# Recognition of Relevant ORP, pH, and DO Bending Points in Ammonia Removal from Drinking Water through Online BAF System

Authors: Hassimi Abu Hasan; Siti Rozaimah Sheikh Abdullah; Siti Kartom Kamarudin; Noorhisham Tan Kofli
Journal: International Journal of Chemical Engineering
 (2010)

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## Abstract

This study was undertaken to identify the relevant bending points in ORP, pH, and DO profiles in ammonia removal through online monitoring. A novelty BAF system as newl application for drinking water treatment that equipped with ORP, pH, DONH4+ and NO3− sensors was used. Two types of polluted drinking water strength (low and high strength) with various NH4+ concentrations and aeration flow were treated at a fixed-time reaction of 24 h. Experiments were conducted at four track studies (TS) of TS1 (NH4+= 50 mg/L, aeration = 0.3 L/min), TS2 (NH4+ = 100 mg/L, aeration = 2.0 L/min), TS3 (NH4+= 100 mg/L, no aeration) and TS4 (NH4+= 10 mg/L, aeration = 0.1 L/min). The results showed that the removal of NH4+ was more than 95% for TS1, TS2, and TS4. From the online monitoring performances, DO elbow and ammonia valley  appeared in ORP and pH profiles, respectively. Similarly, new positive plateaus were observed in DO, indicating that the nitrifiers stopped to consume the DO after NH4+ was completely removed. Hence, based on the bending points, the aeration system is possible to be automatically stopped just after DO elbow and ammonia valley appears in order to save the energy consumption and to shorten the time demands for the drinking water treatment process.


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## Body

## 1. Introduction

The presence of ammonia in drinking water exceeding the Malaysian regulated limit (<1.5 mg/L) became a major problem to drinking water treatment plants (DWTPs). Recently, there is no specific treatment system that can remove the pollutant efficiently which finally causes plant shutdown for a period of time. Consequently, the populations in the area will face a shortage in water supply and interruption in almost daily activities. Moreover, high ammonia level in drinking water provided a complication on chlorination process due to the yield of chloramines [1], human nervous system damage and created a deteriorating taste and odour of water [2]. Therefore, it is necessary to develop an effective additional water treatment system, typically for ammonia removal in order to prevent the plant shutdown due to the high level of ammonia in water.Based on the literature, biological aerated filter (BAF) is a suitable process as an additional system in DWTPs where the system is well known as one of the biological treatment systems in wastewater treatment but not in drinking water treatment. The BAF system is an attached growth process where consortium microorganisms grow on media which are stationary during normal operation with aeration [3, 4]. Among the outstanding advantages of BAF are that it is a flexible reactor and able to perform solids separation as well as aerobic biological treatment, the space requirement for the treatment is also small [5]  and it serves as a small footprint with a large surface area, simple construction and has ability to treat high organic loads [6]. Previous researchers [7–11] reported that almost and over 90% of ammonia was eliminated from wastewater by using BAF system. However, an effective performance can be only achieved with higher removal at optimum operational conditions such as short hydraulic retention time (HRT) and less electrical energy consumption for aeration. Thus, online monitoring can be used as a tool to control the biological ammonia removal from drinking water using BAF system.Recently, online monitoring using pH, oxidation reduction potential (ORP), and dissolved oxygen (DO) as parameters to control the biological nutrient removal has received much attention [11–14]. The ORP and DO levels can successfully indicate the oxidative and biological state of the wastewater, and pH is a good indicator of ongoing biological reactions [15]. The increasing interest toward the online monitoring is due to some advantages, that is, the biological nutrient removal can be controlled through relevant points such as ammonia valley and nitrate knee, it can be used to optimise the aerobic stage where the aeration can be stopped whenever nitrification is completed and subsequent anaerobic stage can be avoided when denitrification is completed [16].ORP is the electromotive force developed when oxidizers or reducers are present in water. Compared with DO, ORP regulation is more in tune with the process dynamics, since many biological substances correlate with ORP values. In addition, protons generated in nitrification lowered pH values. Therefore, the ORP and pH have been commonly studied for real-time monitoring and control of activated sludge process [13, 17–19]. Particularly, several researchers have identified the “ammonia valley” in pH profiles and the “nitrogen break point” or the “DO elbow” in ORP profiles, which indicate the end of nitrification and the “nitrate knee” in ORP profiles and the “nitrate apex” in pH profiles indicating the end of denitrification process [11, 16, 19–21]. Corresponding to the bending point recognition, it was able to monitor the biological ammonia removal to save electrical energy consumption particularly during aeration phase [16].To the best of knowledge, there is lacking information in online monitoring of ammonia removal from drinking water using BAF system, where most of the studies are mainly focused on using a sequencing biological reactor (SBR). Therefore, the aim of this study is to monitor and identify the relevant bending point in the pH, ORP, and DO profiles through online monitoring at various loading rates and operating conditions.


## 2. Materials and Methods

### 2.1. Synthetic Drinking Water

Synthetic polluted drinking water was prepared as feeding by using tap water. The water consists of glucose (C6H12O6: 100–1000 mg/L), ammonium sulphate ((NH4)2SO3: 10–100 mg/L), sodium bicarbonate (NaHCO3: 100 mg/L), magnesium chloride (MgCl2·6H2O: 8 mg/L), iron chloride (FeCl3·6H2O: 0.3 mg/L), manganese chloride (MnCl2·4H2O: 2.0 ± 0.1 mg/L), calcium chloride (CaCl2·2H2O: 4.5 mg/L), and potassium dihydrogen phosphate (KH2PO4: 2.5 mg/L). All the chemicals used are reagent grade salts (Systerm, Malaysia).


### 2.2. Bacteria Seeding

The seeding sewage activated sludge (SAS) as a degrading biofilm source used in the experiment was taken from a sewage treatment plant located in Putrajaya, Malaysia. The SAS is an effective bacteria source in which it contains more complex consortium of microorganisms, surface chemistry, large surface area, porosity, and excellent settling ability [22]. The SAS was acclimatised with sufficient energy source such as glucose (200 mg/L) and inorganic nutrients such as ammonia as nitrogen source (40 mg/L), phosphorus (2.5 mg/L), sulphur (10 mg/L), and trace elements (iron 0.3 mg/L, manganese 0.3 mg/L, and magnesium 8 mg/L) for bacterial growth and enrichment [23]. Sodium bicarbonate (100 mg/L) as an external source of alkalinity was added at initiation of runs in order to prevent an insufficiency of the inorganic carbon that nitrifying bacteria require for their metabolism.


### 2.3. BAF Description and Track Studies

An upward flow configuration of a lab scaled BAF system was designed using transparent polyvinyl chloride (PVC) at a height of 150 cm and diameter of 16 cm with an effective working volume of 16 L. The design was based on the data correlation of removal performances with BAF dimensions obtained from a previous study [24]. The schematic details are depicted in Figure 1. The system consisted of five main components, that is, BAF column, media, influent and effluent tank, influent and backwash pump, air compressor, and online monitoring set. At the top of the column, there was a buffer zone with 20 cm height to stop media from being carried away when treatment and backwash are operated. Sampling ports (SPs) were placed along the column height at 20 cm intervals for biomass and water sampling purposes.Figure 1
Schematic details of BAF equipped with online monitoring tools.The BAF was partially filled (about 12 L) with a plastic media for nitrifiers growth and attachment. The media was made from polypropylene with dimension ratio (H/D) of 0.625 and density of 888 kg/m3. The prepared feed from influent tank was flowed upward using a peristaltic pump (Masterflex, USA) at a flow rate of 580 mL/min to occupy the BAF column in about 30 minutes. Aeration was supplied at the bottom of BAF column with an assistance of air compressor (PUMA XN2040, Taiwan). An air diffuser was used to distribute the air through the column in order to ensure homogenised condition. In the case of media clogging occurrence and maintenance of the nitrifier activity, the backwash system is subsequently operated by using water pump (CPm 158, Italy).Investigation was divided to 4 track studies (TS1, TS2, TS3, and TS4). Each track study   is varied in feed concentration (main interest:NH4+) and aeration rate. Table 1 showed the operating conditions where initial pH and HRT are maintained constantly at pH 6-7 and 24 h HRT. There are two strengths of simulated drinking water treated in this study. At TS1, high strength polluted drinking water (HSPDW) with concentration of 1000 mg/L COD and 50 mg/L NH4+ is fed where the COD : NH4+ ratio follows and the standard C : N ratio of 100 : 5. At TS2, NH4+ concentration and AR were increased in order to observe the influence of DO. Another test (TS3) with no aeration flow was also conducted which consequently created an anaerobic condition in BAF column. At TS4, treatment was conducted for a low strength polluted drinking water (LSPDW), and in parallel a slower aeration flow is supplied.Table 1
Track studies of ammonia removal at various operating conditions.
Track studiesTS1TS2TS3TS4Run (days)1310710COD (mg/L)1000 ± 291000 ± 331000 ± 15100 ± 2.6NH4+ (mg/L)50 ± 2100 ± 5100 ± 210 ± 0.26AR (L/min)0.32.000.1


### 2.4. Analytical and Online Monitoring Setup

COD was determined through digestion method at 150°C for 2 hours in HACH Reactor Digestion (HACH, USA) and measured by a spectrophotometer (HACH DR/2010, USA) at an absorbance of 620 nm (Method 8000). pH, ORP, and DO were continuously measured using pH (Model PD1R1 GLI, USA), ORP (Model PD1R1 GLI, USA), and DO (Model 5400 GLI, USA) probes connected to GLI meters (Model 33, USA),respectively. Meanwhile,NH4+ and NO3- were measured using Swansensor ammonium and Swansensor nitrate ion selective electrodes (ISE) and analysed through SWAN meters (FAM: Ammonium; FAM: Nitrate, Switzerland). All of the instruments were continuously calibrated depending on the sensors performance. An ORP value of +200 mV was used as a reference point to observe the oxidation length of the treatment period. For online monitoring, a program in Microsoft Visual C++ (Version 7.1.3088) software (USA) was set up. The A/D converter interface and data acquisition card (EX92026, Taiwan) provided the connection between PC, meters (pH, ORP, DO, NH4+-N and NO3-), and air valve unit (Figure 1). Online mean values of pH, DO, ORP, NH4+ and NO3- were recorded for every 60 s as presented in Figure 2.Figure 2
Online monitoring profiles as simulated by a Microsoft Visual C++ programming.


## 2.1. Synthetic Drinking Water

Synthetic polluted drinking water was prepared as feeding by using tap water. The water consists of glucose (C6H12O6: 100–1000 mg/L), ammonium sulphate ((NH4)2SO3: 10–100 mg/L), sodium bicarbonate (NaHCO3: 100 mg/L), magnesium chloride (MgCl2·6H2O: 8 mg/L), iron chloride (FeCl3·6H2O: 0.3 mg/L), manganese chloride (MnCl2·4H2O: 2.0 ± 0.1 mg/L), calcium chloride (CaCl2·2H2O: 4.5 mg/L), and potassium dihydrogen phosphate (KH2PO4: 2.5 mg/L). All the chemicals used are reagent grade salts (Systerm, Malaysia).


## 2.2. Bacteria Seeding

The seeding sewage activated sludge (SAS) as a degrading biofilm source used in the experiment was taken from a sewage treatment plant located in Putrajaya, Malaysia. The SAS is an effective bacteria source in which it contains more complex consortium of microorganisms, surface chemistry, large surface area, porosity, and excellent settling ability [22]. The SAS was acclimatised with sufficient energy source such as glucose (200 mg/L) and inorganic nutrients such as ammonia as nitrogen source (40 mg/L), phosphorus (2.5 mg/L), sulphur (10 mg/L), and trace elements (iron 0.3 mg/L, manganese 0.3 mg/L, and magnesium 8 mg/L) for bacterial growth and enrichment [23]. Sodium bicarbonate (100 mg/L) as an external source of alkalinity was added at initiation of runs in order to prevent an insufficiency of the inorganic carbon that nitrifying bacteria require for their metabolism.


## 2.3. BAF Description and Track Studies

An upward flow configuration of a lab scaled BAF system was designed using transparent polyvinyl chloride (PVC) at a height of 150 cm and diameter of 16 cm with an effective working volume of 16 L. The design was based on the data correlation of removal performances with BAF dimensions obtained from a previous study [24]. The schematic details are depicted in Figure 1. The system consisted of five main components, that is, BAF column, media, influent and effluent tank, influent and backwash pump, air compressor, and online monitoring set. At the top of the column, there was a buffer zone with 20 cm height to stop media from being carried away when treatment and backwash are operated. Sampling ports (SPs) were placed along the column height at 20 cm intervals for biomass and water sampling purposes.Figure 1
Schematic details of BAF equipped with online monitoring tools.The BAF was partially filled (about 12 L) with a plastic media for nitrifiers growth and attachment. The media was made from polypropylene with dimension ratio (H/D) of 0.625 and density of 888 kg/m3. The prepared feed from influent tank was flowed upward using a peristaltic pump (Masterflex, USA) at a flow rate of 580 mL/min to occupy the BAF column in about 30 minutes. Aeration was supplied at the bottom of BAF column with an assistance of air compressor (PUMA XN2040, Taiwan). An air diffuser was used to distribute the air through the column in order to ensure homogenised condition. In the case of media clogging occurrence and maintenance of the nitrifier activity, the backwash system is subsequently operated by using water pump (CPm 158, Italy).Investigation was divided to 4 track studies (TS1, TS2, TS3, and TS4). Each track study   is varied in feed concentration (main interest:NH4+) and aeration rate. Table 1 showed the operating conditions where initial pH and HRT are maintained constantly at pH 6-7 and 24 h HRT. There are two strengths of simulated drinking water treated in this study. At TS1, high strength polluted drinking water (HSPDW) with concentration of 1000 mg/L COD and 50 mg/L NH4+ is fed where the COD : NH4+ ratio follows and the standard C : N ratio of 100 : 5. At TS2, NH4+ concentration and AR were increased in order to observe the influence of DO. Another test (TS3) with no aeration flow was also conducted which consequently created an anaerobic condition in BAF column. At TS4, treatment was conducted for a low strength polluted drinking water (LSPDW), and in parallel a slower aeration flow is supplied.Table 1
Track studies of ammonia removal at various operating conditions.
Track studiesTS1TS2TS3TS4Run (days)1310710COD (mg/L)1000 ± 291000 ± 331000 ± 15100 ± 2.6NH4+ (mg/L)50 ± 2100 ± 5100 ± 210 ± 0.26AR (L/min)0.32.000.1


## 2.4. Analytical and Online Monitoring Setup

COD was determined through digestion method at 150°C for 2 hours in HACH Reactor Digestion (HACH, USA) and measured by a spectrophotometer (HACH DR/2010, USA) at an absorbance of 620 nm (Method 8000). pH, ORP, and DO were continuously measured using pH (Model PD1R1 GLI, USA), ORP (Model PD1R1 GLI, USA), and DO (Model 5400 GLI, USA) probes connected to GLI meters (Model 33, USA),respectively. Meanwhile,NH4+ and NO3- were measured using Swansensor ammonium and Swansensor nitrate ion selective electrodes (ISE) and analysed through SWAN meters (FAM: Ammonium; FAM: Nitrate, Switzerland). All of the instruments were continuously calibrated depending on the sensors performance. An ORP value of +200 mV was used as a reference point to observe the oxidation length of the treatment period. For online monitoring, a program in Microsoft Visual C++ (Version 7.1.3088) software (USA) was set up. The A/D converter interface and data acquisition card (EX92026, Taiwan) provided the connection between PC, meters (pH, ORP, DO, NH4+-N and NO3-), and air valve unit (Figure 1). Online mean values of pH, DO, ORP, NH4+ and NO3- were recorded for every 60 s as presented in Figure 2.Figure 2
Online monitoring profiles as simulated by a Microsoft Visual C++ programming.


## 3. Results and Discussion

The track study results of four typical batch runs are presented with the first three runs representative of the HPSDW (TS1, TS2, and TS3) and the last run representative of the LPSDW (TS4).


### 3.1. Track Study 1 (TS1)

Figure3 shows the profiles of TS1 and indicates that, for the 50 mg/L NH4+ fed at constant 0.3 L/min AR, the complete NH4+ removal occurred at the point A (end of 16 h). Along the removal process, the formation of NO3- was observed as increasing until the end of 24 h HRT. The common trends were due to continuous oxidation of NH4+ nitrite (NO2−) and later to NO3- by nitrifiers with the assistance of sufficient DO. In DO profile, a distinct DO plateaus formed at point B after NH4+ was completely removed. The phenomenon shows that the consumption of DO by nitrifiers to oxidize the NH4+ is decreased, and therefore, the DO increased after point B to a higher concentration. The clear appearance of point C on the ORP profile is well correlated to DO elbow which indicates the end of nitrification process. In the mean time, pH values started to increase at point D. However, nitrate knee in ORP and the nitrate apex in pH profiles to indicate the end of denitrification process did not appear. This result is expected, because there was a fully aerobic condition in the BAF column besides the presence of excessive dissolved oxygen for 24 h HRT.Figure 3
Online monitoring profiles from TS1 for pH, DO, ORP,NH4+, and NO3-.


### 3.2. Track Study 2 (TS2)

Figure4 shows the profiles of TS2 and indicates that, for the 100 mg/L NH4+ fed at constant 2.0 L/min AR, the stationary NH4+ concentration was observed after 16 h of reaction time (point A), similar to TS1 profile. Again, once NH4+ depleted, the DO plateau was also formed (point B) but this time only with slight significance. This is because the higher NH4+ concentration is, the more DO will be consumed by nitrifiers for degradation.Figure 4
Online monitoring profiles from TS2 for pH, DO, ORP,NH4+, and NO3-.Therefore, it can be seen from Figure4 that the DO concentration was much lower compared with previous DO profile in TS1. For the ORP profile, two bending points were formed at points C and D, indicating the end of nitrification stage and full oxidation status [25]. However, at point C, the remaining NH4+ concentration was 25 mg/L, and the oxidation process continuously occurred and started to level off at point D which at the time, the concentration was below 0.5 mg/L. Moreover, pH profile started to level off starting from point E, indicating that there is no more hydrogen ion produced [25].The comparison of TS1 and TS2 results with other researchers using on-line BAF monitoring for ammonia removal could not be done. Most of the previous investigations only focused on using on-line SBR monitoring [11–14, 16, 19, 26] compared to other biological systems. Nevertheless, the obtained DO, pH, and ORP bending points in on-line BAF also show similarity to the theoretical principle especially ammonia valley (pH profile) and DO elbow (ORP profile) which indicate the completion of a nitrification process.


### 3.3. Track Study 3 (TS3)

Figure5 presents the profiles of TS3 for the 100 mg/L NH4+ fed without aeration. As can be observed, the removal of NH4+ did not occur without aeration compared with TS2, which was similar in both influent conditions. It was because DO was not sufficiently supplied to the nitrifiers in the BAF system which inhibited the nitrification process at low DO concentration [27, 28]. Moreover, along the treatment period, DO concentration was almost zero which had created an anaerobic condition in BAF column. Through ORP profile, it be can strengthened that the removal of NH4+ did not occur because the profile showed the decreased trend during the period.Figure 5
Online monitoring profiles from TS3 for pH, DO, ORP,NH4+, and NO3-.


### 3.4. Track Study 4 (TS4)

Figure6 illustrates the profile of DO, ORP, pH, NH4+ and NO3- under LSPDW (NH4+≈ 10 mg/L) at aeration flow of 0.1 L/min. Generally, a lower NH4+ concentration in water, a shorter HRT are required for complete degradation process. As can be seen in Figure 6, the NH4+ profile was at steady-state condition starting from point A (after 7 h HRT) representing the complete removal. Meanwhile, NO3- continuously increased because the presence of NH4+ residue in the water and also the denitrification process did not take place due to the excessive aeration period. When NH4+ was completely removed, a new positive DO plateau was formed at point B, and after 9 h a steady-state concentration was achieved with 4.7 mg/L. Moreover, DO elbow (ORP = +240 mV) and ammonia valley (pH 6.28) can be observed at points C and D in ORP and pH, respectively. Since there are no more oxidation occurring and hydrogen ion being produced, ORP decreased to the lowest value of +220 mV while pH increased to a maximum value of 6.6. Therefore, as an effective NH4+ removal using BAF system for the optimum drinking water treatment operation, aeration can be stopped at 7 h HRT to allow denitrification process to take place and save energy of electrical consumption.Figure 6
Online monitoring profiles from TS4 for pH, DO, ORP,NH4+, and NO3-.


## 3.1. Track Study 1 (TS1)

Figure3 shows the profiles of TS1 and indicates that, for the 50 mg/L NH4+ fed at constant 0.3 L/min AR, the complete NH4+ removal occurred at the point A (end of 16 h). Along the removal process, the formation of NO3- was observed as increasing until the end of 24 h HRT. The common trends were due to continuous oxidation of NH4+ nitrite (NO2−) and later to NO3- by nitrifiers with the assistance of sufficient DO. In DO profile, a distinct DO plateaus formed at point B after NH4+ was completely removed. The phenomenon shows that the consumption of DO by nitrifiers to oxidize the NH4+ is decreased, and therefore, the DO increased after point B to a higher concentration. The clear appearance of point C on the ORP profile is well correlated to DO elbow which indicates the end of nitrification process. In the mean time, pH values started to increase at point D. However, nitrate knee in ORP and the nitrate apex in pH profiles to indicate the end of denitrification process did not appear. This result is expected, because there was a fully aerobic condition in the BAF column besides the presence of excessive dissolved oxygen for 24 h HRT.Figure 3
Online monitoring profiles from TS1 for pH, DO, ORP,NH4+, and NO3-.


## 3.2. Track Study 2 (TS2)

Figure4 shows the profiles of TS2 and indicates that, for the 100 mg/L NH4+ fed at constant 2.0 L/min AR, the stationary NH4+ concentration was observed after 16 h of reaction time (point A), similar to TS1 profile. Again, once NH4+ depleted, the DO plateau was also formed (point B) but this time only with slight significance. This is because the higher NH4+ concentration is, the more DO will be consumed by nitrifiers for degradation.Figure 4
Online monitoring profiles from TS2 for pH, DO, ORP,NH4+, and NO3-.Therefore, it can be seen from Figure4 that the DO concentration was much lower compared with previous DO profile in TS1. For the ORP profile, two bending points were formed at points C and D, indicating the end of nitrification stage and full oxidation status [25]. However, at point C, the remaining NH4+ concentration was 25 mg/L, and the oxidation process continuously occurred and started to level off at point D which at the time, the concentration was below 0.5 mg/L. Moreover, pH profile started to level off starting from point E, indicating that there is no more hydrogen ion produced [25].The comparison of TS1 and TS2 results with other researchers using on-line BAF monitoring for ammonia removal could not be done. Most of the previous investigations only focused on using on-line SBR monitoring [11–14, 16, 19, 26] compared to other biological systems. Nevertheless, the obtained DO, pH, and ORP bending points in on-line BAF also show similarity to the theoretical principle especially ammonia valley (pH profile) and DO elbow (ORP profile) which indicate the completion of a nitrification process.


## 3.3. Track Study 3 (TS3)

Figure5 presents the profiles of TS3 for the 100 mg/L NH4+ fed without aeration. As can be observed, the removal of NH4+ did not occur without aeration compared with TS2, which was similar in both influent conditions. It was because DO was not sufficiently supplied to the nitrifiers in the BAF system which inhibited the nitrification process at low DO concentration [27, 28]. Moreover, along the treatment period, DO concentration was almost zero which had created an anaerobic condition in BAF column. Through ORP profile, it be can strengthened that the removal of NH4+ did not occur because the profile showed the decreased trend during the period.Figure 5
Online monitoring profiles from TS3 for pH, DO, ORP,NH4+, and NO3-.


## 3.4. Track Study 4 (TS4)

Figure6 illustrates the profile of DO, ORP, pH, NH4+ and NO3- under LSPDW (NH4+≈ 10 mg/L) at aeration flow of 0.1 L/min. Generally, a lower NH4+ concentration in water, a shorter HRT are required for complete degradation process. As can be seen in Figure 6, the NH4+ profile was at steady-state condition starting from point A (after 7 h HRT) representing the complete removal. Meanwhile, NO3- continuously increased because the presence of NH4+ residue in the water and also the denitrification process did not take place due to the excessive aeration period. When NH4+ was completely removed, a new positive DO plateau was formed at point B, and after 9 h a steady-state concentration was achieved with 4.7 mg/L. Moreover, DO elbow (ORP = +240 mV) and ammonia valley (pH 6.28) can be observed at points C and D in ORP and pH, respectively. Since there are no more oxidation occurring and hydrogen ion being produced, ORP decreased to the lowest value of +220 mV while pH increased to a maximum value of 6.6. Therefore, as an effective NH4+ removal using BAF system for the optimum drinking water treatment operation, aeration can be stopped at 7 h HRT to allow denitrification process to take place and save energy of electrical consumption.Figure 6
Online monitoring profiles from TS4 for pH, DO, ORP,NH4+, and NO3-.


## 4. Conclusions

This study confirms that identification of bending point in ORP and pH profiles corresponding to DO elbow and ammonia valley clearly appears during theNH4+ removal in novelty application of BAF system for drinking water treatment. Although various NH4+ concentrations were fed to the BAF, the ORP, pH and DO showed a similar characteristic in ORP, pH, and DO profiles. From the bending point, the effective NH4+ removal process can be maximized through the real-time control in order to prevent the excessive aeration and time demanding. The appearance of DO elbow and ammonia valley would give possibility to stop the aeration which consequently saves the energy. When no aeration was provided, the significant bending points were not observed and at the mean time the oxidation process did  not occur. Therefore, the online monitoring tools can be used also in troubleshooting of the BAF operational especially when there is a problem in aeration system.



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*Source: 587032-2011-02-27.xml*