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 Journal of Zhejiang University SCIENCE A 2014 Vol.15 No.9 P.743-752 http://doi.org/10.1631/jzus.A14b0066

Calibration and validation of an activated sludge model for a pilot-scale anoxic/anaerobic/aerobic/post-anoxic process*

 Author(s):  Xiang Hu, Li Xie, Chuang Mi, Dian-hai Yang Affiliation(s):  . State Key Laboratory of Pollution Control and Resources Reuse, Tongji University, Shanghai 200092, China Corresponding email(s):   sally_xieli@163.com Key Words:  Activated sludge model, Simulation, Calibration, Validation, Sensitivity analysis Share this article to： More <<< Previous Article|Next Article >>>

Xiang Hu, Li Xie, Chuang Mi, Dian-hai Yang. Calibration and validation of an activated sludge model for a pilot-scale anoxic/anaerobic/aerobic/post-anoxic process[J]. Journal of Zhejiang University Science A, 2014, 15(9): 743-752.

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%A Xiang Hu
%A Li Xie
%A Chuang Mi
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A1 - Li Xie
A1 - Chuang Mi
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J0 - Journal of Zhejiang University Science A
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PB - Zhejiang University Press & Springer
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DOI - 10.1631/jzus.A14b0066

Abstract:
The aim of this study was to establish an activated sludge model and to verify its predictability for use in a pilot-scale anoxic/anaerobic/aerobic/post-anoxic (modified AAO) process. Respirometric measurements were conducted to identify the influent organic characteristics and to determine the yield coefficient (Y H) and decay coefficient (b H) for heterotrophic biomass (OHOs). The values obtained for Y H and b H were 0.72 mg COD/mg COD and 0.275 d−1, respectively. Within the model’s calibration, the most influential stoichiometric and kinetic parameters were identified with the aid of sensitivity analysis. The output of the model was most sensitive to parameters associated with the growth and decay of OHOs and ammonia-oxidizing biomass (AOB) (Y H, μ maxH, K s, b H, μ maxA, K NH4A, and b aeroa,A). Furthermore, all the calibrated parameters, with the exception of Y PAO, aerob related to the phosphorus accumulating organisms (PAOs), could be regarded as influential. Both steady-state and dynamic simulations indicated good agreement between the simulated and measured values of the output variables. The calibrated model can be used to provide insight into the pilot-scale modified AAO process, and information needed to optimize design and operation when applied at full-scale.

## 1.  Introduction

Increasingly stringent limits for nitrogen and phosphorus contamination have encouraged the widespread use of various biological nutrient removal (BNR) processes in wastewater treatment practice worldwide, both for upgrading existing wastewater treatment facilities and for the design of new facilities (Hu et al., ). Facing diverse organisms and complicated conversion processes in a BNR system, activated sludge mathematical models have proved powerful and valuable tools (Petersen et al., ; ). In recent years, many mathematical models based on the activated sludge model (ASM) family (ASM1, ASM2, ASM2d, and ASM3) have been evaluated and optimized for BNR processes such as anaerobic/anoxic/aerobic (AAO) (Pai, ; Liwarska-Bizukojc et al., ), Johannesburg (JHB) (Makinia et al., ), modified University of Cape Town (MUCT) (Czerwionka et al., ), sequencing batch reactor (SBR) (Ni et al., ), and membrane bioreactor (MBR) (Fenu et al., ). A novel anoxic/anaerobic/aerobic (modified AAO) process with an anoxic stage before an anaerobic stage, developed by Zhang and Gao (), has shown high removal efficiencies for nitrogen and phosphorus from low C/N wastewater. This modified AAO process has been extensively applied in more than 100 wastewater treatment plants (WWTP) in China and Japan (Fu et al., ). Nevertheless, limited information is available on performance evaluation and especially on mathematical modeling of the modified AAO process, which requires detailed wastewater characterization and model calibration/validation (Gernaey et al., ).

Model calibration, which is necessary for successfully applying mathematical models to describe the overall behavior of a BNR system, is defined as the adaptation of the model to fit a certain set of information obtained from a practical WWTP (Petersen et al., ). Different methods for the calibration of ASM models have been developed (Vanrolleghem et al., ; Langergraber et al., ), and a detailed summary and comparisons were presented by Sin et al. (). Note that the above studies emphasized the role of sensitivity analysis in the process of model calibration. The calibration and determination of all model parameters is expensive and time-consuming. Thus, a sensitivity analysis that enables the identification of the most influential parameters would be a very practical tool for a given model. Hence, a sensitivity analysis could be incorporated into the calibration protocol, both to minimize effort and to optimize the overall calibration procedure (Vanrolleghem et al., ). Several attempts have been made to identify the most sensitive parameters for ASM-family models (Weijers and Vanrolleghem, ; Brun et al., ; Petersen et al., ; Makinia et al., ). Weijers and Vanrolleghem () proposed a reduced set of the most sensitive parameters by means of sensitivity analysis, for calibrating ASM1 to a full-scale plant. The reduced set included the following kinetic and stoichiometric parameters: a yield coefficient for heterotrophic biomass (Y H), a yield coefficient for autotrophic biomass (Y A), the maximum specific growth rate for heterotrophic biomass (μ maxH), a decay rate constant for heterotrophic biomass (b H), the maximum specific growth rate for autotrophic biomass (μ maxA), a substrate half-saturation constant for heterotrophic organisms (K s), an oxygen half-saturation constant for autotrophic organisms (K OA), and an anoxic growth factor (η anoxic,H). Makinia et al. () identified the most influential parameters for ASM2d and ASM3P models for simulation of nitrogen removal on the basis of the normalized sensitivity coefficient (S i, j ). The most influential parameters for effluent PO4 3−-P and NH4 +-N concentrations were related to the ammonia-oxidizing biomass (AOB), phosphorus accumulating organisms (PAOs) and wastewater composition. However, low values of S i,j were associated with effluent NO3 -N. Liwarska-Bizukojc et al. () reported that, based on calculations of S i,j , 17 (steady-state) or 19 (dynamic conditions) kinetic and stoichiometric parameters were sensitive. Most of them were associated with growth and decay of ordinary heterotrophic organisms (OHOs) and PAOs.

The aim of this study was to establish and verify the predictability of an activated sludge model for a pilot-scale anoxic/anaerobic/aerobic/post-anoxic (modified AAO) process. Calibration and validation of the model were implemented, with the most sensitive parameters singled out by sensitivity analysis. The use of sensitivity analysis in the development of an activated sludge model for a modified AAO process has not previously been reported.

## 2.  Materials and methods

### 2.1.  Pilot-scale modified AAO plant

The pilot-scale modified AAO plant treats municipal wastewater at a flow rate of 50 m3/d, and is located in the city of Hefei, Anhui Province (southern China). The process configuration is anoxic/anaerobic/aerobic/post-anoxic followed by a membrane tank to replace the settling tank for solid-liquid separation (Fig. 1). A unique feature of this system is a post-anoxic zone, located between the aerobic zone and the membrane tank to reduce the dissolved oxygen (DO) concentration of the aerobic effluent to below 0.5 mg/L before its recirculation to the anoxic zone. Two different internal recycles were provided: R1 (Q=400%) from the post-anoxic to the anoxic zone, and R2 (Q=100%) from the membrane tank to the aerobic zone. The anoxic and anaerobic zones were each equipped with a low-speed mixer to keep the mixed liquor suspended solids (MLSS) in suspension. The membrane tank was fitted with a submerged hollow fiber membrane (PVDF) with a nominal pore size of 0.1 μm (Mohua Membrane Materials of Science and Technology Co., Ltd., Suzhou, China). The total membrane area was 256 m2. A permeate pump was operated according to a timing sequence that consisted of a 9 min switch on and a 1 min switch off. Excess sludge was removed daily as waste from the membrane tank to maintain a relatively stable MLSS concentration and the desired sludge retention time (SRT) of 16 d. The plant was provided with a programmable logic controller (PLC) that controlled all of the automatic control loops of the system. The detailed design and operational parameters of the modified AAO plant are summarized in Table 1.

Fig.1
Schematic diagram of the pilot-scale modified AAO plant

#### Table 1

Design and operational parameters of the pilot-scale modified AAO plant
 Operating parameter Value Anoxic (ANO) volume (m3) 12 Anaerobic (ANE) volume (m3) 6 Aerobic volume (AE) (m3) 12 Post-anoxic volume (PANO) (m3) 6 MBR volume (m3) 12 Influent flow (m3/d) 50 R1a (%) 400 R2b (%) 100 HRT (h) 14.66 SRT (d) 16 Temperature (°C) 25±7 pH 7.5±0.5 MLSS in AE (mg/L) 3500±1000 MLSS in MBR (mg/L) 5500±2500 DO in AE (mg/L) 2.5±0.5 DO in MBR (mg/L) 7.0±1.0

• aRecycle ratio with respect to inflow flow from PANO to ANO

• bRecycle ratio with respect to inflow flow from MBR to AE

### 2.2.  Data collection for the calibration and validation of the model

Data collected from the pilot-scale modified AAO plant from April to May 2012 (Phase I) were used as input values for model calibration. The model was then validated on the basis of two independent datasets, obtained in June (Phase II) and July 2012 (Phase III) (Table 2), respectively. These data were evaluated using Student’s t-test (to compare the means of the different datasets) and the F-test (to compare differences between the standard deviations of the datasets). Student’s t-test was paired with the F-test to determine the statistical significance of the observed differences between the measured data for the total chemical oxygen demand (TCOD), soluble COD (SCOD), ammonia (NH4 +-N), nitrate (NO3 -N), nitrite (NO2 -N), total nitrogen (TN), total phosphorus (TP), total suspended solids (TSS), and pH at the 95% confidence level. Finally, the average values were used as input for the model. The analysis of TCOD, SCOD, NH4 +-N, NO3 -N, NO2 -N, TN, TP, and TSS was conducted in accordance with standard methods (APHA, ). The pH was measured using a Cyber Scan pH 510 pH/ORP pH meter (Eutech).

#### Table 2

Influent and effluent characteristics at different phases (unit: mg/L except pH)
 Phase TCOD SCOD NH4 +-N NO3 −-N NO2 −-N TN TP TSS pH Ia Influent 224±68 97±24 28.71±10.86 1.06±0.95 0.06±0.002 50±3.12 4.20±1.80 127±11 7.63±0.12 Effluent 22.47±1.47 – 1.47±1.28 25.08±2.14 0.04±0.002 27.05±2.50 2.31±2.19 0±0 7.18±0.28 IIb Influent 239±135 102±29 31.26±8.52 1.04±0.39 0.06±0.003 40.44±8.69 4.60±2.41 116±23 7.53±0.10 Effluent 21.59±3.54 – 1.83±1.18 23.02±2.79 0.04±0.002 25.36±2.86 2.04±1.56 0±0 7.12±0.24 IIIc Influent 232±87 91±31 32.41±7.62 0.94±0.38 0.06±0.002 40.29±8.30 3.16±1.70 133±26 7.61±0.08 Effluent 20.89±2.93 – 1.67±0.92 20.93±3.27 0.03±0.002 22.34±3.93 2.17±1.63 0±0 6.92±0.11

• aMean±SD (n=26)

• bMean±SD (n=21)
cMean±SD (n=19)

### 2.3.  Respirometric tests

Respirometric tests, based on the measurement of oxygen uptake rate (OUR), were first used to estimate the COD fractions of the influent wastewater. At the beginning of the respirometric test, fresh returned activated sludge (RAS) was diluted with the treated wastewater to obtain 3 L of mixed liquor with an MLVSS concentration of around 1500 mg/L. The actual MLVSS concentration in the reactor was measured at the beginning of the test. The DO set point in the main reactor was 6.0 mg O2/L. The OUR measurement in one cycle was conducted for 3 min.

Respirometric tests were also carried out to measure the kinetic parameters of the heterotrophic biomass, i.e., the heterotrophic yield coefficient (Y H) and decay coefficient (b H). Detailed methods for evaluation of Y H and b H can be found in (Ni and Yu, ).

### 2.4.  Model and simulation environment

The simulations in this work were performed using the full general activated sludge (AS) model implemented in BioWinTM 3.1 (EnvirnSim ). The modified AAO plant was modeled using the basic reactors available in BioWinTM 3.1, i.e., influent, non-aerated bioreactors, aerated bioreactors, MBR, nitrate recirculation, effluent, and sludge wastage effluent (Fig. 2).

Fig.2
Model configuration of the modified AAO plant in the BioWin simulator
SAS: surplus activated sludge

### 2.5.  Sensitivity analysis

Sensitivity analysis was used to evaluate the extent to which the parameters used in model calibration could influence the model’s output. The analysis was conducted using the various carbonaceous and nutrient fractions in the wastewater (estimated from measurements of the influent), as well as the default values for each stoichiometric and kinetic parameter defined in the BioWin AS model. Specifically, the sensitivity analysis used the normalized sensitivity functions (S i, j ) shown in Eq. (1) defined by US EPA (), representing the percentage change in the output variable (yj ), resulting from a 10% change in the input variable (xi ): $${S_{i,j}} = \frac{{\Delta {y_j}/{y_j}}}{{\Delta {x_i}/{x_i}}}$$.

The influence of each parameter on the model’s output was classified into one of four categories proposed by Petersen et al. (): (a) no significant influence (S i, j <0.25); (b) influential (0.25≤S i, j <1); (c) very influential (1≤S i, j <2); (VI) extremely influential (S i,j ≥2). When the values of a parameter and the output change were in the same direction, this was interpreted as positive; otherwise, the result was considered negative.

## 3.  Results

### 3.1.  Respirometric tests results

The composition of the influent COD was calculated based on respirometric profiles, and the contributions of the constituents to the TCOD are presented in Table 3. The estimated readily biodegradable fraction (S S) and the slowly biodegradable COD (X S) accounted for 6.0%–11.2% and for 6.9%–16.8% of TCOD, respectively. Comparative studies performed on raw wastewater in a BNR plant in southern China revealed a similar ratio of S S in the range of 6.9%–10.3%, but higher X S ratio (38.9%– 45.5%) of TCOD (Zhou et al., ). Higher ratios of S S and X S of TCOD were reported in another modified AAO plant in southern China (Zhou et al., ). The fraction of inert particulate organic compounds (X I) in this study accounted for 60.6%–70.1% of TCOD, much higher than reported values (18.5%–45.5%) for wastewaters in China (Zhou et al., ; ). The most likely reason for the relatively lower S S and X S but higher X I in this study is that the influent was not raw wastewater, but wastewater from the primary settled clarifier, in which S S was biodegraded and X S was partly hydrolyzed. Another possibility is that the biodegradable substrates in the influent partially converted to non-biodegradable organic compounds under the active biomass growth in the sewer after a long pipeline transportation.

#### Table 3

Organic matter fraction in the influent at the modified AAO plant
 Component Concentration (mg/L) TCOD (%) This study Plant 1 (Zhou et al., 2009) Plant 2 (Zhou et al., 2011) S I 12.9–35.8 8.2–22.0 6.3–9.9 10.65–17.1 S S 10.2–18.2 6.0–11.2 6.9–10.3 Approximately 20 X I 98.7–129.4 60.6–71.1 23.3–31.1 17.33–34.34 X S 12.8–31.2 6.9–16.8 38.9–45.5 14.20–26.41 TCOD 156.2–185.8 100.0 100.0 100.00

Based on the respirometric results (Fig. 3), the Y H and b H for the heterotrophic biomass were calculated as 0.72 mg COD/mg COD and 0.275 d−1, respectively. This will be discussed in detail in Section 3.4.

Fig.3
Typical respirometric profiles used for the measurements of (a) Y H and (b) b H

It is clear from other studies that there is an interaction between wastewater characteristics and the calibration of a full-scale model to the available data (Petersen et al., ). In this study, the various carbonaceous and nutrient fractions present in the influent included in the BioWin AS model are listed in Table 4. If data were not available, the default values in the model were used.

#### Table 4

Default and calibrated carbonaceous and nutrient fractions in wastewater
 Fraction Default value Input value Readily biodegradable, F bs (g COD/g TCOD) 0.20 0.22a Acetate, F ac (g COD/g rbCOD) 0.15 0.15 Non-colloidal slowly biodegradable, F xsp (g COD/g sbCOD) 0.75 0.54a Non-biodegradable soluble, F us (g COD/g TCOD) 0.05 0.14a Non-biodegradable particulate, F up (g COD/g TCOD) 0.13 0.10a Ammonia, F na (g NH3-N/g TKN) 0.66 0.57a Particulate organic nitrogen, F nox (g N/g Organic N) 0.50 0.10a Soluble non-biodegradable TKN, F nus (g N/g TKN) 0.02 0.02 N:COD ratio for non-biodegradable particulate COD, F upN (g N/g COD) 0.035 0.036a Phosphate, F po4 (g PO4-P/g TP) 0.50 0.62a P:COD ratio for influent non-biodegradable particulate COD, F upP (g P/g COD) 0.011 0.015a

• aCalibrated using the experimental data

•  The simulations, performed with the default values of the kinetic and stoichiometric parameters in the BioWin AS model, revealed discrepancies between the measured and simulated values of the output variables (Fig. 4). These discrepancies were especially prominent with several output variables characterizing the effluent, i.e., COD, TN, NH4 +-N, and NO3 -N. This suggested the need for model calibration.

Fig.4
Measured data vs. simulated values of the selected output variables in the effluent using the default values (unit: mg/L except pH)

### 3.3.  Sensitivity analysis

The normalized sensitivity coefficient (S i, j ) ranks model parameters based on their contribution to the overall error in the model predictions. In this study, the sensitivity analysis comprised 11 stoichiometric and 24 kinetic parameters. The most sensitive (S i, j ≥0.25) parameters and their corresponding S i, j , calculated with respect to 8 effluent characteristics, are presented in Table 5. However, for two of them, i.e., effluent COD and pH, the S i, j values were always below 0.25. Note also that as all the S i, j values for the PAOs were below 0.25, they were excluded from Table 5. Based on the values of S i, j for each parameter, 4 stoichiometric and 18 kinetic parameters were found to be sensitive while 9 parameters could be classified as influential (0.25≤S i, j <1), 6 as very influential (1≤S i, j <2), and 7 as extremely influential (S i, j ≥2).

#### Table 5

S i, j values for the most sensitive (S i, j ≥0.25) parameters of the calibrated model
 Parameter S i, j COD BOD NH4 +-N NO3 −-N NO2 −-N TN TP pH Stoichiometric Y H 1.481 −2.333 Y H,anoxic −0.467 P:COD −0.707 Kinetic AOB μ maxA 1.000 −3.594 2.691 −3.000 −3.732 −2.025 K NH4A 1.155 0.777 b aeroa,A 3.367 1.175 0.558 0.264 OHOs μ maxH −1.852 0.347 K s 1.046 −0.308 b H 0.886 0.339

Among the 11 stoichiometric parameters, the heterotrophic biomass yield (Y H) showed high S i, j values for the TP (S i, j =−2.333) and BOD (S i, j =1.481) concentrations in the effluent (Table 5). This indicated that a small variation in Y H would result in a large change in the simulated model output on effluent TP and BOD. Y H,anoxic exerted an influence (S i, j =−0.467) on the effluent TP level, as did the P:COD ratio (S i, j =−0.707). An increase in the P concentration in a low COD influent will increase phosphorus levels in the effluent.

The kinetic parameters identified as sensitive were associated with the growth and decay of AOB and OHOs. For the AOB, the maximum growth rate (μ maxA) influenced most of the simulated model output. Five of the eight simulated model outputs had sensitivity values higher than 2. The S i, j of μ maxA on NH4 +-N was −3.594, which confirmed that even a slight modification of the value of μ maxA can have a significant impact on the model’s output for NH4 +-N. In addition, K NH4A was found to have less impact on the nitrification process, i.e., for the AOB the nitrification rate from NH4 +-N to NO3 -N was slower, along with a decreased KNH4A. This trend also led to a decrease in TN removal. Similarly, a change in b aeroa,A can be expected to influence strongly NH4 +-N under aerobic conditions. For the OHOs, μ maxH, K s, and b H were influential for effluent BOD and TP.

Most of the parameters identified as influential in ASM1 were found to be sensitive in this study for the BioWin AS model. Five out of eight kinetic and stoichiometric parameters belonging to the reduced set of parameters determined in a previous study (Weijers and Vanrolleghem, ) were found also to be influential in this work. These parameters were associated with the growth and decay of OHOs and AOB, i.e., Y H, μ maxH, b H, μ maxA, and K s. These results coincide with the findings of Liwarska-Bizukojc and Biernacki () and indicate that some basic parameters of Monod kinetics for OHOs and AOB should be determined regardless of the model used, preferably with the help of an appropriate experimental procedure.

### 3.4.  Model calibration

Based on the sensitivity analysis, seven parameters (b aerob,A for AOB, μ maxH, b H, K s, Y H, Y H,anoxic for OHOs and Y PAO,aerob for PAOs) were selected to calibrate the specific model in order to match the predicted and measured effluent concentrations. In Table 6, all calibrated parameters for the steady-state and dynamic calibrations are compared with published values (Henze et al., ; Liwarska-Bizukojc et al., ). Under steady-state conditions, five parameters associated with AOB and OHOs needed to be calibrated, while under dynamic conditions, the calibration of all seven parameters associated with three groups of organisms (AOB, OHOs, and PAOs) was necessary. Note that the same parameters that were sensitive in the steady-state calibration were also sensitive in the dynamic calibration. Similar findings were obtained by other researchers (Liwarska-Bizukojc et al., ). In the steady-state simulations, there was no need to calibrate the parameters related to PAOs, whereas under dynamic conditions the additional calibration of Y PAO,aerob was required to reflect accurately the changes in the phosphorus concentration of the effluent.

#### Table 6

Comparison of the default, calibrated, and literature values of the selected parameters
 Parameter Default value Calibrated value (steady-state) Calibrated value (dynamic) Literature value (Henze et al., 2000; Bizukojc et al., 2011) AOB b aerob,A (d−1) 0.17 0.74 0.75 0.05–0.15 OHOs μ max,H (d−1) 3.2 6 5 4–8 b H (d−1) 0.62 0.275 0.275 0.1–0.62 K s (mg COD/L) 5 2.1 2.1 4 Y H (mg COD/mg COD) 0.67 0.72 0.72 0.5–0.74 Y H,anoxic (mg COD/mg COD) 0.54 – 0.21 – PAOs Y PAO,aerob (mg COD/mg COD) 0.64 – 0.50 0.5–0.625

The calibration of Y H and b H for the heterotrophic biomass was carried out based on the respirometric measurements. The obtained Y H was 0.72 mg COD/mg COD for the activated sludge from the modified AAO plant, which was slightly higher than the default value of 0.67 mg COD/mg COD and very similar to the reported values of 0.71–0.72 mg COD/mg COD (Grady et al., ). The aerobic decay rate for OHOs (b H=0.275 d−1) was lower than the default value (0.62 d−1), but remained in the range of the reference values. The calibrated value for the half-saturation constant for the heterotrophic biomass (K s) was 2.1 mg COD/L, which is much lower than either the default value (5 mg COD/L) or the published value (4 mg COD/L) (Henze et al., ). This relatively low value for K s was most likely attributable to the influent, which consisted of typical municipal wastewater containing heterotrophic biomass with a good affinity for the substrate.

The other four parameters (b aerob,A for AOB, μ maxH, Y H,anoxic for OHOs, and Y PAO,aerob for PAOs) were calibrated directly through modification of the default values. The observed maximum specific growth rate (μ maxH) was increased from the default value of 3.2 d−1 to 5 d−1, and was still within the range of μ maxH in the ASMs. Note that the calibrated optimum decay coefficient (b aerob,A) for AOB was 4.4 times that of the default value. This may be attributed to the relatively long SRT (16 d) in the BNR system, which influenced the aerobic decay of AOB. In addition, significant fractional differences between the influent in this study and the wastewaters used in other studies accounted reasonably for the discrepancies between the calibrated values and those reported in the literature (Liwarska-Bizukojc et al., ).

Based on the Si , j values (Table 5) and the calibrated parameters (Table 6), we conclude that almost all of the calibrated parameters were influential, except Y PAO,aerob. The sensitivity analysis confirmed that the model’s output was sensitive to those parameters modified from the default values, which warranted the performance of the analysis. Calibration of the Y PAO,aerob was necessary to obtain a good prediction of the TP concentration in the effluent.

### 3.5.  Validation of the calibrated model

To validate the calibrated model, we determined whether model predictions and measured values from an independent dataset were within acceptable tolerances. A simulation can be considered successful if there are no statistically significant differences between the simulated and measured values of the investigated variables (Petersen et al., ). The measured and simulated values after calibration of the selected variables in the effluent under steady-state conditions are shown in Fig. 5. Clearly, each of the simulated output variables is within the confidence interval estimated for the measured effluent pH, COD, TN, NH4 +-N, NO2 -N, NO3 -N, and TP. The calibration was therefore successful, which implies that the calibrated model can then be used to predict the general performance of the pilot plant.

Fig.5
Measured data vs. simulated values of the selected output variables in the effluent under steady-state conditions (unit: mg/L except pH)

### 3.6.  Dynamic simulation of the calibrated model

The calibrated model was used to predict the general performance of the pilot-scale modified AAO plant. Simulated and measured results are presented in Fig. 6. The measured and predicted data for TCOD, NO3 -N, TN, and TP in the effluent either overlapped or were within the range of ±20%. This indicates that the calibrated model generally tracked the effluent concentrations of the pilot plant. It should be emphasized that the aim of a dynamic calibration is not to predict each value of an individual output variable, but to predict the trend of its changes. In this respect, the performed dynamic calibration was fully successful.

Fig.6
Dynamic simulation of effluent quality: (a) TCOD; (b) NO3 -N; (c) TN; (d) TP

## 4.  Conclusions

In this work, data from a pilot-scale modified AAO plant were used in the calibration and validation of a BioWin AS model. Based on the results obtained, the following conclusions can be summarized:

1. The composition of organic matter by respirometric tests characterized the influent in this study as having relatively lower biodegradable substrates, but higher inert organic matter ratios of TCOD (S I, 8.2%–22.0%; S S, 6.0%–11.2%; X I, 60.6%–71.1%; X S, 6.9%–16.8%). The values determined for two kinetic parameters Y H and b H were 0.72 mg COD/mg COD and 0.275 d−1, respectively.

2. Sensitivity analysis is a very useful tool for identifying the most influential parameters and to guide experimental measurements in model calibration. The sensitivity analysis for the parameters of the BioWin AS model revealed that the model’s output was most sensitive to the parameters associated with the growth and decay of OHOs and AOB (Y H, μ maxH, K s, b H, μ maxA, K NH4A, b aeroa,A). Moreover, with the exception of YPAO,aerob, all the calibrated parameters were determined to be influential.

3. Successful calibration was demonstrated by the fact that none of the simulated values exceeded the confidence intervals estimated for the effluent characteristics (pH, COD, TN, NH4 +-N, NO2 -N, NO3 -N, and TP) in the steady-state simulation. In the dynamic simulations, the calibrated model was capable of generally tracking the effluent concentration, predicting the effluent quality (TCOD, NO3 -N, TN, and TP) within the range of 0–20%.

4. With the calibrated model, more scenarios can be tested to provide insight into the pilot-scale modified AAO process, as well as information needed to optimize the design and operation when applied at full-scale.

* Project supported by the National Water Pollution Control and Management of Science and Technology (No. 2011ZX07303-001), China

## References

[1] APHA, 1998. Standard Methods for the Examination of Water and Wastewater (20th Ed.), Washington DC, USA :

[2] Brun, R., Kuhni, M., Siegrist, H., 2002. Practical identifiability of ASM2d parameters-systematic selection and tuning of parameters subsets. Water Research, 36(16):4113-4127.

[3] Czerwionka, K., Makinia, J., Kaszubowska, M., 2012. Distillery wastes as external carbon sources for denitrification in municipal wastewater treatment plants. Water Science & Technology, 65(9):1583-1590.

[4] Fenu, A., Guglielmi, G., Jimenez, J., 2010. Activated sludge model (ASM) based modelling of membrane bioreactor (MBR) processes: A critical review with special regard to MBR specificities. Water Research, 44(15):4272-4294.

[5] Fu, G., Dong, B., Zhou, Z.Y., 2004. Design characteristics and operating parameters of inverted AAO process. Water & Wastewater, (in Chinese),20(9):53-55.

[6] Gernaey, K.V., van Loosdrecht, M.C.M., Henze, M., 2004. Activated sludge wastewater treatment plant modelling and simulation: state of the art. Environmental Modelling & Software, 19(9):763-783.

[7] Grady, C.P.L., Daigger, G.T., Lim, H.C., 1999.  Biological Wastewater Treatment. Marcel Dekker Inc.,New York :

[8] Henze, M., Gujer, W., Mino, T., 2000. Activated sludge models ASM1, ASM2, ASM2d and ASM3.  IWA Science and Technical Report No. 9. IWA Publishing,London :

[9] Hu, Z.R., Houweling, D., Dold, P., 2012. Biological nutrient removal in municipal wastewater treatment: new directions in sustainability. Journal of Environmental Engineering, 138(3):307-317.

[10] Langergraber, G., Rieger, L., Winkler, S., 2004. A guideline for simulation studies of wastewater treatment plants. Water Science & Technology, 50(7):131-138.

[11] Liwarska-Bizukojc, E., Biernacki, R., 2010. Identification of the most sensitive parameters in the activated sludge model implemented in BioWin software. Bioresource Technology, 101(19):7278-7285.

[12] Liwarska-Bizukojc, E., Olejnik, D., Biernacki, R., 2011. Calibration of a complex activated sludge model for the full-scale wastewater treatment plant. Bioprocess and Biosystems Engineering, 34(6):659-670.

[13] Makinia, J., Rosenwinkel, K.H., Swinarski, M., 2006. Experimental and model-based evaluation of the role of denitrifying polyphosphate accumulating organisms at two large scale WWTPs in northern Poland. Water Science & Technology, 54(8):73-81.

[14] Ni, B.J., Yu, H.Q., 2008. Simulation of heterotrophic storage and growth processes in activated sludge under aerobic conditions. Chemical Engineering Journal, 140(1-3):101-109.

[15] Ni, B.J., Xie, W.M., Liu, S.G., 2009. Modeling and simulation of the sequencing batch reactor at a full-scale municipal wastewater treatment plant. AIChE Journal, 55(8):2186-2196.

[16] Pai, T.Y., 2007. Modeling nitrite and nitrate variations in A2O process under different return oxic mixed liquid using an extended model. Process Biochemistry, 42(6):978-987.

[17] Petersen, B., Gernaey, K., Henze, M., 2002. Evaluation of an ASM1 model calibration procedure on a municipal-industrial wastewater treatment plant. Journal of Hydroinform, 4(1):15-38.

[18] Petersen, B., Gernaey, K., Henze, M., 2003. Calibration of activated sludge models: a critical review of experimental designs.  Biotechnology for the Environment: Wastewater Treatment and Modelling, Waste Gas Handling. Kluwer Academic Publishers,Dordrecht :

[19] Sin, G., van Hulle, S.W.H., de Pauw, D.J.W., 2005. A critical comparison of systematic calibration protocols for activated sludge models: a SWOT analysis. Water Research, 39(12):2459-2474.

[20] US EPA, 2009. Guidance on the Development, Evaluation and Application on Environmental Models, EPA 100/K-09-003, Washington DC, USA :

[21] Vanrolleghem, P.A., Insel, G., Petersen, B., 2003. A comprehensive model calibration procedure for activated sludge models. Proceedings of the Water Environment Federation. , 76th Annual Technical Exhibition and Conference, Los Angeles, CA, USA, 210-237. :210-237.

[22] Weijers, S.R., Vanrolleghem, P.A., 1997. A procedure for selecting best identifiable parameters in calibrating activated sludge model No. 1 to full-scale plant data. Water Science & Technology, 36(5):69-79.

[23] Zhang, B., Gao, T.Y., 2000. Principle and characteristics of reversed A2/O process. Water & Wastewater, (in Chinese),16(7):11-15.

[24] Zhou, Z., Wu, Z.C., Wang, Z.W., 2009. Fractionation of soluble COD in wastewater based on batch respirometric method. Environmental Science, (in Chinese),30(1):75-79.

[25] Zhou, Z., Wu, Z.C., Wang, Z.W., 2011. Simulation and performance evaluation of the anoxic/anaerobic/aerobic process for biological nutrient removal. Korean Journal of Chemical Engineering, 28(5):1233-1240.