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Environ Eng Res > Volume 25(2); 2020 > Article
Nga, Hiep, and Hung: Kinetic modeling of organic and nitrogen removal from domestic wastewater in a down-flow hanging sponge bioreactor

Abstract

A down-flow hanging sponge (DHS) bioreactor was operated for the treatment of domestic wastewater. The Stover-Kincannon model was applied for kinetic evaluation of the reactor performance during the operational period. As a result, the coefficient of determination (R2) for straight lines of effluent concentration from the experimental data and from the predictive data of BOD5; NH4+-N; and TN were 0.9727; 0.9883; and 0.9934, respectively. The calculation of saturation value constant (Umax - g L−1 d−1) and maximum utilization rate constant (KB - g L-1 d-1) were 56.818 and 75.034 for BOD5; 2.960 and 4.713 for NH4+-N; 2.810 and 8.37 for TN, respectively. The study suggests that Stover-Kincannon model can be used for effective evaluation of kinetic removal of BOD5; NH4+-N; and TN from domestic wastewater treated in a DHS bioreactor.

1. Introduction

In recent years, environmental pollution is one of the most serious challenges due to the population boom, industrialization, and urbanization [14]. Going together with industrial activities many toxic compounds have been discharged into the environment and have created negative impacts on public health and environment. Therefore, developing technologies for removing contaminants from wastewater has attracted remarkable attention in the world [57].
Biological treatment is the prior process to remove organic matters and nutrients in wastewater [8]. In bioreactors, microorganisms perform in two behaviors which are attached growth and suspended growth. In the attached growth process, microorganisms attach to the support materials to form biofilms [9]. The DHS reactor is one application of attached process which has many advantages such as high organic loading rate, high removal efficiency, long sludge retention time, short hydraulic retention time [1, 1012]. Therefore, many authors have been investigated this model in treating different types of wastewater [11, 1316]. Mahmoud et al. [11] applied a hybrid up-flow anaerobic sludge blanket reactor and a DHS reactor to treat domestic wastewater. They found out that this system could gain the removal values of CODtotal, CODsoluble, BOD5total, TSS and TN were 90 ± 4, 78 ± 8, 95 ± 2, 96 ± 5 and 72 ± 8%, respectively.
In addition, the DHS model was good at organic matter and nitrogen removal with OLR up to 4.8 kgCOD m−3d−1 [11]. Tawfik et al. [13] operated DHS system treating UASB reactor effluent, they demonstrated that when increasing the retention time from 1.0 to 6.0 h, sponge bulk volume from 12.9 to 51.6 liter, and decreasing sponge pored size from 1.92 to 0.56 mm the removal of fecal coliform was improved. Fleifle and colleagues researched on modeling and profile analysis of a DHS system treating agricultural wastewater with the hydraulic retention time of 2 h and organic loading rate of 3 kg COD m−3 d−1. Results showed that the average removal was 83.7% for CODtotal, 88.6% for CODsoluble, 66.7% for TKN, 85.0% for NH4+-N, and 88.9% for TSS [14]. In another investigation, DHS model was applied to treat low strength sewage at HRT of 1.5 h the reactor achieved the removal efficiency of TSS, BOD and Coliform at 90%; 85%; 98%, respectively without external aeration energy [16]. Nomoto et al. [15] studied on the performance of DHS with four layers, they demonstrated that half of the COD was removed by the first layer, organic removal followed the first order reaction equation from the second to the fourth layers. When increasing the hydraulic retention time, the removal of NH4+–N was improved [15]. These studies indicated the potential of applying DHS system in wastewater treatment. Thus, it needs to be investigated deeply in term of changing type of wastewater, operated conditions as long as kinetic modeling to make full understanding and wide application in environmental engineering.
Kinetic models have been applied to determine the trend of substrate utilization rates. These are principally nonlinear and the nonlinear regression approach is applied for calculation of kinetic constant values [17]. By using kinetic models, the experimental results can be used for estimating the performance of similar processes in the similar operational conditions [18, 19]. An understanding of the process kinetics provides a judicious basis for the design, prediction, development, and operation of processes [2022]. Kinetic models have presently used in environmental engineering for designing and optimizing the wastewater treatment. Especially, many kinetic models have developed to investigate the biodegradation of wastewater in both anaerobic processes [23, 24] and aerobic processes [2529]. Many kinetic models have been studied to determine the substrate removal rate in wastewater treatment such as First-order, Grau second-order, Monod and Stover–Kincannon [17, 18, 20]. The Stover–Kincannon model was developed by Kincannon and Stover to designate the relationship between substrate utilization rate and organic loading rate for a biofilm reactor [30]. The performance of a bioreactor can be predicted base on the kinetic constants found out from this model such as maximum utilization rate (Umax) and saturation value (KB). Therefore, the Stover–Kincannon model has been commonly applied to describe carbonaceous removal of organic matters and nutrients in wastewater treatment [1719, 31]. However, there is limited research that refers to the determination of biodegradation kinetic constants for attached growth process of the aerobic attached growth in DHS model treating domestic wastewater. Therefore, this paper presents an analytical approach of using the Stover–Kincannon model for removing of BOD, NH4+–N and TN a DHS reactor.

2. Materials and Methods

2.1. Reactor Structure and Wastewater Source

A down-flow hanging sponge bioreactor had capacity of 60 L and made by polyvinyl chloride (PVC) was operated at ambient condition. The dimensions of DHS system were 1.5 m in height and 0.2 m in width of the internal surface. The DHS module column consisted of three identical segments connected vertically in series. Air windows were located between segments for air diffusion. Each segment was filled with polyurethane Bio-Bact spheres (30% (V/V) of the segment volume). Each polyurethane Bio-Bact sphere had 36 mm diameter and contains sponge at the core. This structure could avoid the clogging and enhancing air diffusion into the sponge. The schematic diagram of the experimental set up is presented in Fig. 1. The total area of sponge and polyurethane sphere had a surface area at 3,300 m2 m−3, a density at 150 kg m−3, a void ratio at 90% [32].
The raw wastewater was collected from the storage tank of wastewater discharged from dormitory of a university. Before injecting to the reactor, wastewater was pumped into a container for primary settling of suspended solid matter. The quality of influent wastewater to the reactor for BOD5; NH4+-N; TN was in the range of 154 ± 20 (mg L−1); 40 ± 20 (mg L−1); 45 ± 10 (mg L−1), respectively.

2.2. Biofilm Forming and Acclimation

In this study, activated sludge from the secondary settling tank of a municipal wastewater treatment plant was used to be seed sludge for forming biofilm in the Bio-Bact spheres of DHS reactor. The seed sludge was diluted with tap water to achieve mix liquor suspended solids (MLSS) as at 3,000 mg L−1. This sludge solution was pumped and recycled continuously through the segments of the DHS system to create the biofilms on the sponge and spheres. After that, dormitory wastewater was injected at low organic loading rate as 0.2 kgCOD m−3 d−1 for acclimation. This stage was done when the effluent quality was stable and biofilms were uniform in the material.

2.3. Reactor Operation and Analytical Methods

After forming biofilms, the experiment was started. During the experiment, wastewater was injected into the top of the DHS model and passed through a distributor and flowed into the segments by gravity and collected at sedimentation tank. Three phases of the experiment were operated in this study corresponding to three levels of organic loading rate as 0.5; 1 and 1.5 (kg COD m−3 day−1), each level of organic loading rate levels was operated in 20–30 d with sampling duration was 81 d. The flow rate was adjusted daily to keep the design organic loading rate depending on organic concentration in the influent. The circular ratio was maintained at 1:1 enhance hydraulic retention time and removal efficiency. Samples of the influent and effluent were taken three times per week and analyzed such parameter pH, DO, BOD5, COD, NO3 N NH4+-N, TN, to evaluate the performance of the reactor. Such parameters COD, NO3 N, NH4+-N, TN, TP were analyzed in the laboratory according to APHA [33]. Biochemical oxygen demand was analyzed by using BOD-OxiDirect (AL606) AQUALYTIC, Germany [34, 35]. Other parameters such as DO, pH, and turbidity were directly tested by a Multi-Parameter Water Quality Meter, WQC-22A (Japan) [32].

2.4. Kinetic Modeling

Kinetic modeling is a significant analytical method for prediction of reactor performance. The Stover–Kincannon model considers the substance removal rate as a function of organic loading rate at steady state as in forms of Eq. (1) and Eq. (2) below [20]:
(1)
dSdt=QV(Si-Se)
(2)
dSdt=Umax(QSi/V)KB+(QSi/V)
where ds/dt is the substrate removal rate (g/L-day), Umax is the maximum utilization rate constant (g L−1 day−1), KB is the saturation value constant (g L−1 day−1), Q is the flow rate (L day−1), and V is the effective volume of the reactor (L).
The modification of Eq. (1) and Eq. (2) by in inversing of the substrate removal rate resulting the in-linearization form Eq. (3) followed:
(3)
dSdt=VQ(Si-Se)=KBUmax×VQSi+1Umax
In this equation, V/[Q(Si − Se)] and an inverse of the total loading rate V/(QS0) the linear relationship. This straight line has intercept as 1/Umax and slope as KB/Umax.
After achieving the kinetic constants Umax and KB from the straight line of V/[Q(S0 − Se)] versus V/(QS0) above and the reformation of Eq. (3), the effluent substrate concentration can be calculated at Eq. (4) below when organic loading rate and influent substrate concentration are given.
(4)
Se=SiUmaxSiKB+(QSi/V)
In this research, the Stover–Kincannon model was applied for the kinetic study of BOD5; NH4+-N; TN profile during the time course. From the experimental result, by applying this model, kinetic constants Umax and KB for those parameters were determined. This result was used to predict the effluent concentration and removal efficiency of BOD5; NH4+-N; TN.

3. Results and Discussion

3.1. Performance Evaluation Results of Operational Parameters

After the acclimation, the experiment was conducted in 81 d in which organic loading rate was increased stepwise from 0.5 to 1.5 kgCOD m−3 day−1 by adjusting the circulation ratio and decreasing hydraulic retention time. Table 2 summaries the performance results of operational parameters. The detail of reactor performance was described in our previous paper [31]. During the operational period, the pH was stable in the range of 7.0–7.3, this pH was suitable for the growth of microorganisms in bio-digester. The concentration of DO in the influent was slightly higher than that of effluent. Perhaps, the circulation of the effluent could enhance the diffusion of oxygen from the atmosphere to the DHS reactor segments. During the duration of reactor operation, the influent characteristic was affected by dormitory policy. From d 1–40, cooking was prohibited at the room therefore wastewater was almost from their personal cleaning such as bathing and washing, BOD5 concentration in this phase was in range 34–58 mg L−1. From day 41, many students graduated and moved out; the university allowed to cook inside the dormitory thus BOD5 was remarkably increased in this phase (135–151 mg L−1) even COD was not much changed. Hence, the ratio of BOD/COD was significantly increased in the later phase. The average COD concentration in the influent and effluent was 279.58 mg L−1 and 78.95 mg L−1, respectively. The maximum COD and BOD5 removal efficiency was 80% and 82.8 %, respectively. In previous studies, many authors operated bio-digesters for treatment of wastewater and showed their achieved results. Javid and colleagues operated MBBR for municipal wastewater treatment and achieved average BOD5 removal efficiency of 88% [8]. In another study, the treatment of sugar industry wastewater treatment by using moving-bed biofilm sequencing batch reactor was investigated and found out the BOD5 and COD removal efficiencies were obtained to be 85% and 79%, respectively [19]. The removal efficiency of COD and BOD5 in those authors was higher than that in the present study. It is illustrated that the different of reactor structure, wastewater type, operational conditions effected on experimental results. The average concentration of NH4+-N in the influent was varied in range 31.3–63.8 mg L−1; the average removal efficiency of ammonia nitrogen was 60%. Yang and colleagues operated biofilm reactor treating raw water obtained from eutrophicated water bodies with the influent NH4+-N in the range of 0.36–3.91 mg L−1, the average effluent NH4+-N concentration was at 0.31 ± 0.09 mg L−1, the removal efficiency of 84.0 ± 8.1% [36]. Perhaps, the lower of NH4+-N concentration in the influent and the different operational conditions resulting in higher removal ammonium nitrogen compare to the recent study. Nitrate concentration in the influent was illegible; however, its concentration in the effluent was increased in all loading rate (7.3–9.0 mg L−1), and this result indicated the nitrification process performed well in the reactor. The average of total nitrogen removal in this study was about 50%, which is not high. It can be explained that the nitrogen in the influent underwent the reactor only change the form throughout the nitrification process some parts of nitrogen were used for forming biomass of microorganisms in the assimilation process. Based on the structure of reactor and operational conditions, it can be consider that the main mechanisms of organic and nitrogen removal in this research was by aerobic conversion. Organic matters in different forms were underwent assimilation and catabolism. As results, those compounds from wastewater were mainly converted to biomass, carbon dioxide; the untreated portion was presented in the effluent. Ammonia nitrogen was converted to nitrite and then nitrate through the nitrification process.Table 1

3.2. Kinetic of Nutrient Removal

3.2.1. Kinetic of BOD removal

The result of linear relationship plotting between V/[Q(Si − Se)] and V/QSi for BOD profile derived from the modified Stover–Kincannon model equation is shown in Fig. 2(a). The high value of correlation coefficient values (R2 = 0.9928) indicates a good agreement between the prediction and the experimental data for DHS reactors. Thus, it could be considered that the modified Stover–Kincannon model is capable in describing the performance of the BOD removal used in this study. Kinetic constant KB and Umax were calculated as 75.034 and 56.818 g L−1 day−1, respectively. Rate expression for the BOD takes the forms below, Eq. (5)
(5)
Q(Si-Se)V=56.818(QSi/V)75.034+(QSi/V)
The relationship between predicted and observed effluent BOD concentration in DHS reactor is shown in Fig. 2b. It illustrates that there is a linear relationship between the observed and predicted effluent BOD concentration with R2 = 0.9727 regression coefficient. Thus, kinetic constants can be used in predicting effluent BOD concentration of DHS reactor. By reforming the Eq. (5), the prediction of effluent BOD concentration is determined by Eq. (5-1), and the prediction of removal efficiency can be given in Eq. (5-2).
(5-1)
Se=56.8181Si75.034+(QSi/V)
(5-2)
E=56.81875.034+(QSi/V)
According to Eq. (5-2), the predicted result of BOD removal by employing Stover-Kincannon model was over 70%. Comparing the maximum BOD removal from experiment and maximum BOD removal from kinetic models, they are highly correlated. From the previous studied, Faridnasr et al. [19] investigated the kinetic modeling for treatment of sugar-industry wastewater treatment by using a moving-bed biofilm sequencing batch reactor (MBSBR). The result showed that, modified Stover-Kincannon model equation on removal of BOD5 at concentration 500 mg L−1 had R2 = 0.9998; Umax = 16.690 gBOD5 L−1 d−1 and KB = 16.631 gBOD5 L−1 d−1. Those values of Umax and KB were lower than Umax and KB found in this study indicated that the DHS has an immense potential towards BOD removal. These contradictory results could be due to the effect of different operational conditions and different reactor structures. Several previous studies indicated the results of the modified Stover-Kincannon model application on COD removal. Abyar et al. [17] operated an up-flow anoxic/aerobic sludge bioreactor (UAASB) and achieved the correlation coefficient (R2) as 0.9917 and other kinetic constants as KB = 25.997 gCOD L1 d1and Umax = 24.75 gCOD L1 d1. Hassani et al. [37] used a moving bed biofilm reactor (MBBR) treating wastewater containing ethylene glycol, kinetic modeling for removal of COD, the results showed that the modified Stover–Kincannon model was matched with experimental data (R2 = 0.9919), Umax and KB were calculated as 13.62 g COD L1 d1 and 13.14 g COD L1 d1, respectively. Kapdan [20] studied on dyestuff and COD removal of synthetic wastewater. In the result, experimental data was suitable with Modified Stover–Kincannon model and they found out some kinetic constants for dyestuff and COD were KB = 17.8 g COD L1 d1, Umax = 19.5 g COD L1 d1, and KB = 37.9 g COD L1 d1, Umax = 12.9 g COD L1 d1, respectively. The variance between the mean kinetic constants among researches indicates that reactor configuration and operational conditions can have a great influence on the value of kinetic coefficients. In addition, the relationship between influent/initial concentration and effluent/equilibrium concentration have been developed by many authors [38, 39]. The other models such as Grau second-order model; Monod model; First order model; Sum-Kinetic model have been applied for kinetic modeling pollutants removal and provided significant results for each case study [29, 4042].

3.2.2. Kinetic of ammonium nitrogen removal

The application of modified Stover-Kincannon model for simulating of ammonium removal is shown in Fig. 3(a). When V/[Q(Si-Se)] is plotted against V/(QSi), KB/Umax is the slope and 1/Umax is the intercept point. From the slope and intercept of Fig. 3(a), kinetic constant KB and Umax values were calculated as 4.713 g L−1 day−1 and 2.96 g L−1 day−1, respectively. The correlation coefficient is 0.9991, which considered fairly good precision with the data obtained, confirming the applicability of the modified Stover-Kincannon model. In this study, the saturation constant (KB) and maximum utilization rate (Umax) values are larger than those obtained by Yang and colleagues in a Stover–Kincannon model [43]. Abbas et al. [44] investigated partial nitrification and anaerobic ammonia oxidation of synthetic wastewater containing NH4+, they obtained KB = 27.253 g L1 d1 and Umax = 22.29 g L1 d1 (R2 = 0.9810) when applied Stover–Kincannon model for collected data [44].
As a result, the rate expression for NH4+-N removal takes the following from Eq. (6)
(6)
Q(Si-Se)V=2.96(QSi/V)4.713+(QSi/V)
The relationship between predicted and observed effluent NH4+-N concentration in DHS reactor is shown in Fig. 3(b). The Eq. (6) is reformed to calculate the effluent NH4+-N concentration in Eq. (6-1). Also, the predicted result of NH4+-N removal by employing Stover-Kincannon model was over 57% according to Eq. (6-2).
(6-1)
Se=Si-2.961Si4.713+(QSi/V)
(6-2)
E=2.964.713+(QSi/V)
Comparing the maximum NH4+-N removal from experiment and maximum NH4+-N removal from kinetic models, they are similar. This result demonstrates a high correlation between the actual experimental data and the model data. There have not many publishes described about the using of Stover–Kincannon model for investigation of NH4+-N removal in bioreactors.

3.2.3. Kinetic of total nitrogen removal

Fig. 4(a) illustrates the straight relationship between V/[Q(Si-Se)] and V/(QSi). The high value of correlation coefficient values (R2 = 0.9903) demonstrates a significant experimental result to calculate the value of kinetic constants in order to predict the trend of the treatment system. From this result, the saturation constant (KB) and the maximum utilization rate (Umax), the rate constant in modified Stover-Kincannon model, were found to be 8.37 g L−1 day−1 and 2.81 g L−1 day−1, respectively. In this study, the KB and Umax values were lower than those published in 2012 by Akhbari and colleagues [45], but the correlation coefficient (R2) was higher. Ni et al. [46] applied the modified Stover–Kincannon model to simulate the nitrogen removal process of the UASB. The values of KB and Umax constants were calculated as 12.1 g L1 d1 and 11.4 g L1 d1, respectively, with the correlation coefficient is 0.9990. By using this model, Tomar et al. [47] investigated the nitrogen removal by an anammox hybrid reactor, kinetic constant of Umax and Kb were calculated as 45.045 and 47.072 g L1 d1, respectively. On the other hand, in this study, KB and Umax values were higher than those of Vandith and colleagues [48]. In another study, Modified Stover Kincannon model was applied for kinetic evaluating of UASB-anammox in total nitrogen removal the calculation of Umax and KB were like 3.33 and 4.03, g L1 d1, respectively [49]. This implies that the hybrid reactor configuration has animmense potential towards nitrogen removal. The relationship between predicted and observed effluent TN concentration in DHS reactor is shown in Fig. 4(b). The effluent TN concentration can then be predicted by using Eq. (7). Furthermore, the modified Stover–Kincannon model was developed to predict the efficiency of TN removal. The formula is given in Eq. (8)
(7)
Se=Si-2.81Si8.37+(QSi/V)
(8)
E=2.818.37+(QSi/V)

4. Conclusions

In the present research, a down-flow hanging sponge bioreactor was operated for the treatment of domestic wastewater. The reactor was performed stably during the experimental duration. The kinetic modeling of BOD5; NH4+-N; and TN removal was investigated by using Stover–Kincannon model. The results of this study demonstrated that the Stover–Kincannon model fits well for estimating of kinetic coefficients indicated at a high value of the coefficient of determination. From these coefficients, the prediction of removal efficiency was 70% for BOD5; 57% for NH4+-N and 33% for TN. In conclusion, it is suitable to undertake a nonlinear regression technique using of kinetic coefficients of Stover–Kincannon model for predicting the performance of down-flow hanging sponge bioreactor.

Acknowledgments

The authors would like to express their sincerest thanks to Vietnam Ministry of Natural resource and Environment for financial support; Ho Chi Minh City University of Natural resource and Environment, Nong Lam University – Ho Chi Minh City for accommodation the experimental facilities.

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Fig. 1
The schematic diagram of a DHS bioreactor.
/upload/thumbnails/eer-2018-390f1.gif
Fig. 2
The kinetic modeling of BOD5 removal. (a) Modified Stover-Kincannon model plot for BOD5 removal, (b) Relationship between observed and predicted effluent BOD5 concentrations.
/upload/thumbnails/eer-2018-390f2.gif
Fig. 3
The kinetic modeling of NH4+-N removal. (a) Modified Stover-Kinconnon model plot for NH4+-N removal, (b) Relationship between observed and predicted effluent.
/upload/thumbnails/eer-2018-390f3.gif
Fig. 4
The kinetic modeling of NH4+-N removal. (a) Modified Stover-Kincannon model for TN removal in DHS reactor, (b) Relationship between observed and predicted effluent
/upload/thumbnails/eer-2018-390f4.gif
Table 1
Summary of the DHS Bioreactor Performance at Different Organic Loading Rates
Parameter OLR1
0.5 kgCOD m−3 day−1
OLR2
1 kgCOD m−3 day−1
OLR3
1.5 kgCOD m−3 day−1



Influent Effluent Removal efficiency (%) Influent Effluent Removal efficiency (%) Influent Effluent Removal efficiency (%)
pH 7.3±0.2 7.0±0.2 - 7.2±0.2 7.1±0.2 - 7.3±0.1 7.1±0.1 -
COD (mg L−1) 276.8±52.6 73.3±19.2 72.1±11 289.2±37.2 64.5±3.2 77.4±2.2 275.4±55.4 91.2±28.7 67.2±7.1
BOD5 (mg L−1) 50.7±9.2 11.2±1.3 77.4±4.2 72.8±38.3 18.7±15.4 76.4±4.7 141.4±4.5 41.8±4.2 70.5±2.3
TSS (mg L−1) 40±10 20±10 43.4±17.7 50±10 20±10 62±13.2 60±10 20±10 62±13.2
NH4+N (mg L−1) 51.4±18.8 19.7±7.2 61.6±0.5 31.3±1.3 12±0.9 61.6±1.3 63.8±5.9 27.2±2.1 57.2±1.6
NO3 (mg L−1) 0.2±0.1 8.6±1.1 NA 0.1±0 7.3±0.5 NA 0.2±0.1 9.0±0.2 NA
TN 53.5±18.8 36.8±13.7 46.8±4.4 33.3±1.4 22±1.3 51.1±3.4 65.9±5.9 44.2±3.9 49±1.7
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