinylidene fluoride with a lining.
Preferably, the filtration precision of the hollow fiber membrane is 0.1 μm; the inner diameter of the membrane filaments of the hollow fiber membrane is 1.2 mu m; the outer diameter of the membrane filaments of the hollow fiber membrane is 2.2 mu m.
Preferably, the hollow fiber membrane has an effective membrane area of 0.06m2。
Preferably, the hollow fiber membrane is pretreated before use, and the pretreatment comprises the following steps: immersing the hollow fiber membrane in an ethanol solution, and sequentially standing, washing and thermally treating.
The invention also provides a denitrification method based on the anaerobic ammonia oxidation membrane bioreactor, which comprises the following steps: according to the technical scheme, the denitrification parameter is obtained by the method for optimizing the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor based on the response surface method, and sewage is introduced into the anaerobic ammonia oxidation membrane bioreactor for denitrification treatment according to the obtained denitrification parameter.
The invention provides a method for optimizing denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method, which comprises the following steps: adopting a single factor variable method to obtain each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor corresponding to the condition that the total nitrogen removal rate of the sewage is more than or equal to 80 percent; the single factors comprise the concentration of an inorganic carbon source of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor; and (3) carrying out a response surface optimization test by taking the single factor values as independent variables and the total nitrogen removal rate of the sewage as response values, and carrying out multiple regression fitting on the data of the obtained multiple groups of response surface optimization tests to obtain a regression equation of the total nitrogen removal rate of the sewage: and respectively solving a first-order partial derivative of the temperature of the membrane bioreactor, the concentration of the inorganic carbon source of the sewage and the hydraulic retention time of the membrane bioreactor through the regression equation to obtain a ternary linear equation set, and solving the equation set to obtain the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment.
The invention optimizes the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor by adopting a response curved surface method, simultaneously analyzes the processed data by adopting multiple regression fitting, displays the functional relation between the response value (total nitrogen removal rate) and the independent variable (temperature, inorganic carbon source concentration and hydraulic retention time) by establishing a regression equation by using a reasonable test method, and helps to visually observe and select the optimal denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor by the relation between the response value and the independent variable under the combined interaction, thereby solving the problem that the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor is influenced by the combined action of three factors of the inorganic carbon source concentration of sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor in the actual engineering, and being capable of being quickly, quickly and quickly applied in the actual engineering, And more reasonable denitrification parameters are effectively determined, so that the anaerobic ammonia oxidation membrane bioreactor has high total nitrogen removal rate of sewage.
The denitrification performance of the anaerobic ammonia oxidation membrane bioreactor is optimized by adopting the response surface method, compared with the traditional full factor test, the continuous multiple tests are not needed, and under the condition of the same factor number, the experimental combination of the response surface method is less than that of the full factor test design, so that the method is more economic and rapid.
The method for optimizing the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor based on the response curved surface method has the advantages of high implementation reliability, popular and easy understanding, simple operation and contribution to popularization and application of the process parameter regulation and control process of the anaerobic ammonia oxidation bioreactor of the actual sewage treatment plant.
Drawings
FIG. 1 is a schematic diagram of an anaerobic ammonia oxidation membrane bioreactor apparatus according to the present invention;
FIG. 2 is a flow chart of a method of modeling a response surface;
FIG. 3 is a response surface graph of the influence of inorganic carbon source concentration and temperature on the total nitrogen removal rate of wastewater;
FIG. 4 is a response surface plot of hydraulic retention time and inorganic carbon source concentration effects on total nitrogen removal from wastewater;
FIG. 5 is a graph of the response curve of hydraulic retention time and temperature effect on total nitrogen removal from wastewater;
FIG. 6 is a graph of the change in membrane flux of the system over the entire phase of response surface optimization;
FIG. 7 is a thermogravimetric curve test result plot for hollow fiber membranes before and after response surface optimization;
FIG. 8 is a graph of results of infrared analysis testing of hollow fiber membranes before and after response surface optimization;
FIG. 9 is a comparison graph of infrared analysis of hollow fiber membranes before and after response surface optimization;
FIG. 10 is a three-dimensional AFM surface topography of PVDF hollow fiber membranes before and after response surface optimization: wherein (a) is before optimization and (b) is after optimization.
Detailed Description
The invention provides a method for optimizing denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method, which comprises the following steps:
adopting a single factor variable method to obtain each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor corresponding to the condition that the total nitrogen removal rate of the sewage is more than or equal to 80 percent; the single factors comprise the concentration of an inorganic carbon source of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor;
and (3) carrying out a response surface optimization test by taking the single factor values as independent variables and the total nitrogen removal rate of the sewage as response values, and carrying out multiple regression fitting on the data of the obtained multiple groups of response surface optimization tests to obtain a regression equation of the total nitrogen removal rate of the sewage:
and respectively solving a first-order partial derivative of the temperature of the membrane bioreactor, the concentration of the inorganic carbon source of the sewage and the hydraulic retention time of the membrane bioreactor through the regression equation to obtain a ternary linear equation set, and solving the equation set to obtain the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment.
The single factor variable method is adopted to obtain each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor corresponding to the condition that the total nitrogen removal rate of the sewage is more than or equal to 80 percent; the single factors comprise the concentration of the inorganic carbon source of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor.
In the invention, the structure of the anaerobic ammonia oxidation membrane bioreactor is shown in figure 1. The anaerobic ammonia oxidation membrane bioreactor comprises a water inlet and a water outletThe device comprises a port, a membrane component, a water bath heating layer, a water bath heating box, a heating rod, a water bath heating pump, an exhaust port, a DO/pH detector, a DO/pH probe and a PLC (programmable logic controller); the membrane module of the membrane bioreactor is preferably a hollow fiber membrane; the hollow fiber membrane is preferably made of polyvinylidene fluoride (PVDF) with a lining; the filtration precision of the hollow fiber membrane is preferably 0.1 μm; the inner diameter of the membrane filaments of the hollow fiber membrane is preferably 1.2 mu m; the outer diameter of the membrane filaments of the hollow fiber membrane is preferably 2.2 μm; the effective membrane area of the hollow fiber membrane is preferably 0.06m2。
In the present invention, the hollow fiber membrane is preferably subjected to a pretreatment before use, and the pretreatment preferably includes the steps of: immersing the hollow fiber membrane in an absolute ethyl alcohol solution with the volume fraction of 50%, standing for 5-6 h, then washing the vacuum fiber membrane with deionized water, soaking the obtained membrane in the deionized water for 4h, and then carrying out heat treatment in a vacuum drying oven for 5 h; the temperature of the heat treatment is preferably 100-110 ℃, and more preferably 105 ℃. The PVDF hollow fiber membrane is inevitably polluted by foreign matters in the production, manufacture and transportation processes, and is soaked in moisturizing substances such as glycerin in the storage process, so that the PVDF hollow fiber membrane is pretreated in order to prevent the membrane from becoming brittle due to long-term exposure to air.
In the invention, before the sewage enters the anaerobic ammonia oxidation membrane bioreactor, the anaerobic ammonia oxidation membrane bioreactor is preferably started by anaerobic ammonia oxidation sludge; the starting method of the anaerobic ammonia oxidation sludge preferably comprises the following steps: inoculating sludge with anaerobic ammonia oxidation activity in the anaerobic ammonia oxidation membrane bioreactor to ensure that the suspended solid concentration of mixed liquor in the inoculated anaerobic ammonia oxidation membrane bioreactor is 2300mg/L, and gradually increasing NH (ammonia) of inlet water4+-N and NO2The concentration of N and the mode of reducing the hydraulic retention time acclimatize the anaerobic ammonia oxidation sludge, and start the anaerobic ammonia oxidation membrane bioreactor. The volume and concentration of the inoculated sludge with anammox activity are not particularly limited, and can be selected according to actual conditions. In the present example, the inoculated cells were anaerobically inoculatedSpecifically, the volume of the sludge having ammoxidation activity was 500mL, and the concentration of the seeded sludge having anaerobic ammoxidation activity was 2300 mg/L.
Before the anaerobic ammonia oxidation membrane bioreactor is started, black sponge blocks are preferably filled in the anaerobic ammonia oxidation membrane bioreactor to serve as carriers, a black plastic bag is used for wrapping the anaerobic ammonia oxidation membrane bioreactor, and concentrated sulfuric acid with the mass fraction of 5% is used for adjusting the pH of the anaerobic ammonia oxidation membrane bioreactor to 7.0-7.6. The black sponge block of the invention has no special limitation on the size, and the black sponge block with the size known in the field can be adopted. In the embodiment of the invention, the size of the black sponge block is specifically 2cm × 2cm × 2 cm.
In the invention, NH of the anaerobic ammonia oxidation membrane bioreactor4 +The removal rate of-N is preferably>95％，NO2 -The removal rate of-N is preferably>95 percent, the TN removal rate is preferred>80%, the total nitrogen removal load is preferably not less than 0.33 kg/(m)3D), the anaerobic ammonia oxidation membrane bioreactor is successfully started.
In the invention, a single factor variable method is adopted, and the process of obtaining each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor when the total nitrogen removal rate of the sewage is more than or equal to 80 percent preferably comprises the following steps: and sequentially changing the temperature of the membrane bioreactor, the concentration of the inorganic carbon source of the sewage and the hydraulic retention time of the membrane bioreactor to carry out a single-factor variable screening experiment, and analyzing the experiment result to obtain each single-factor value of the corresponding denitrification process when the total nitrogen removal rate of the sewage of the anaerobic ammonia oxidation membrane bioreactor is more than or equal to 80%.
In the single-factor variable method, the value range of the inorganic carbon source concentration of the sewage is preferably 0.5-1.5 mg/L, and in the embodiment of the invention, the inorganic carbon source concentration of the sewage is 0.5mg/L, 1.0mg/L and 1.5 mg/L; the temperature of the membrane bioreactor preferably ranges from 30 ℃ to 36 ℃, and in the embodiment of the invention, the temperature of the membrane bioreactor is 30 ℃, 33 ℃ and 36 ℃; the value range of the hydraulic retention time of the membrane bioreactor is preferably 8-12 h, and in the embodiment of the invention, the hydraulic retention time of the membrane bioreactor is 8h, 10h and 12 h.
After obtaining each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor corresponding to the condition that the total nitrogen removal rate of the sewage is more than or equal to 80 percent, carrying out a response curved surface optimization test by taking each single factor value as an independent variable and the total nitrogen removal rate of the sewage as a response value, and carrying out multiple regression fitting on the data of the obtained multiple groups of response curved surface optimization tests to obtain a regression equation of the total nitrogen removal rate of the sewage;
in the embodiment of the invention, the total nitrogen removal rate of the sewage is YAThe regression equation of (a) is shown in formula I: y isA＝80.30+9.38A-1.91B+2.28C-4.06AB-2.92AC-3.97BC-0.97A2-15.32B2-11.34C2
Formula I;
in the formula I, YAThe total nitrogen removal rate of the sewage is shown as A, the temperature of the membrane bioreactor is shown as B, the concentration of the inorganic carbon source of the sewage is shown as B, and the hydraulic retention time of the membrane bioreactor is shown as C.
In the invention, the Design and the multiple regression fitting of the response surface optimization test are preferably carried out by Design Expert 8.0.6 software; the response surface optimization test is preferably a three-factor three-level response surface optimization test. In the present invention, the value of the independent variable is preferably an end point value and a middle value of a value range of each single factor.
In the invention, according to the design principle of a response surface, the temperature of the membrane bioreactor, the concentration of an inorganic carbon source of sewage and the hydraulic retention time of the membrane bioreactor are selected as independent variables on the basis of a single-factor experiment, the total nitrogen removal rate of the sewage is a response value, and a three-factor three-level response surface optimization experiment is carried out. In the invention, when response surface optimization is carried out, the end value and the middle value of the value range of each single factor of the corresponding denitrification process are taken as the value of the independent variable when the total nitrogen removal rate of the sewage is more than or equal to 80 percent determined by a single variable method.
After a regression equation of the total nitrogen removal rate of the sewage is obtained, the first-order partial derivatives of the temperature of the membrane bioreactor, the inorganic carbon source concentration of the sewage and the hydraulic retention time of the membrane bioreactor are respectively obtained through the regression equation, a ternary linear equation set is obtained, the equation set is solved to obtain the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment, and the inorganic carbon source concentration of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor corresponding to the maximum value of the total nitrogen removal rate of the sewage are obtained.
In the invention, the concentration of the inorganic carbon source in the sewage in the denitrification parameter is preferably 0.85-0.95 mg/L, and more preferably 0.9 mg/L; the temperature of the anaerobic ammonia oxidation membrane bioreactor is preferably 33.5-36 ℃, and more preferably 36 ℃; the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor is preferably 9.95-10.07 h, and more preferably 10.01 h. The source of the wastewater is not particularly limited in the present invention, and wastewater known in the art may be used.
According to the invention, through response surface analysis, when the concentration of the inorganic carbon source of the sewage is 0.9mg/L, the temperature of the membrane bioreactor is 36 ℃, and the hydraulic retention time of the membrane bioreactor is 10.01h, the total nitrogen removal rate of the sewage reaches the highest, the predicted highest value is 89.29%, and according to the denitrification condition of the actual anaerobic ammonia oxidation membrane bioreactor, the optimal denitrification condition of the anaerobic ammonia oxidation membrane bioreactor is determined to be that the concentration of the inorganic carbon source of the sewage is 0.9mg/L, the temperature of the membrane bioreactor is 36 ℃, and the hydraulic retention time of the membrane bioreactor is 10.01 h. The method is characterized in that 3 times of repeated experiments are carried out under the optimal denitrification optimization condition to verify the reliability of the response curved surface model, the average value of the total nitrogen removal rate of the sewage obtained by the three experiments is 88.98%, the measured value and the theoretical value have good fitting degree, and the optimized denitrification parameters are suitable for the anaerobic ammonia oxidation membrane bioreactor to carry out denitrification treatment on the sewage.
After obtaining the regression equation, the present invention preferably further comprises performing significance analysis and variance analysis on the regression equation, and determining the coefficient R according to the significance P of the model2Correction coefficient R2 AdjAnalysis of the results of the signal-to-noise ratio and the coefficient of variationAccuracy and reliability of the model.
In the invention, the flow of the method for optimizing the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor based on the response surface method is shown in figure 2. The method comprises the steps of obtaining each single factor value of a denitrification process corresponding to the maximum total nitrogen removal rate of the sewage of the anaerobic ammonia oxidation membrane bioreactor through variable selection, starting of the anaerobic ammonia oxidation membrane bioreactor and a single factor experiment, simulating the total nitrogen removal rate of the sewage under the interaction of each single factor by establishing a response surface optimization scheme, optimizing each single factor through multiple regression fitting analysis, significance analysis and variance analysis to obtain the inorganic carbon source concentration of the sewage, the temperature of the membrane bioreactor and the hydraulic retention time of the membrane bioreactor corresponding to the maximum total nitrogen removal rate of the sewage under the interaction of the three factors of the inorganic carbon source concentration of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time, and setting denitrification parameters of the anaerobic ammonia oxidation membrane bioreactor in practical engineering as the inorganic carbon source concentration of the sewage, the concentration of the sewage corresponding to the maximum total nitrogen removal rate of the sewage, Verifying the total nitrogen removal rate of the sewage by the temperature and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor, and determining final denitrification parameters.
The method for optimizing the denitrification parameters of the anaerobic ammonia oxidation membrane bioreactor by using the response surface method solves the influence of the multi-factor combination problem on the total nitrogen removal rate of the sewage of the anaerobic ammonia oxidation membrane bioreactor, and has the characteristics of low experimental cost, short treatment time, rapidness, effectiveness, safety, environmental protection and high total nitrogen removal rate of the sewage, and has certain application and popularization values.
The invention also provides a denitrification method of the anaerobic ammonia oxidation bioreactor, which comprises the following steps: according to the technical scheme, the denitrification parameter is obtained by the method for optimizing the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor based on the response surface method, and sewage is introduced into the anaerobic ammonia oxidation membrane bioreactor for denitrification treatment according to the obtained denitrification parameter.
The PVDF hollow fiber membrane after the response curved surface optimization has poor stability and rough membrane surface, is influenced by certain membrane pollution, needs to make a suitable membrane cleaning scheme, removes dirt on the membrane surface and realizes long-term stable operation of the anaerobic ammonia oxidation membrane bioreactor.
The invention preferably also comprises the step of cleaning the membrane module of the anaerobic ammonia oxidation membrane bioreactor after the denitrification treatment is finished, wherein the cleaning process comprises the following steps:
and (3) draining the solution or liquid substance in the membrane pores of the membrane component of the anaerobic ammonia oxidation membrane bioreactor, pumping ultrapure water into the membrane component reversely for cleaning, and finally, chemically cleaning the membrane component.
In the present invention, the apparatus for draining is preferably a syringe; the equipment for pumping ultrapure water in the reverse direction is preferably a peristaltic pump; the pumping speed of the ultrapure water into the reaction tank is preferably 20 mL/min; the cleaning solution used for the chemical cleaning is preferably 2 wt.% citric acid solution and 0.01mol/L NaOH solution, and the volume ratio of the citric acid solution to the NaOH solution is preferably 1: 1; the pH value of the citric acid solution is preferably 2; the pH of the NaOH solution is preferably 12. In the invention, the ultrapure water is pumped in the reverse direction, so that pollutants in the hollow fiber membrane can be washed loose or separated from the membrane component and enter the solution; along with the extension of the working time of the membrane component, the membrane pollution is aggravated, the transmembrane pressure and the membrane flux are reduced in different degrees, and the membrane component needs to be cleaned chemically at regular intervals.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention.
Example 1
(1) Starting anaerobic ammonia oxidation membrane bioreactor
Starting the anaerobic ammonia oxidation membrane bioreactor by using simulated wastewater: the composition of the test wastewater comprises: NH (NH)4 +-N and NO2 -N is each NH4Cl and NaNO2Adding the mixture in a form with the concentration of 80.40mg/L and 106.13mg/L respectively; other components also include: NaHCO 23 CaCl2·2H2O 0.1g/L，KH2PO4 0.05g/L，MgSO4·7H2O 0.1g/L，Na2SO30.05g/L, 1ml/L microelement liquid; the microelement component is ZnSO4·7H2O 0.43g/L，MnCl2·4H2O 0.99g/L，EDTA 10g/L，CuSO4·5H2O 0.25g/L，NiCl2·6H2O 0.19g/L，CoCl2·6H2O 0.24g/L，NaSeO4·10H2O 0.21g/L，H3BO30.014 g/L. The inorganic carbon source is NaHCO3The concentration of the inorganic carbon source was measured by a multi N/C3100 TOC measuring instrument.
Before starting the anaerobic ammonia oxidation membrane bioreactor, black sponge blocks with the size of 2cm multiplied by 2cm are filled in the anaerobic ammonia oxidation membrane bioreactor to serve as carriers, a black plastic bag is used for wrapping the reactor, concentrated sulfuric acid with the mass fraction of 5% is used for adjusting the pH of the reactor to 7.5, and the temperature in the reactor is controlled to be 34 +/-2 ℃ through water bath heating. 500mL of sludge with anammox activity and the inoculated concentration of 2300mg/L is inoculated in the membrane bioreactor, and the suspended solid concentration of the mixed solution in the anaerobic ammonia oxidation membrane bioreactor after inoculation is 2300 mg/L.
The hollow fiber membrane is made of PVDF material with lining, the filtration precision is 0.1 μm, the inner diameter and the outer diameter of the membrane thread are 1.2 μm and 2.2 μm respectively, and the effective membrane area is 0.06m2. Immersing the hollow fiber membrane in 50% absolute ethyl alcohol solution, standing for 6h, taking out the membrane module after immersion, washing with deionized water, soaking in deionized water for 4h, and then placing in a vacuum drying oven at 105 ℃ for heat treatment for 5 h.
The early stage of starting the anaerobic ammonia oxidation membrane bioreactor is that the NH of inlet water is gradually increased within 60 days4 +-N、NO2 -Concentration of N and reduction of hydraulic retention time to NH4 +-N、NO2 -The removal rates of-N and TN reached 96.22%, 99.91% and 81.66%, respectively, and the total nitrogen removal load (NRR) reached 0.33 kg/(m)3D). After the system is started successfully, on the basis of successful start of the reactor, a single-factor variable experiment is carried out to screen three-factor parameter ranges, and the three-factor parameter ranges are obtained through the single-factor variable experimentThe optimal range of the values of all the factors is used as an experimental basis for response surface optimization, and a corresponding experimental scheme is obtained.
(2) Experiment with single factor variable
And sequentially changing the values of the temperature, the concentration of the inorganic carbon source and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor to carry out a single-factor variable screening experiment, and determining the optimal range of the values of all variables to be 30-36 ℃, 0.5-1.5 mg/L and 8-12 h by analyzing the experiment result.
The response surface optimization is carried out on the basis of the single-factor test, and the reliability of the test is ensured. The schematic diagram of the reactor and the PVDF hollow fiber membrane module are shown in figure 1.
(3) Test item and method
The total nitrogen removal rate of the sewage is an important parameter for representing the treatment capacity of the anaerobic ammonia oxidation strain of the MBR, and is determined by an alkaline potassium persulfate digestion ultraviolet spectrophotometry; the surface characteristics of the hollow fiber membrane before and after response surface optimization are tested by adopting a VEECO atomic force microscope (Bruker dimension icon), morphological parameters such as surface roughness, pore size distribution and the like of the PVDF membrane are obtained, and analysis of the relationship between the surface characteristic behaviors of the hollow fiber membrane before and after response surface optimization is facilitated.
Pretreatment of the membrane material is required before testing for thermogravimetric and infrared spectral properties. The specific operation is as follows: taking out the hollow fiber membrane module, cutting a membrane wire with the length of about 5cm at the middle part of the membrane module, placing the membrane wire in a centrifugal tube for storage, freeze-drying the centrifugal tube filled with the membrane wire for 24 hours, dehydrating the centrifugal tube, cutting the centrifugal tube under the aseptic condition, cutting the centrifugal tube into square blocks with the diameter of about 1mm multiplied by 1mm, grinding and sieving the square blocks, and placing part of samples into a hot-weight crucible for later use; and adding the rest sample into an agate mortar, mixing with KBr, fully grinding and uniformly mixing under an infrared baking lamp, and preparing the infrared sample to be detected through infrared tabletting.
Thermogravimetric analysis was performed using a mettler-toledo TGA2 thermogravimetric analyzer; analyzing the difference of functional groups on the surface of the PVDF hollow fiber membrane before and after response surface optimization by using a THERMO IR spectrometer, and judging the chemical structure of the surface of the PVDF membrane and the composition of the functional groups before and after response surface optimization.
(4) Responsive surface design
Anaerobic ammonium oxidation bacteria can effectively remove various nitrogen elements in the MBR, and the total nitrogen removal rate of sewage under the conditions of different factor levels is an important comprehensive index for representing the anaerobic ammonium oxidation effect of the MBR. According to the Box-Behnken design principle, the total nitrogen removal rate of the sewage is taken as a response value YAThe method comprises the steps of designing a three-factor three-level response surface curve experiment by using Design Expert software (Version 8.0.6), selecting three influence factors including temperature (A) in an MBR reactor, inorganic carbon source concentration (B) and MBR reactor Hydraulic Retention Time (HRT) (C), and selecting three levels (shown in table 1) for each factor on the basis of a previous single-factor experiment so as to obtain optimal reaction conditions.
The reactor needs to be backwashed after each set of condition tests is finished, because proper backwashing of the membrane modules helps to prolong the service life of the hollow fiber membranes. The initial membrane flux of each test group was 20L/m2H, the sludge concentration was controlled at a MLSS concentration of 2300mg/L, the reactor run time for each test group means the time it took to run when it reached stability after changing the test conditions, the time for each test group to run stably and the data was stably recorded at 7 d.
TABLE 1 response surface analysis factor horizon
(5) Regression model and analysis of variance
Designing experimental factors and levels by using Design Expert software, responding to the experimental values of the surface modification condition optimized by the curved surface, wherein the experimental values are shown in table 2, the table contains 17 experimental points, the first 12 points are factorial points, and the independent variable value is shown in a three-dimensional vertex formed by A, B, C; the latter 5 are zeros, which are the center points of the regions, for estimating experimental errors.
TABLE 2 optimization test scheme and results of PVDF hollow fiber membrane response curved surface in MBR anaerobic ammonia oxidation
And (3) performing multiple regression fitting on the experimental data in the table 2 by using Design Expert software to obtain a secondary multiple regression model of the total nitrogen removal rate of the sewage to A, B, C, wherein the secondary multiple regression model comprises the following steps:
YA＝80.30+9.38A-1.91B+2.28C-4.06AB-2.92AC-3.97BC-0.97A2-15.32B2-11.34C2formula I;
wherein, YAThe total nitrogen removal rate of the sewage is shown as A, the temperature of the membrane bioreactor is shown as B, the concentration of the inorganic carbon source of the sewage is shown as B, and the hydraulic retention time of the membrane bioreactor is shown as C.
The results of the model analysis of variance are shown in table 3, and the significance test of the model coefficients is shown in table 4. As can be seen from table 3, the F value of the model is 56.27, indicating that this model is significant; correction decision coefficient R of model20.9864, P < 0.0001, indicating that the model accounts for a change in response value of 98.64%; the p-value of the mismatching term is 0.1376, greater than 0.05, CV% (Y) of the modelAThe variation coefficient of the model is very low (3.35), the signal-to-noise ratio index Adeq Precision measured by the model is 17.930, which shows that the mismatching item is not significant, the model has good fitting degree and reliability, the experimental error is small, the model is accurate and reliable, and the model can be used for detecting the index in a certain experimental range; in conclusion, the model has good fitting degree and small experimental error, and the response curve model can be used for analyzing and predicting the change of the total nitrogen removal rate of the sewage in the Anammox-MBR regulation and control process. As can be seen from the significance test of the model coefficients in Table 4, the influence of the simulation primary temperature (A) is extremely significant, the influence of the inorganic carbon source concentration (B) and the hydraulic retention time (C) is significant, and the influence sequence of the factors is that A is more than C is more than B; second order term A2Not significant, B2And C2The method is extremely remarkable; the interaction terms AB and BC are extremely significant, and AC is significant.
TABLE 3 regression model ANOVA
Note: p is less than 0.05, and the difference is obvious. Denoted by "; 0.01 < P < 0.05, the difference was very significant, indicated by x.
TABLE 4 Return equation coefficient significance inspection chart
| Factors of the fact | Correlation coefficient | df | Standard deviation of | Lower limit of 95% CI | Upper limit of 95% CI | VIF |
| Intercept of a beam | 80.30 | 1 | 1.01 | 77.92 | 82.69 | |
| A | 9.38 | 1 | 0.80 | 7.49 | 11.26 | 1.00 |
| B | -1.91 | 1 | 0.80 | -3.79 | -0.023 | 1.00 |
| C | 2.28 | 1 | 0.80 | 0.40 | 4.17 | 1.00 |
| AB | -4.06 | 1 | 1.13 | -6.72 | -1.39 | 1.00 |
| AC | -2.92 | 1 | 1.13 | -5.59 | -0.25 | 1.00 |
| BC | -3.97 | 1 | 1.13 | -6.63 | -1.30 | 1.00 |
| A2 | -0.97 | 1 | 1.10 | -3.57 | 1.63 | 1.01 |
| B2 | -15.32 | 1 | 1.10 | -17.92 | -12.72 | 1.01 |
| C2 | -11.34 | 1 | 1.10 | 13.94 | -8.75 | 1.01 |
(5) Response curve optimal condition determination and verification
The method for obtaining the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment through the regression equation preferably includes the steps of solving the regression equation for the first-order partial derivatives of the independent variables respectively, obtaining a ternary linear equation set, and solving the equation set to obtain the inorganic carbon source concentration of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor corresponding to the maximum value of the total nitrogen removal rate of the sewage, so as to obtain the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment.
The effect of inorganic carbon source concentration and temperature on total nitrogen removal from wastewater when the Hydraulic Retention Time (HRT) in the reactor was 10.01h is shown in FIG. 3. As can be seen from FIG. 3, the total nitrogen removal rate of the wastewater increases and then decreases with the increase of the concentration of the inorganic carbon source when the temperature is unchanged; the concentration of the inorganic carbon source is unchanged, and the change of the total nitrogen removal rate of the sewage is slowly increased along with the increase of the temperature. The effect of HRT and inorganic carbon source concentration on total nitrogen removal from wastewater at a reactor temperature of 36 ℃ is shown in FIG. 4. As can be seen from FIG. 4, the concentration of the inorganic carbon source is unchanged, and the total nitrogen removal rate of the wastewater is increased and then decreased along with the increase of HRT; HRT is unchanged, and the total nitrogen removal rate of the sewage is increased and then reduced along with the increase of the concentration of the inorganic carbon source. The effect of HRT and temperature on total nitrogen removal from wastewater when the concentration of inorganic carbon source in the reactor was 0.90mg/L is shown in FIG. 5. As can be seen from FIG. 5, the total nitrogen removal rate of the wastewater increases and then decreases with the increase of HRT at a constant temperature; HRT is unchanged, and the change of the total nitrogen removal rate of the sewage slowly increases along with the increase of the temperature.
The optimal conditions obtained by Design Expert software analysis are as follows: the temperature is 36 ℃, the HRT is 10.01h, the concentration of the inorganic carbon source is 0.90mg/L, and the total nitrogen removal rate of the sewage predicted by the model at the moment is 89.29%. And 3 times of repeated experiments are carried out under the experimental conditions determined by the quadratic regression model to verify the reliability of the response surface model, the average value of the total nitrogen removal rate of the sewage obtained by the three times of experiments is 88.98%, and the average value is basically consistent with the theoretical predicted value of the model, so that the reliability of the optimal surface modification condition obtained by optimizing the response curve is high, and the optimal surface modification condition has actual reference value.
(6) Characterization characteristics of hollow fiber membrane before and after response surface optimization
Through response surface optimization research, the temperature, HRT and inorganic carbon source concentration of the model under the optimal condition under the condition that the total nitrogen removal rate of the sewage is 89.29% are screened out. In the process of response surface optimization, the anaerobic ammonia oxidation membrane bioreactor has obvious advantages in response surface optimization, but the anaerobic ammonia oxidation membrane bioreactor inevitably has membrane pollution phenomenon, which is a main problem influencing the mature development of the MBR process. Relevant researches show that the membrane pollution behavior of the anaerobic ammonia oxidation membrane bioreactor is mainly caused by membrane attachment pollution in the anaerobic ammonia oxidation reaction process, and based on the membrane pollution behavior, the membrane flux change, the thermal analysis change, the functional group type difference and the surface morphology characteristic change before and after the response surface optimization are analyzed, so that effective control measures are provided for the membrane pollution problem in the practical application of the anaerobic ammonia oxidation membrane bioreactor process.
1) Response to changes in membrane flux before and after optimization of the curved surface
The membrane bioreactor process has incomparable advantages of other sewage treatment methods in the sewage treatment field, but in the research, the anaerobic ammonia oxidation membrane bioreactor system continuously increases the filtration resistance caused by membrane pollution when in operation, and although the response curve surface of the anaerobic ammonia oxidation membrane bioreactor system is optimized, the system still has the problem of membrane filtration flux attenuation, so that the monitoring of the membrane flux is particularly important.
The definition of membrane flux refers to the amount of permeate per unit of membrane area per unit time, and is defined by the formula:
wherein V represents the volume of solution that permeates the MBR reactor; s represents the effective area of the membrane; t represents an operation time. The results of the membrane flux calculations are shown in fig. 6. The first day and the 121 th day represent data before and after the response surface optimization respectively, the middle 119 days of data (17 factors, each factor being 7 days) represent data of one week after the stabilization of 17 anaerobic ammonia oxidation membrane bioreactor systems set under different condition response surface optimization conditions, and the sequence is tested according to the sequence in table 2. As can be seen from FIG. 6, the membrane flux generally decreased correspondingly throughout the response surface optimization reactor, i.e., after each experimental runLess tendency, 15.815L/m before response surface optimization2H is reduced to 7.123L/m after response surface optimization2H, probably because the improvement on membrane pollution is not obvious and the membrane flux is reduced on the contrary, as the response surface optimization process is carried out, although the operation efficiency of the membrane bioreactor for removing nitrogen wastewater by anaerobic ammonia oxidation is optimized.
2) Hollow fiber membrane thermogravimetric analysis before and after response surface optimization
The thermogravimetric analysis test results are shown in fig. 7. The temperature rise rate of thermogravimetric analysis is 10 ℃/min, and the atmosphere is high-purity nitrogen. The overall weight loss process of the PVDF sample before the optimization of the response curve can be divided into two stages, the first stage is from room temperature to 165 ℃, the percentage of the total weight of the sample lost in the first stage is 10.8%, and the component lost is water or residual volatile substances in the sample, which can be 3363.41cm in the infrared spectrum-1The occurrence of a stretching vibration peak of-OH in water is proved. The temperature of 350-. The No. 2 PVDF sample after the optimization of the response curved surface has only one step, loses 81.45 percent of the total weight of the sample at the temperature of 350-400 ℃, and the weight loss of the two samples at the second step is caused by the dehydrofluorination reaction of PVDF, so that double bond rearrangement and oxidation reaction occur, and the quality of the sample is reduced.
By combining the thermal analysis results, the PVDF sample with the optimized response surface has certain thermal stability and is not easy to decompose below 340 ℃. However, the decomposition temperature of the PVDF sample before the optimization of the response surface is obviously higher than that of the PVDF sample after the optimization of the response surface, which shows that the thermodynamic stability of the PVDF sample after the optimization of the response surface is reduced. After the temperature continued to rise to 500 ℃, the sample had degraded completely, meaning that the reaction had substantially ended at 500 ℃, with residual groups of 15.58% and 18.53% of the sample before and after contamination, respectively.
The method of determining the kinetic parameters of the reaction using the values of the reaction rate (d α/dt) max at the peak of the DTG curve and the corresponding values of (1- α) p and temperature Tp is called the maximum rate method. Clearly, the reaction rate is maximal at the peak of the DTG curve and there are:
taking natural logarithms on two sides of the formula (2), and obtaining a derivative of the temperature T at the position where T is T', and finishing the derivative to obtain the following product:
in the formula
For the reaction rate, the subscript P represents a number taken at the peak of the DTG curve, A is a frequency factor, E is the reaction activation energy (kJ/mol), R is the molar gas constant (J/(mol. K)), T is the absolute temperature (K) at the time of reaction, and n is the number of reaction stages.
The activation energy E of the PVDF sample before and after the optimization of the response curved surface is calculated to be 215.92kJ/mol and 122.09kJ/mol respectively, the activation energy of the PVDF sample after the optimization of the response curved surface is reduced, and meanwhile, the thermogravimetric analysis result shows that the thermal-mechanical stability of the PVDF hollow fiber membrane in the anaerobic ammonia oxidation membrane bioreactor process has a tendency of reduction after the optimization of three related factors.
3) Film filament surface infrared analysis before and after response surface optimization
The results of the IR analysis are shown in FIG. 8. it can be seen from FIG. 8 that the sample was 3363.41cm before response optimization-1The broad peak is the stretching vibration peak of different structures of-OH, and the appearance of the peak is probably caused by the moisture contained in the sample. The sample before optimization and the sample after optimization are both 2923.38cm-1Is represented by CH2Is symmetrically telescopicVibration absorption peaks, here more similar; the sample was at 1654.07cm before response optimization-1The weak absorption peak is C ═ C stretching vibration peak. The peak intensity is weakened after the response surface optimization, and the weakening phenomenon of the peak intensity can be caused by the free movement of C ═ C free radicals at the end groups of the macromolecules. Also, as can be seen in FIG. 8, the two samples are at 1401.56cm-1And 875.57cm-1All are CH2The variable angle vibration absorption peak of (2) at 840.08cm-1Is CF2Has an asymmetric stretching vibration absorption peak of 1273.72cm-1The left and right are antisymmetric telescopic vibration of C-C at 1172.72cm-1Vicinity to CF2Peak of stretching vibration at 1071.76cm-1Characteristic absorption peak of 1000cm-1The following stretching vibration frequency is the absorption peak of long-chain hydrocarbon at 508cm-1Vicinity to CF2Bending vibration and rocking vibration frequencies.
Through comparison, the types of functional groups of the sample after the response surface optimization have certain difference, which is mainly shown in that the sample after the optimization is 1731.3cm-1Where the aldehyde carbonyl, carboxylic acid carbonyl and ester carbonyl and ketone carbonyl C ═ O stretching vibrations occur. The reason why the C ═ O stretching vibration occurs is that after the response surface is optimized, an induction effect is generated to cause the bonding electron density to approach the geometric center of the bond, and the intermediate electron density of C ═ O is increased by adding the increase of the bond force constant, so that the C ═ O stretching vibration occurs. Meanwhile, it can be seen that the absorption peaks of other functional groups are weakened. The analysis result further proves that the structure of the sample functional group after the response surface optimization has certain change.
Since the membrane material for thermogravimetric and infrared spectroscopic property analysis was not washed, it was necessary to prove that the increase of functional groups such as aldehyde carbonyl, carboxylic acid carbonyl and ester carbonyl and ketone carbonyl was not derived from microorganisms attached to the membrane surface, so that the two curves of fig. 8 were analyzed by placing them at different heights in the vertical direction with the abscissa unchanged. It can be seen that the two curves are at 2920cm-1、2850cm-1The peaks are respectively attributed to C-H bond antisymmetric stretching vibration and symmetric stretching vibration peaks in the hydrocarbon group, and the wave number in the PVDF film before the optimization of the response curved surfaceIs 763cm-1、840cm-1、875cm-1The peak is C-H bond wobble vibration and C-F bond stretching vibration in the membrane, 1172cm-1、1401cm-1And 1071cm-1The presence of the absorption band may be due to C-C bending. In the PVDF film after the optimization of the response surface, the wave number is 763cm-1、840cm-1、876cm-1The peak is C-H bond swing vibration and C-F bond stretching vibration in the membrane, 1178cm-1、1402cm-1And 1071cm-1The presence of the absorption band may be due to C-C bending. 1644cm-1The peak is H-O-H variable angle vibration, 1731cm-1The peak is carbonyl C ═ O bond stretching vibration peak, 1654cm in PVDF film after response surface optimization-1A stretching vibration peak of carbonyl C ═ O bond also appears in the vicinity. This indicates that no new carbonyl peak appears after the PVDF membrane is optimized by the response surface, thereby proving that the increase of the content of aldehyde carbonyl, carboxylic acid carbonyl, ester carbonyl or ketone carbonyl does not originate from microorganisms on the surface of the PVDF membrane.
4) Hollow fiber membrane atomic force microscopy analysis before and after response surface optimization
The change of the film surface appearance characteristic is further observed by an Atomic Force Microscope (AFM), and the principle is that the electrostatic force generated by the surface load interaction between the micro probe and the solid material to be detected is utilized to present the physical characteristics of the surface of the object to be detected. In AFM, one scan can obtain images of two different data types, namely an elevation map and a phase map. The height map reflects the topography of the material surface, and the image can be directly used to evaluate the roughness of the material surface. The change in surface roughness of PVDF hollow fiber membranes before and after response surface optimization is shown in fig. 10.
As can be seen from the surface topography, the surface of FIG. 10(a) has stronger layering, part of the area has severe fluctuation, and the surface of the membrane wire is relatively smooth. In FIG. 10(b), the surface is mostly small blocky protrusions, and the surface roughness is stronger. As can be seen from fig. 10(a), the PVDF surface is smooth before the response surface optimization, the roughness is close to zero, the rms (rq) roughness is 30.6nm, the average roughness (Ra) is 24.9nm, when the reactor after the response surface optimization is in operation, sludge, microorganisms and other substances are attached to the surface of the hollow fiber membrane, the roughness of the PVDF hollow fiber membrane is improved, the rms (rq) roughness is improved to 77.9nm, and the average roughness (Ra) is improved to 57.1 nm. The comparison shows that the roughness of the PVDF hollow fiber membrane after response optimization is really improved, and the filtration performance is reduced due to the microbial adhesion interaction or mechanical action on the surface of the membrane, so that the phenomena of adsorption, deposition and pollution of the membrane surface are caused.
On the basis of early-stage anaerobic ammonia oxidation membrane bioreactor starting and single-factor experiments, a secondary polynomial regression model of temperature, inorganic carbon source concentration and HRT (high resolution transformation) on the change of the total nitrogen removal rate of sewage is established by a response curve method, and tests show that the model is reasonable and reliable. According to the feasibility of model optimization and practical experiments, the response surface condition when the total nitrogen removal rate of sewage in the Anammox-MBR is the highest is obtained, wherein the temperature is 36 ℃, the concentration of the inorganic carbon source is 0.90mg/L, and the HRT is 10.01 h. The PVDF hollow fiber membrane after response surface optimization has reduced thermodynamic stability and reduced activation energy; after the response curved surface is optimized, functional groups on the surface of the membrane wire are changed, and groups such as aldehyde carbonyl, carboxylic acid carbonyl, ester carbonyl, ketone carbonyl and the like are added; the optimized PVDF hollow fiber membrane has increased roughness (Rq is increased from 30.60nm to 77.90nm) due to the fact that sludge, microorganisms and the like are attached to the surface in the regulation and optimization process. The PVDF hollow fiber membrane after the response curved surface optimization has poor stability and rough membrane surface, is influenced by certain membrane pollution, and needs to make a suitable membrane cleaning scheme to remove dirt on the membrane surface so as to realize the long-term stable operation of Anamox-MBR.
Although the present invention has been described in detail with reference to the above embodiments, it is only a part of the embodiments of the present invention, not all of the embodiments, and other embodiments can be obtained without inventive step according to the embodiments, and the embodiments are within the scope of the present invention.
Claims (10)
1. A method for optimizing denitrification performance of an anaerobic ammonia oxidation membrane bioreactor based on a response surface method is characterized by comprising the following steps:
adopting a single factor variable method to obtain each single factor value of the denitrification process of the anaerobic ammonia oxidation membrane bioreactor corresponding to the condition that the total nitrogen removal rate of the sewage is more than or equal to 80 percent; the single factors comprise the concentration of an inorganic carbon source of the sewage, the temperature of the anaerobic ammonia oxidation membrane bioreactor and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor;
and (3) carrying out a response surface optimization test by taking the single factor values as independent variables and the total nitrogen removal rate of the sewage as response values, and carrying out multiple regression fitting on the data of the obtained multiple groups of response surface optimization tests to obtain a regression equation of the total nitrogen removal rate of the sewage:
and respectively solving a first-order partial derivative of the temperature of the membrane bioreactor, the concentration of the inorganic carbon source of the sewage and the hydraulic retention time of the membrane bioreactor through the regression equation to obtain a ternary linear equation set, and solving the equation set to obtain the denitrification parameter of the anaerobic ammonia oxidation membrane bioreactor for sewage treatment.
2. The method according to claim 1, wherein in the single-factor variable method, the concentration of the inorganic carbon source in the sewage is 0.5-1.5 mg/L, the temperature of the anaerobic ammonia oxidation membrane bioreactor is 30-36 ℃, and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor is 8-12 h.
3. The method according to claim 1 or 2, wherein the values of the independent variables are end values and intermediate values of the value ranges of the individual factors.
4. The method of claim 1, wherein the Design of the response surface optimization test and the multiple regression fitting are performed by Design Expert 8.0.6 software.
5. The method according to claim 1, wherein the concentration of the inorganic carbon source in the sewage in the denitrification parameters is 0.85-0.95 mg/L, the temperature of the anaerobic ammonia oxidation membrane bioreactor is 33.5-36 ℃, and the hydraulic retention time of the anaerobic ammonia oxidation membrane bioreactor is 9.95-10.07 h.
6. The method according to claim 1, wherein the membrane module of the anaerobic ammonia oxidation membrane bioreactor is a hollow fiber membrane; the hollow fiber membrane is made of polyvinylidene fluoride with a lining.
7. The method according to claim 6, wherein the hollow fiber membrane has a filtration precision of 0.1 μm; the inner diameter of the membrane filaments of the hollow fiber membrane is 1.2 mu m; the outer diameter of the membrane filaments of the hollow fiber membrane is 2.2 mu m.
8. The method according to claim 7, wherein the hollow fiber membrane has an effective membrane area of 0.06m2。
9. A method according to any one of claims 6 to 8, wherein the hollow fibre membranes are pre-treated prior to use, the pre-treatment comprising the steps of: immersing the hollow fiber membrane in an ethanol solution, and sequentially standing, washing and thermally treating.
10. A denitrification method based on an anaerobic ammonia oxidation membrane bioreactor is characterized by comprising the following steps: the method for optimizing the denitrification performance of the anaerobic ammonia oxidation membrane bioreactor based on the response surface method according to any one of claims 1 to 9 is used for obtaining denitrification parameters, and sewage is introduced into the anaerobic ammonia oxidation membrane bioreactor for denitrification treatment according to the obtained denitrification parameters.
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| Publication number | Priority date | Publication date | Assignee | Title |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2015230864A1 (en) * | 2014-10-31 | 2016-05-19 | Nanjing University | Method for measuring concentration of dissolved organic nitrogen of secondary effluent |
| CN109665596A (en) * | 2018-12-14 | 2019-04-23 | 浙江工业大学 | Optimize the method for reverse osmosis membrane removal biogas slurry COD and ammonia nitrogen effect simultaneously |
| CN111612235A (en) * | 2020-05-13 | 2020-09-01 | 吉林省农业科学院 | Method for optimizing parameters of magnetic separation process for treating aquaculture sewage in combination mode |
| CN111948346A (en) * | 2020-08-11 | 2020-11-17 | 江苏省地质工程勘察院 | Response curved surface optimization method for biochar preparation for removing cadmium in solution |
| CN112908430A (en) * | 2019-12-03 | 2021-06-04 | 中国科学院大连化学物理研究所 | Experimental method for optimizing normal olefin prepared by high-carbon alcohol dehydration by using response surface method |
| CN113609442A (en) * | 2021-08-18 | 2021-11-05 | 中冶生态环保集团有限公司 | Fenton oxidation high-concentration wastewater multi-factor optimization method based on response curved surface |
-
2021
- 2021-11-26 CN CN202111419423.3A patent/CN114084955A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2015230864A1 (en) * | 2014-10-31 | 2016-05-19 | Nanjing University | Method for measuring concentration of dissolved organic nitrogen of secondary effluent |
| CN109665596A (en) * | 2018-12-14 | 2019-04-23 | 浙江工业大学 | Optimize the method for reverse osmosis membrane removal biogas slurry COD and ammonia nitrogen effect simultaneously |
| CN112908430A (en) * | 2019-12-03 | 2021-06-04 | 中国科学院大连化学物理研究所 | Experimental method for optimizing normal olefin prepared by high-carbon alcohol dehydration by using response surface method |
| CN111612235A (en) * | 2020-05-13 | 2020-09-01 | 吉林省农业科学院 | Method for optimizing parameters of magnetic separation process for treating aquaculture sewage in combination mode |
| CN111948346A (en) * | 2020-08-11 | 2020-11-17 | 江苏省地质工程勘察院 | Response curved surface optimization method for biochar preparation for removing cadmium in solution |
| CN113609442A (en) * | 2021-08-18 | 2021-11-05 | 中冶生态环保集团有限公司 | Fenton oxidation high-concentration wastewater multi-factor optimization method based on response curved surface |
Non-Patent Citations (2)
| Title |
|---|
| 刘建伟: "《垃圾渗滤液处理技术及工程实例》", vol. 1, 北京：中国建材工业出版社, pages: 156 - 158 * |
| 唐正坤等: "响应曲面法分析pH和温度对厌氧氨氧化脱氮效能的影响", 《净水技术》, vol. 38, no. 03, pages 82 - 87 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114455691A (en) * | 2022-03-03 | 2022-05-10 | 北京工业大学 | Composite sewage denitrification process device and operation parameter optimization method |
| WO2023165001A1 (en) * | 2022-03-03 | 2023-09-07 | 北京工业大学 | Composite sewage denitrification process device and operation parameter optimization method |
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