Nitrogen Removal Comparison in Porous Ceramic Media Packed-Bed Reactors by a Consecutive Nitrification and Denitrification Process
Nitrogen Removal Comparison in Porous Ceramic Media Packed-Bed Reactors by a Consecutive Nitrification and Denitrification Process
Environmental Engineering Research. 2011. Dec, 16(4): 231-236
Copyright ©2011, Korean Society of Environmental Engineering
This is an Open Access article distributed under the terms of the Creative Commons Attribution Non-Commercial License ( which permits unrestricted non-commercial use, distribution, and reproduction in any medium, provided the original work is properly cited.
  • Received : September 11, 2010
  • Accepted : December 02, 2011
  • Published : December 31, 2011
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Gee-Bong, Han
Mi-Hee, Woo

Biological nitrogen removal, using a continuous flow packed-bed reactor (CPBR) in a consecutive nitrification and denitrification process, was evaluated. An apparent decline in the nitrification efficiency coincided with the steady increase in NH 4 + -N load. Sustained nitrification efficiency was found to be higher at longer empty bed contact times (EBCTs). The relationship between the rate of alkalinity consumption and NH 4 + -N utilization ratio followed zero-order reaction kinetics. The heterotrophic denitrification rate at a carbon-to-nitrogen (C/N) ratio of >4 was found to be >74%. This rate was higher by a factor of 8.5 or 8.9 for NO 3 -N/volatile solids (VS)/day or NO 3 -N/m 3 ceramic media/day, respectively, relative to the rates measured at a C/N ratio of 1.1. Autotrophic denitrification efficiencies were 80–90%. It corresponds to an average denitrification rate of 0.96 kg NO 3 -N/m 3 ceramic media/day and a relevant average denitrification rate of 0.28 g NO 3 -N/g VS/day, were also obtained. Results presented here also constitute the usability of an innovative porous sulfur ceramic media. This enhanced the dissolution rate of elemental sulfur via a higher contact surface area.
1. Introduction
Organics in wastewater are usually removed by an activated sludge process. This is a standard conventional wastewater treat-ment technology. Nutrients including nitrogen and phosphorus are also required to be removed from the effluent of wastewater treatment plants [1 , 2] . Generally, at high levels of concentration these nutrients cause eutrophication and toxic effects to the wa-ter environment. So as a result, removal of these nutrients from wastewater is often the primary objective in wastewater treat-ment around the world [3 - 6] .
One of the most economical and effective processes for ni-trogen removal at wastewater treatment plants is the introduc-tion of biological nitrification with a subsequent denitrification process [7] . Microbial nitrogen removal involves aerobic nitrifi-cation, oxidizing NH 4 + -N to NO 3 -N, followed by anoxic denitri-fication, which reduces NO 3 -N to gaseous nitrogen. During the nitrification process, the oxidation of NH 4 + -N to NO 3 -N is con-ducted by various bacteria groups. Two different bacteria groups were earlier recognized namely: Nitrosomonas , which converts ammonia to nitrite; and Nitrobacter , which oxidizes nitrites to nitrates [8] .
Recent studies on advanced treatment technologies have fo-cused on the development of economical and effective methods for nitrogen removal. They focus especially on heterotrophic denitrification, such as simultaneous partial nitrification and denitrification or simultaneous nitrification-denitrification in a membrane system for shortcut nitrification-denitrification [9 - 11] . However, these denitrification systems are challenging to operate due to the required complex reaction conditions. Moreover, construction of such systems is generally expensive for commercial applications. Therefore, these technologies will not be widely adopted unless more incentives are introduced to compensate for these weaknesses.
Immobilization can retain bacteria for an extended time in a continuous flow. Thus, the utilization of a fixed biofilm can en-hance the reduction of the nitrifying bacteria loss due to wash away [12 , 13] . Attached growth in a fixed biofilm is a more fa-vored method for wastewater treatment than the usage of a suspended growth process. Biofilms have a buffering capacity to prevent shock loading due to a high density of bacteria and produce small amounts of residual sludge [14] .
The rate of ammonia oxidation is strongly influenced by the nature of the nitrifying cultures. It is also influenced by a vari-ety of environmental factors, including substrate concentration, temperature, dissolved oxygen, and pH [15] . Attached growth in a fixed biofilm provides some protection against temperature or toxic shock [16 , 17] . Generally, porous ceramic media have high porosity ratio, superior durability, high specific surface area, and abundance for attachment of microorganisms. Compared to non-porous media [18] , porous media used is better for organic removal. One of the most significant parameters for attached slow-growing autotrophic bacteria can be the selection of the supporting media because the characteristics of the supporting media for biofilms can significantly influence reactor perfor-mance [19] .
Heterotrophic bacteria denitrify using NO 3 -N as electron ac-ceptor with the addition of organics as external carbon sources. But, autotrophic bacteria requires inorganics in the denitrifi-cation process instead of organics, as external carbon sources [20 , 21] . Thus, when a low carbon-to-nitrogen (C/N) ratio is favorable, autotrophic denitrification can occur. Conventional ceramic media are typically prepared from clay obtained from soil. Specific chemical compounds can also be included as an electron donor to produce new supporting media, such as sulfur ceramic media, for autotrophic denitrification.
In this study, experiments were carried out in a continuous flow packed-bed reactor (CPBR) to 1) evaluate the nitrification efficiency with respect to alkalinity consumption; 2) compare the effectiveness of denitrification between heterotrophic and autotrophic reaction; and 3) test the feasible porous sulfur ce-ramic media.
2. Materials and Methods
- 2.1. Process and Instrumentation for CPBR System
In this study, three packed-bed reactors were used to com-pare the nitrogen removal efficiencies of biofilms attached to porous ceramic media. A schematic diagram of CPBR system is shown in Fig. 1 (a). These packed-bed reactors were designed to evaluate the nitrogen removal efficiencies using porous ceramic media. The CPBR system consisted of consecutive nitrification and denitrification processes (heterotrophic and autotrophic conditions). The working volumes of each CPBR for nitrification (110 mm ¢ × 950 mm/hr), heterotrophic denitrification (80 mm ¢ × 750 mm/hr), and autotrophic denitrification (80 mm ¢ × 750 mm/hr) were 7.60, 3.02, and 3.02 L, respectively. The nitrification CPBR was aerated to supply oxygen concentrations of around 2.0–3.5 mg/L.
In this study, all CPBRs are packed with porous ceramic me-dia (60% v/v) as a support for biofilm growth. They were fed con-tinuously in the up-flow mode with by using peristaltic pumps. The ceramic media used in this experiment composed of clay. It contained an abundance of small pores. These pores provide sufficient surface area for a physically stable environment for microorganism growth. The ceramic media packed for auto-trophic denitrification CPBR contained 35% of elemental sulfur as the electron donor. The specifications of the porous ceramic media were as follows: 8–9 mm diameter, 0.7–0.8 g/cm 3 appar-ent density, 55.8% porosity, 70–100 μm pore size, 0.42 cm 3 /g pore volume, 0.47 m 2 /g surface area, 0.47–0.57 m 2 /m 3 specific surface area, 1.0–1.2 specific gravity [22] . A simplified flow chart of man-ufacturing sulfur ceramic media is depicted in Fig. 1 (b).
- 2.2. CPBR System Operation
The synthetic wastewater was fed to the nitrification CPBR. It contained NH 4 Cl 157–764 mg/L, NaHCO 3 335–1,344 mg/L,
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Schematic diagrams for (a) continuous flow packed-bed re-actors (CPBR) system and (b) manufacturing sulfur ceramic media.
NaH 2 PO 4 ·2H 2 O 6 mg/L , MgCl 2 ·6H 2 O 15 mg/L, KCl 35 mg/L. 1 mL/L of the stock trace element solution was also included in the synthetic wastewater. The stock trace element solution composed of: ZnCl 2 45 mg/L , MnCl 2 ·4H 2 O 450 mg/L, (NH 4 ) 6 Mo 7 O 24 ·4H 2 O 80 mg/L, Na 2 SeO 3 ·5H 2 O 90 mg/L, and NiCl 2 ·6H 2 O 45 mg/L. 50 mg of NH 4 + -N/L as NH 4 Cl of the synthetic wastewater was initially supplemented. Then, it was increased to about 200 mg of NH 4 + -N/L stepwise as the experiment proceeded. The composition of the synthetic wastewater was chosen from previously reported wastewater compositions [23 , 24] . The influent flow rate was in the range of 21.6–30.48 L/day. The empty bed contact time(EBCT) was also in the range of 6 to 8 hr. All experiments were conducted at 20 to 28±1℃ and they were buffered at pH 7.5–8.5.
The C/N ratio for heterotrophic denitrification CPBRs was adjusted by adding 0.75 to 5.2 of methanol as an external carbon source, whenever necessary. As a result, ceramic volumetric or-ganic loading rate of 0.2–5.6 kg COD/m 3 ceramic media/day was applied to determine the influence of organic load on denitrifi-cation. The influent was supplied at a flow rate of 0.86 L/hr, with an average nitrogen concentration of 87 mg NO 3 -N/L, and an EBCT of 3.5 hr. The pH was adjusted to 7.5.
The autotrophic denitrification CPBR was fed with 85 mg NO 3 -N/L influent. During the experiment, the EBCT was varied in the range of 4.6 to 7.6 hr. The volumetric loading rate therefore varied over the range of 0.83–1.37 kg NO 3 -N/m 3 ceramic me-dia/day , and the alkalinity was increased to 400 mg CaCO 3 /L through additions of NaHCO 3 , when required. The ceramic me-dia containing elemental sulfur served as an energy substrate (electron donor) as well as a physical support for Thiobacillus denitrificans .
The detachment of biomass is caused by the up-flow of air bubbles and hydraulic shearing. This occurs during the 100% internal recycling process in CPBRs eliminated excess biomass without outside intervention. As a result, reactor backwashing was not necessary due to the biomass self-washing process. Many studies have reported that the accumulation of biomass depends on the packing material, void fraction, and shear forces associated with the hydraulic conditions. But, the biomass self-washing process was mainly dependent on the size of the pack-ing material [25 - 27] .
- 2.3. Inoculation of Biomass for Start-up and Enrichment of Thiobacillus denitrificans
The seed sludge mixture consisting of initial biomass con-centrations (mixed liquor suspended solids, MLSS) of 5,800 mg MLSS/L and sludge volume index (SVI), 75 mL/g was obtained from the Gulpocheon Advanced Sewage Treatment Plant in Gyeonggi-do, Korea. The nitrification CPBR packed with po-rous ceramic media was inoculated with concentrated activated sludge. The new seed sludge contains initial biomass concentra-tions of 6,350 mg MLSS/L and 89 mL/g SVI was also added to supply the washed-out sludge in the reactor. Cultures of Thioba-cillus denitrificans were isolated in a mineral medium containing Na 2 S 2 O 3 ·5H 2 O (4 g/L), K 2 HPO 4 (1.5 g/L), KNO 3 (1.5 g/L), NaHCO 3 (0.8 g/L), NH 4 Cl (0.4 g/L), MgCl 2 ·7H 2 O (0.4 g/L), FeSO 2 ·7H 2 O (0.01 g/L) and incubated at 28℃. By following the previous studies, they were cultivated [24] . The enriched cultures were introduced into the denitrification CPBR for autotrophic denitrification us-ing sulfur as an electron donor. Based on the previous studies compositions of mineral medium were chosen [24] .
- 2.4. Analytical Methods
Biochemical oxygen demand (BOD), chemical oxygen de-mand (COD), NH 4 + -N, and total Kjeldahl nitrogen (TKN) were determined in accordance with the Standard Methods, USA [28] . The ionic concentrations of nitrite (NO 2 ) and nitrate (NO 3 ) were determined by ionic chromatography using a DIONEX model DX 100 (Dionex, Sunnyvale, CA, USA) which is equipped with a DIONEX AS-14 (4 x 25 mm) column. The liquid samples were analyzed after filtration through a 0.45 μm glass fiber filter. Al-kalinity was measured using a spectrophotometer (DR4000; HACH, Loveland, CO, USA). The dissolved oxygen (DO) concen-tration was determined using a DO meter (YSI 58; YSI Inc., Yellow Springs, OH, USA). The pH of the solution was measured using a pH meter (Orion-3STAR, Thermo Scientific Inc., Waltham, MA, USA).
The amount of accumulated biomass was estimated by fol-lowing the total solids (TS) and the total volatile solids (TVS) measurement methods [28] . Samples of the porous ceramic me-dia were taken from the CPBR, dried at 105℃, burned at 550℃ and 1,200℃, then weighed. The VS was deduced by subtracting the difference in dry weights at 550℃ and 1,200℃ from the dif-ference in dry weights at 105℃ and 1,200℃.
3. Results and Discussion
- 3.1. Efficiency in the Nitrification CPBR
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Influence of NH4+-N loading rate on nitrification efficiency at an empty bed contact time (EBCT) of (a) 6 hr and (b) 8 hr.
The system was monitored on a daily basis for 43 days. NH 4 + -N in the influent was increased stepwise from 50 to 200 mg/L, yielding a relevant ceramic volumetric nitrogen loading rate of about 0.45–2.40 kg NH 4 + -N/m 3 ceramic media/day with an inter-nal recirculation rate of 100%. The NH 4 + -N loading rate was one of the factors which was affecting the nitrification rate in CPBRs. The nitrification efficiency of EBCTs of 6 and 8 hr, is shown in Figs. 2 (a) and 3 (b), respectively. The average biomass of 9.2 ± 1.0 gVS/m 3 ceramic media was obtained in the nitrification CPBR.
At an EBCT of 6 hr, the influent NH 4 + -N concentration was raised stepwise from 50 to 200 mg/L. It is shown in Fig. 2 (a). The nitrification efficiency was obtained to be 89–74% with the NH 4 + -N utilization rate of 0.08–0.16 g/g VS/day. However, the nitrifica-tion efficiency decreased to the range of 71–59% with 0.24–0.31 g NH 4 + -N/g VS/day. As a result, the nitrification efficiency was found to be in the range of 59–89% with the volumetric nitrogen loading rate of about 0.6–2.4 kg NH 4 + -N/m 3 ceramic media/day, and with the NH 4 + -N utilization rate of around 0.08–0.31 g/g VS/day, respectively.
At an EBCT of 8 hr, the influent NH 4 + -N concentration was raised stepwise from 50 to 200 mg/L. It is shown in Fig. 2 (b). The average nitrification efficiency was obtained to be 80.8% when the volumetric influent NH 4 + -N loading rate was increased step-wise from 0.45 to 1.8 kg NH 4 + -N/m 3 ceramic media/day. How-ever, the nitrification efficiency fluctuated between 78% and 69% as the influent NH 4 + -N loading rate increased above 1.35 kg NH 4 + -N/m 3 ceramic media/day, with the NH 4 + -N utilization rate of 0.18 g/g VS/day. As a result, the nitrification efficiency decreased from an average of 89.4% to the level of 80.8%. This occurred when the volumetric nitrogen loading rate increased stepwise from 0.45 to 1.8 kg NH 4 + -N/m 3 ceramic media/day, with the NH 4 + -N utilization rate in the range 0.06–0.24 g/g VS/day.
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Linear relationship plot for alkalinity consumption rate vs. the NH4+-N utilization rate. EBCT: empty bed contact time VS: vola-tile solids.
As a result, the reduction of nitrification efficiency depended on the increase of the NH 4 + -N loading throughout the test pe-riod. The nitrification efficiency maintained a higher level at lon-ger EBCTs. Thereby, it has more significant effect to the micro-bial nitrification reaction rate instead of NH 4 + -N concentration. The nitrification rate by NH 4 + -N oxidized/m 3 ceramic media/day decreased as the system NH 4 + -N concentration increased. The calculated nitrification rates were midrange with respect to the rates reported by other investigators [29 , 30] .
- 3.2. Alkalinity Consumption
Alkalinity was consumed due to the production of acids (HNO 2 , HNO 3 ) during ammonium oxidation. Alkalinity con-sumption affected both the pH and nitrification rate, but it can be remedied by increasing the available alkalinity. The relation-ship between the alkalinity consumption rate and the NH 4 + -N utilization rate at EBCTs of 6 and 8 hr are shown in Fig. 3 . These relationships were obtained to be R 2 = 0.78 and 0.86. They indi-cate that the rate of alkalinity consumption against the NH 4 + -N utilization rate follows zero-order reaction kinetics. As shown in Fig. 3 , the alkalinity consumption rate was found to be higher at an EBCT of 8 hr than at an EBCT of 6 hr, even though the NH 4 + -N utilization rate was the same. The maximum alkalinity consump-tion rate was found to be 6.08 g/L as CaCO 3 at a nitrification rate of 0.24 kg NH 4 + -N/VS/day. This was equivalent to 6.08 kg/m 3 as CaCO 3 consumed at a nitrification rate of 1.26 kg NH 4 + -N/m 3 ce-ramic media/day. The stoichiometric alkalinity required for ni-trification was 7.07 g as CaCO 3 /g N, is presented in Equation (1).
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Therefore, the theoretical value for alkalinity consumption at a nitrification rate of 1.26 kg NH 4 + -N/m 3 ceramic media/day was 8.91 kg as CaCO 3 /m 3 , but smaller quantities of alkalinity were consumed during the test period. Nitrifying bacteria grow slowly. The optimum EBCTs were 8 and 10 hr for Nitrosomonas and Ni-trobacter , respectively. It was reported previously [31] .
- 3.3. Heterotrophic Denitrification as a Function of the C/N Ratio
During the denitrification test period, an average of 87 mg NO 3 -N/L and an EBCT of 3.5 hr were applied with varying C/N ratio. The heterotrophic denitrification rate, in terms of nitrate
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Denitrification efficiencies at various carbon-to-nitrogen (C/N) ratio. VSS: volatile suspended solid.
loading to VS and ceramic media volume, under various C/N ra-tios, is shown in Fig. 4 .
When the C/N ratio was varied from 1.1 to 2.5, the denitrifica-tion rate was found to vary from 1.0 g NO 3 -N/g VS/day. This was corresponding to 0.15 kg NO 3 -N/m 3 ceramic media/day, to 2.20 g NO 3 -N/g VS/day, corresponding to 0.56 kg NO 3 -N/m 3 ceramic media/day. In this range, the average calculated denitrification rate was 1.68 g NO 3 -N/g VS/day, 0.32 kg NO 3 -N/m 3 ceramic me-dia/day , which was comparable to or higher than the previously reported denitrification rates, 0.240–0.480, 0.158, and 0.043 kg NO 3 -N/m 3 /day, for the same carbon source [32 - 34] . When the C/N ratio was above 4, the average denitrification rate increased to 8.49 g NO 3 -N/g VS/day, 1.33 kg NO 3 -N/m 3 ceramic media/day. Hamlin et al. [35] Regardless of the carbon source used (methanol, acetic acid, molasses, or hydrolyzed starch), reported a maximum daily denitrification rate for biofilms was around 0.67–0.68 kg nitrogen removed/m 3 media/day. Therefore, our CPBR system showed a denitrification rate for biofilms accumu-lated on porous ceramic media that was higher by a factor of two relative to the rate reported in a previous study [35] .
The denitrification rate is measured as a function of the ni-trate reduction (g NO 3 -N/g VS/day and kg NO 3 -N/m 3 ceramic media/day). It is increased from 8.5 and 8.9 as C/N ratios were raised from 1.1 to >4, respectively. Under the maximum nitrate loading to ceramic media volume of 1.8 kg NO 3 -N/m 3 ceramic media/day, the highest average denitrification rate was found to be 1.33 kg NO 3 -N/m 3 ceramic media/day. Thus, if the C/N ratio was raised above 4, the denitrification efficiency was measured at 74%, with sufficient organic content for denitrification. No previous reports have given denitrification rates in units of both g NO 3 -N/g VS/day and kg NO 3 -N/m 3 ceramic media/day for a single system.
- 3.4. Autotrophic Denitrification in the CPBR Packed with Porous Ceramic Sulfur Media
The autotrophic denitrification efficiency and NO 3 -N con-centration profiles for CPBR packed with porous ceramic sulfur media for varying EBCTs are illustrated in Fig. 5 . An average of 84 NO 3 -N mg/L was fed to the autotrophic denitrification CPBR under an EBCT in the range of 4.5–7.5 hr, corresponding to a NO 3 -N load of 0.84–1.38 kg NO 3 -N/m 3 ceramic media/day.
During the test period, autotrophic denitrification efficiency and the levels of NO 3 -N in the effluent of autotrophic denitri-fication CPBR were found to be in the range of 80–90% and 3.6–7.7 mg NO 3 -N/L, respectively. Thus, the average denitrification
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NO3-N concentration and denitrification efficiency at several empty bed contact times (EBCTs).
rates were obtained to be 0.96 kg NO 3 -N/m 3 ceramic media/day and 0.28 g NO 3 -N/g VS/day. Some researchers [24 , 36] re-ported a maximum specific denitrification rates using NO 3 -N as an electron donor were 0.15 g NO 3 -N/g VSS/day in laboratory-scale batch test and 0.1–0.2 g NO 3 -N/g VSS/day in a suspended growth system. The stoichiometric autotrophic denitrification rate with sulfur as an electron donor is presented in Equation (2).
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In this study, the maximum autotrophic denitrification rate was resulted twice the rate reported by previous studies [24 , 36] .
Usage of sulfur particles as an electron donor for autotrophic denitrification was restricted due to the decrease in the diam-eter of sulfur particles. Because the contact between NO 3 -N and Thiobacillus denitrificans was limited, the denitrification efficiency was also reduced [37] . The slow dissolution rate of el-emental sulfur is also one of the limiting factors to be used as sole electron donor. In this study, the dissolution rate of elemen-tal sulfur was enhanced by the use of a porous sulfur ceramic media, which contained 30% elemental sulfur and an increased contact surface area. Thus, the autotrophic denitrification rate was improved relative to the previous studies [24 , 36] .
4. Conclusions
The NH 4 + -N loading rate is a key influencing factor for the ni-trification rate in CPBRs. The nitrification efficiency was found to be in the range of 59–89% with the volumetric nitrogen load-ing rate of about 0.6–2.4 kg NH 4 + -N/m 3 ceramic media/day, and with the NH 4 + -N utilization rate of about 0.08–0.31 g/g VS/day, respectively. The nitrification efficiency decreased from an aver-age of 89.4%, but it sustained to an average of 80.8%, when the volumetric nitrogen loading rate was increased stepwise from 0.45 to 1.8 kg NH 4 + -N/m 3 ceramic media/day, with the NH 4 + -N utilization rate in the range of 0.06–0.24 g/g VS/day, respectively, at an EBCT of 8 hr.
The alkalinity consumption rate was found to be higher at an EBCT of 8 hr than at an EBCT of 6 hr. Therefore, the nitrifica-tion efficiency was more affected by EBCT than by the volumet-ric loading with NH 4 + -N concentration, even though the NH 4 + -N utilization rate was the same.
When the C/N ratio was raised from 1.1 to >4, the hetero-trophic denitrification rate was increased by a factor of 8.5 or 8.9 for the NO 3 -N/g VS/day or NO 3 -N/m 3 ceramic media/day measurements, respectively. The highest average denitrification rate of 1.33 kg NO 3 -N/m 3 ceramic media/day was obtained for a maximum nitrate loading to ceramic media volume of about 1.8 kg NO 3 -N/m 3 ceramic media/day. Thus, a denitrification ef-ficiency of >74% was achieved with sufficient organic content at a C/N ratio of >4.
Autotrophic denitrification efficiencies of 80–90%, corre-sponding to an average denitrification rate of 0.96 kg NO 3 -N/m 3 ceramic media/day and 0.28 g NO 3 -N/g VS/day, were obtained during the test period. Thus, the levels of NO 3 -N in the effluent of the autotrophic denitrification CPBR ranged from 3.6 to 7.7 mg NO 3 -N/L. The porous sulfur ceramic media enhanced the dissolution rate of elemental sulfur through an increased contact surface area. It also raised the autotrophic denitrification rate.
This study was supported by the Research Fund, 2010 of The Catholic University of Korea.
Kim Hs , Gellner JW , Boltz JP , Freudenberg RG , Gunsch CK , Schuler AJ 2010 Effects of integrated fixed film activated sludge media on activated sludge settling in biological nutrient re-moval systems. Water Res. 44 1553 - 1561    DOI : 10.1016/j.watres.2009.11.001
Kim D , Kim KY , Ryu HD , Min KK , Lee SI 2009 Long term operation of pilot-scale biological nutrient removal process in treating municipal wastewater. Bioresour. Technol. 100 3180 - 3184    DOI : 10.1016/j.biortech.2009.01.062
Rajesh Banu J , Uan DK , Yeom IT 2009 Nutrient removal in an A2O-MBR reactor with sludge reduction. Bioresour. Technol. 100 3820 - 3824    DOI : 10.1016/j.biortech.2008.12.054
Fu Z , Yang F , Zhou F , Xue Y 2008 Control of COD/N ratio for nu-trient removal in a modified membrane bioreactor (MBR) treating high strength wastewater. Bioresour. Technol. 100 136 - 141
Ma Y , Peng Y , Wang X 2009 Improving nutrient removal of the AAO process by an influent bypass flow by denitrifying phospho-rus removal. Desalination 246 534 - 544    DOI : 10.1016/j.desal.2008.04.061
Zhang H , Wang X , Xiao J , Yang F , Zhang J 2009 Enhanced biologi-cal nutrient removal using MUCT-MBR system. Bioresour. Technol. 100 1048 - 1054    DOI : 10.1016/j.biortech.2008.07.045
Ahn YH 2006 Sustainable nitrogen elimination biotechnologies: a review. Process Biochem. 41 1709 - 1721    DOI : 10.1016/j.procbio.2006.03.033
Teske A , Alm E , Regan JM , Toze S , Rittmann BE , Stahl DA 1994 Evolutionary relationships among ammonia- and nitrite-oxidizing bacteria. J. Bacteriol. 176 6623 - 6630
Chen H , Liu S , Yang F , Xue Y , Wang T 2009 The development of si-multaneous partial nitrification ANAMMOX and denitrifica-tion (SNAD) process in a single reactor for nitrogen removal. Bioresour. Technol. 100 1548 - 1554    DOI : 10.1016/j.biortech.2008.09.003
Park W , Nam YK , Lee MJ , Kim TH 2009 Simultaneous nitrification and denitrification in a CEM (cation exchange membrane)-bounded two chamber system. Water Res. 43 3820 - 3826    DOI : 10.1016/j.watres.2009.05.039
Zhang Y , Zhou J , Zhang J , Yuan S 2009 An innovative membrane bioreactor and packed-bed biofilm reactor combined sys-tem for shortcut nitrification-denitrification. J. Environ. Sci. 21 568 - 574    DOI : 10.1016/S1001-0742(08)62309-8
Liu Y , Capdeville B 1994 Kinetic behaviors of nitrifying biofilm growth in wastewater nitrification process. Environ. Technol. 15 1001 - 1013    DOI : 10.1080/09593339409385509
Nogueira R , Lazarova V , Manem J , Melo LF 1998 Influence of dis-solved oxygen on the nitrification kinetics in a circulating bed biofilm reactor. Bioprocess Eng. 19 441 - 449    DOI : 10.1007/s004490050546
Fitch MW , Pearson N , Richards G , Burken JG 1998 Biological fixed-film systems. Water Environ. Res. 70 495 - 518    DOI : 10.2175/106143098X134226
Yan J , Hu YY 2009 Partial nitrification to nitrite for treating am-monium-rich organic wastewater by immobilized biomass system. Bioresour. Technol. 100 2341 - 2347    DOI : 10.1016/j.biortech.2008.11.038
Mallick N 2002 Biotechnological potential of immobilized algae for wastewater N, P and metal removal: a review. BioMetals 15 377 - 390    DOI : 10.1023/A:1020238520948
Morita M , Kudo N , Uemoto H , Watanabe A , Shinozaki H 2007 Protective effect of immobilized ammonia oxidizers and phenol-degrading bacteria on nitrification in ammonia- and phenol-containing wastewater. Eng. Life Sci. 7 587 - 592    DOI : 10.1002/elsc.200700014
Show KY , Tay JH 1999 Influence of support media on bio-mass growth and retention in anaerobic filters. Water Res. 33 1471 - 1481    DOI : 10.1016/S0043-1354(98)00352-2
Chung J , Bae W , Lee YW , Rittmann BE 2007 Shortcut biological nitrogen removal in hybrid biofilm/suspended growth reac-tors. Process Biochem. 42 320 - 328    DOI : 10.1016/j.procbio.2006.09.002
Aesoy A , Ødegaard H , Bach K , Pujol R , Hamon M 1998 Denitrifica-tion in a packed bed biofilm reactor (biofor) - experiments with different carbon sources. Water Res. 32 1463 - 1470    DOI : 10.1016/S0043-1354(97)00358-8
Wang Z 1998 Application of biofilm kinetics to the sulfur/lime packed bed reactor for autotrophic denitrification of ground-water. Water Sci. Technol. 37 97 - 104
Parent LE , Caron J 1993 Physical properties of organic soils. In: Carter MR ed. Soil sampling and methods of analysis. Lewis Publishers Boca Raton ch. 43.
Hashimoto S , Furukawa K , Shioyama M 1987 Autotrophic de-nitrification using elemental sulfur. J. Ferment. Technol. 65 683 - 692    DOI : 10.1016/0385-6380(87)90011-2
Koenig A , Liu LH 2001 Kinetic model of autotrophic deni-trification in sulphur packed-bed reactors. Water Res. 35 1969 - 1978    DOI : 10.1016/S0043-1354(00)00483-8
Hamoda MF , Abd-El-Bary MF 1987 Operating characteristics of the aerated submerged fixed-film (ASFF) bioreactor. Water Res. 21 939 - 947    DOI : 10.1016/S0043-1354(87)80011-8
Huang JC , Chang SY , Liu YC , Jiang Z 1985 Biofilm growths with sucrose as substrate. J. Environ. Eng. 111 353 - 363    DOI : 10.1061/(ASCE)0733-9372(1985)111:3(353)
Stensel HD , Brenner RC , Lee KM , Melcer H , Rakness K 1988 Bio-logical aerated filter evaluation. J. Environ. Eng. 114 655 - 671    DOI : 10.1061/(ASCE)0733-9372(1988)114:3(655)
Clescerl LS , Greenberg AE , Eaton AD 1999 Standard methods for the examination of water and wastewater. 20th ed. American Public Health Association American Water Works Association Water Environment Federation New York
Dempsey MJ , Lannigan KC , Minall RJ 2005 Particulate-biofilm expanded-bed technology for high-rate low-cost wastewa-ter treatment: nitrification. Water Res. 39 965 - 974    DOI : 10.1016/j.watres.2004.12.017
Lekang OI , Kleppe H 2000 Efficiency of nitrification in trickling fil-ters using different filter media. Aquacult. Eng. 21 181 - 199    DOI : 10.1016/S0144-8609(99)00032-1
Bock E , Koops HP , Harms H 1986 Cell biology of nitrifying bacte-ria. In: Prosser JI Society for General Microbiology eds. Ni-trification. IRL Press Washington DC 17 - 38
Gómez MA , González-López J , Hontoria-García E 2000 Influ-ence of carbon source on nitrate removal of contaminated groundwater in a denitrifying submerged filter. J. Hazard. Mater. 80 69 - 80    DOI : 10.1016/S0304-3894(00)00282-X
Menasveta P , Panritdam T , Sihanonth P , Powtongsook S , Chuntapa B , Lee P 2001 Design and function of a closed recircu-lating seawater system with denitrification for the culture of black tiger shrimp broodstock. Aquacult. Eng. 25 35 - 49    DOI : 10.1016/S0144-8609(01)00069-3
Suzuki Y , Maruyama T , Numata H , Sato H , Asakawa M 2003 Perfor-mance of a closed recirculating system with foam separation nitrification and denitrification units for intensive culture of eel: towards zero emission. Aquacult. Eng. 29 165 - 182    DOI : 10.1016/j.aquaeng.2003.08.001
Hamlin HJ , et al. , Michaels JT , et al. , Beaulaton CM , et al. 2008 Comparing de-nitrification rates and carbon sources in commercial scale upflow denitrification biological filters in aquaculture. Aqua-cult. Eng. et al. 38 79 - 92    DOI : 10.1016/j.aquaeng.2007.11.003
Batchelor B , Lawrence AW 1978 Autotrophic denitrifucation using elemental sulfur. J. Water Pollut. Control Fed. 50 1986 - 2001
Lee DU , Lee IS , Choi YD , Bae JH 2001 Effects of external carbon source and empty bed contact time on simultaneous hetero-trophic and sulfur-utilizing autotrophic denitrification. Pro-cess Biochem. 36 1215 - 1224    DOI : 10.1016/S0032-9592(01)00163-7