"Applied Science, Faculty of"@en . "Civil Engineering, Department of"@en . "DSpace"@en . "UBCV"@en . "Kosari, Fatemeh"@en . "2011-08-26T17:44:46Z"@en . "2011"@en . "Master of Applied Science - MASc"@en . "University of British Columbia"@en . "Nitrogen removal from wastewater through partial nitrification/Anammox was investigated. The objectives of the research were divided to three distinctive and related areas: Partial Nitrification (PN) process, Anammox reaction and green house gases emission from partial nitrification and Anammox reactor. \n\nIn the PN process, research objectives were to determine: 1) the effect Dissolved Oxygen concentration, alkalinity on the PN reaction 2) evaluation of continuous moving bed biofilm reactor (MBBR) and sequencing batch reactor (SBR) for partial nitrification process. The main goals of the Anammox process study was to investigate: 1) parameters, which affect the Anammox process 2) evaluation of continuous moving bed biofilm reactor, hybrid reactor and up-flow fixed-bed reactor for the Anammox process. In the last stage, N\u00E2\u0082\u0082O and NO emissions from both partial nitrification and Anammox reactor under various operating conditions were determined.\n\nPartial nitrification in the sequencing batch reactor was more efficient, compared to continuous moving bed biofilm reactor. Alkalinity was investigated as a limiting factor for oxidizing more ammonium to nitrite in the PN reactor. The effluent of the MBBR contained 59.7% ammonium, 31.7 % nitrite and 8.5 % nitrate and gaseous products, such as nitrous oxide and nitrogen as initial nitrogen load. Whereas, the SBR could convert more than 45% of the ammonium to nitrite; in fact, the effluent of the SBR reactor contained 45.1% ammonium, 45.1% nitrite and 1.9% nitrate, as initial nitrogen load. \n\nSubsequent Anammox treatment, after the MBBR, resulted in 38.8% additional ammonium removal and nitrite removal of 83.1 %. As a result, total ammonia removal in the combined system reached 79.1% and total nitrogen removal was 56.8 %.\n\nThe Hybrid Anammox reactor removed an average of 55.8% of NH\u00E2\u0082\u0084-N, versus 48.3% NH\u00E2\u0082\u0084-N removal in the up-flow fixed-bed reactor. Nitrite removal in the hybrid and up-flow fixed-bed Anammox reactor was 80.8% and 62.5%, respectively.\n\nThis research indicates that nitrous oxide and nitric oxide emission from partial nitrification at DO being controlled at 2 mg/L were 2.6\u00C2\u00B10.2% and 0.6\u00C2\u00B10.3% as nitrogen load, respectively. Relatively low N\u00E2\u0082\u0082O of 0.15\u00C2\u00B10.02% was observed from the Anammox reactor, compared to partial nitrification and NO emissions was none detected."@en . "https://circle.library.ubc.ca/rest/handle/2429/36921?expand=metadata"@en . " NITROGEN REMOVAL FROM WASTEWATER THROUGH PARTIAL NITRIFICATION / ANAMMOX PROCESS by Fatemeh Kosari B.Sc. Iran University of Science and Technology 2005 A THESIS SUBMITED IN PARTIAL FULFILMENT OF THE REQUIREMENTS FOR THE DEGREE OF MASTER OF APPLIED SCIENCE in The Faculty of Graduate Studies (Civil Engineering) THE UNIVERSITY OF BRITISH COLUMBIA (Vancouver) August 2011 \u00C2\u00A9 Fatemeh Kosari,2011 ii Abstract Nitrogen removal from wastewater through partial nitrification/Anammox was investigated. The objectives of the research were divided to three distinctive and related areas: Partial Nitrification (PN) process, Anammox reaction and green house gases emission from partial nitrification and Anammox reactor. In the PN process, research objectives were to determine: 1) the effect Dissolved Oxygen concentration, alkalinity on the PN reaction 2) evaluation of continuous moving bed biofilm reactor (MBBR) and sequencing batch reactor (SBR) for partial nitrification process. The main goals of the Anammox process study was to investigate: 1) parameters, which affect the Anammox process 2) evaluation of continuous moving bed biofilm reactor, hybrid reactor and up-flow fixed-bed reactor for the Anammox process. In the last stage, N2O and NO emissions from both partial nitrification and Anammox reactor under various operating conditions were determined. Partial nitrification in the sequencing batch reactor was more efficient, compared to continuous moving bed biofilm reactor. Alkalinity was investigated as a limiting factor for oxidizing more ammonium to nitrite in the PN reactor. The effluent of the MBBR contained 59.7% ammonium, 31.7 % nitrite and 8.5 % nitrate and gaseous products, such as nitrous oxide and nitrogen as initial nitrogen load. Whereas, the SBR could convert more than 45% of the ammonium to nitrite; in fact, the effluent of the SBR reactor contained 45.1% ammonium, 45.1% nitrite and 1.9% nitrate, as initial nitrogen load. Subsequent Anammox treatment, after the MBBR, resulted in 38.8% additional ammonium removal and nitrite removal of 83.1 %. As a result, total ammonia removal in the combined system reached 79.1% and total nitrogen removal was 56.8 %. iii The Hybrid Anammox reactor removed an average of 55.8% of NH4-N, versus 48.3% NH4-N removal in the up-flow fixed-bed reactor. Nitrite removal in the hybrid and up-flow fixed-bed Anammox reactor was 80.8% and 62.5%, respectively. This research indicates that nitrous oxide and nitric oxide emission from partial nitrification at DO being controlled at 2 mg/L were 2.6\u00C2\u00B10.2% and 0.6\u00C2\u00B10.3% as nitrogen load, respectively. Relatively low N2O of 0.15\u00C2\u00B10.02% was observed from the Anammox reactor, compared to partial nitrification and NO emissions was none detected. iv Table of contents Abstract ..................................................................................................................................... ii Table of contents ....................................................................................................................... iv List of tables ............................................................................................................................. vi List of figures ........................................................................................................................... vii Acknowledgements .....................................................................................................................x 1. Introduction .........................................................................................................................1 1.1 Background ...................................................................................................................1 1.2 Objective of the study ...................................................................................................4 1.3 Literature review ...........................................................................................................4 1.3.1 Conventional nitrification-denitrification .....................................................................4 1.3.2 De-Ammonification.....................................................................................................6 1.3.3 Anammox ...................................................................................................................6 2. Materials and methods ....................................................................................................... 17 2.1 Feed ............................................................................................................................ 17 2.2 Apparatuses ................................................................................................................ 17 2.3 Sample analysis .......................................................................................................... 21 3. Partial nitrification followed by Anammox in continuous moving-bed biofilm reactors (MBBR) .................................................................................................................................... 23 3.1 Summary .................................................................................................................... 23 3.2 Introduction ................................................................................................................ 23 3.2.1 Objective of this stage of research ............................................................................. 24 3.3 Materials and methods ................................................................................................ 25 3.3.1 Feed .......................................................................................................................... 25 3.3.2 Experiment design ..................................................................................................... 25 3.3.3 Chemical analysis ...................................................................................................... 27 3.4 Results and discussion................................................................................................. 28 3.4.1 Performance of the partial nitrification in the continuous moving bed biofilm reactor 28 4. Partial nitrification in sequencing batch reactor followed by Anammox ............................. 32 4.1 Summary .................................................................................................................... 32 4.2 Introduction ................................................................................................................ 32 v 4.2.1 Objective of this study ............................................................................................... 34 4.3 Materials and methods ................................................................................................ 35 4.3.1 Feed .......................................................................................................................... 35 4.3.2 Experimental design .................................................................................................. 35 4.3.3 Chemical analysis ...................................................................................................... 38 4.4 Results and discussion................................................................................................. 39 4.4.1 Performance of the partial nitrification/Anammox process ......................................... 39 4.4.2 Partial nitrification in the sequencing batch reactor .................................................... 39 4.4.3 Anammox in hybrid reactor and up-flow fixed-bed reactor ........................................ 52 5. Greenhouse gases (nitrous oxide and nitric oxide) emission from partial nitrification and Anammox system ...................................................................................................................... 59 5.1 Summary .................................................................................................................... 59 5.2 Introduction ................................................................................................................ 59 5.2.1 Objective of this study ............................................................................................... 60 5.3 Material and methods .................................................................................................. 61 5.3.1 Feed .......................................................................................................................... 61 5.3.2 Experiment design ..................................................................................................... 61 5.3.3 Chemical analyses ..................................................................................................... 63 5.4 Results and discussion................................................................................................. 64 5.4.1 Performance of the partial nitrification/Anammox process ......................................... 64 5.4.2 N2O and NO emissions .............................................................................................. 65 6. Conclusions ....................................................................................................................... 73 6.1 Recommendation for the future research ..................................................................... 76 References ................................................................................................................................ 77 Appendix 1. Raw data of the partial nitrification followed by Anammox in the continuous moving-bed biofilm reactors (MBBR) ....................................................................................... 88 Appendix 2.Raw data of partial nitrification in the sequencing batch reactor ........................... 108 Appendix 3. Data of the hybrid and the up-flow fixed-bed Anammox reactors ........................ 121 vi List of tables Table 1. N2O and NO emissions from partial nitrification in different conditions ...................... 71 vii List of figures Figure 1. Anammox bacteria enriched on nonwoven fabric media at environmental lab (University of British Columbia) , the color of the enriched cubes have turned to red after 6 months ........................................................................................................................................8 Figure 2.Anammox reaction ...................................................................................................... 13 Figure 3. Partial nitrification reactor on the right side, Anammox reactor on the left side .......... 18 Figure 4. Dissolved oxygen controller ....................................................................................... 18 Figure 5. Sequencing batch reactor ............................................................................................ 19 Figure 6. On the right side the Anammox process in a hybrid reactor, on the left side the Anammox process in an up-flow fixed-bed biofilm reactor ....................................................... 20 Figure 7.pH, Temperature and ORP monitor ............................................................................. 20 Figure 8. Aquarium heater ......................................................................................................... 21 Figure 9. Schematic of bench scale partial nitrification /Anammox in continuous moving bed biofilm reactors ......................................................................................................................... 26 Figure 10. Ammonium, nitrate and nitrite test kits (UBC Environmental Lab) ........................... 27 Figure 11. Ammonium, nitrite, nitrate, nitric oxide and nitrogen gas in the PN reactor .............. 28 Figure 12. Schematic of bench scale partial nitrification in sequencing batch reactor followed by Anammox in two reactors ......................................................................................................... 37 Figure 13.Nitrogen species in the partial nitrification reactor over an 8-hour Cycle under base line conditions ........................................................................................................................... 40 Figure 14. pH measurement in the partial nitrification reactor over an 8 hour cycle under base line conditions ........................................................................................................................... 41 Figure 15. Nitrogen species in the partial nitrification reactor over an 8-hour cycle, level of dissolved oxygen controlled between 0.3 and 0.7 mg/L ............................................................. 42 Figure 16. Nitrogen species in the partial nitrification reactor over an 8-hour cycle, level of dissolved oxygen controlled between 3.5 and 4.5 mg/L ............................................................. 43 Figure 17. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; pH controlled at 7.2 by additional sodium hydroxide ....................................................................................... 45 viii Figure 18. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; pH controlled at 6.6 by additional hydrochloric acid ........................................................................................ 46 Figure 19. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; pH controlled at 6 by additional hydrochloric acid ........................................................................................... 47 Figure 20. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed slowly at the rate of 25 ml/min in 100 minutes .................................................................... 48 Figure 21. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed fast at the rate of 250 ml/min for 3 minutes, then centrate was pumped slowly at the rate of 25 ml/min for 70 minutes .......................................................................................................... 49 Figure 22. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed fast at the rate of 250 ml/min for 6 minutes, then centrate was pumped slowly at the rate of 25 ml/min for 40 minutes (how come nitrate and nitrate and nitrite are fluctuating ) ................. 50 Figure 23. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed fast at the rate of 250 ml/min for 10 minutes........................................................................ 51 Figure 24. Average of ammonium removals in the hybrid Anammox reactor in 5 different nitrite to ammonium ratios .................................................................................................................. 53 Figure 25. Average of nitrite removals in the hybrid Anammox reactor in 5 different nitrite to ammonium ratios ...................................................................................................................... 54 Figure 26. Average of total nitrogen removals in the hybrid Anammox reactor in 5 different nitrite to ammonium ratios ........................................................................................................ 55 Figure 27. Average of ammonium removals in the up-flow fixed-bed Anammox reactor in 5 different nitrite to ammonium ratios .......................................................................................... 56 Figure 28. Average of nitrite Removals in the up-flow fixed-bed Anammox reactor in 5 different nitrite to ammonium ratios ........................................................................................................ 57 Figure 29. Average of total nitrogen removals in the up-flow fixed-bed Anammox reactor in 5 different nitrite to ammonium ratios .......................................................................................... 58 Figure 30. Schematic of bench scale partial nitrification/Anammox process .............................. 62 Figure 31. Nitrogen species in the partial nitrification reactor under base line conditions ........... 66 Figure 32. pH measurement in the partial nitrification reactor .................................................. 67 Figure 33.N2O emission from partial nitrification reactor under base line conditions ................. 68 ix Figure 34.NO emission from partial nitrification reactor under base line conditions .................. 69 x Acknowledgements I would like to thank my Research Supervisors, Prof. Victor Lo and Prof. Donald Mavinic, Department of Civil Engineering, under whose diligent supervision and guidance this research and thesis have been successfully completed. I would also like to thank Dr. Babak Rezania, Research Fellow, Department of Civil Engineering, for his contributions, advice and discussions which were essential in the structuring of experiments and analysis of data. I sincerely appreciate My thanks go to Paula Parkinson and Tim Ma, Environmental Engineering Laboratory, Department of Civil Engineering, whose support contributed to the completion of laboratory analysis. I also would like to thank my colleagues, Ali Abedini, Ryan Thoren, Selina Yawson, Isabel Londono, Chad Novotny, and Kerry Black for their support during my time in Civil Engineering Department. Finally, I want to express my gratitude to my friends Minoo Jalali and Ali Bakhoda, my family and Seyed Mahdi Beheshtian for their support and encouragements. xi Dedication To God, for his countless blessings; To my Mother for her support, encouragement, and constant love have sustained me throughout my life. 1 1. Introduction 1.1 Background Nitrogen and phosphorus are fundamental elements for the microorganism, plants, animals and human beings growth. The characteristics of global nitrogen cycle can be identified by the perpetuation of a small pool of fixed or combined, nitrogen in continuous exchange with the huge reservoir of atmospheric dinitrogen (N2). The conversion of N2 to fixed nitrogen occurs through microbial nitrogen fixation and industrial nitrogen fixation process; whereas, the only effective process that regenerates Nitrogen is bacterial denitrification (Thamdrup & Dalsgaard, 2002). During the last decade, researchers have figured out that their knowledge of microbial nitrogen cycle and its major participants is far from complete (Jetten, 2008). The global reservoir of fixed nitrogen is controlled by the balance between these sources and sink terms. Methods and practices which affect the availability of fixed nitrogen are substantial director of ecosystem function and global biochemistry because of the fundamental role of nitrogen as a limiting nutrient for primary growth. (Schlesinger, 1997; Codispoti, 1995). The dominant sink for nitrogen and most nitrification occurs in the seafloor, as current aquatic nitrogen resources (Christensen et al, 1994; 140 Galloway et al, 1995; Middelburg et al, 1996). Nitrogen is vital component in the synthesis of protein and it is required in the process of wastewater treatment (Metcalf & Eddy, 2003).In wastewater, ammonia(NH3), ammonium (NH4+), nitrogen gas, nitrite ion (NO2-) and nitrate ion (NO3-)are the most common and significant forms of nitrogen. The nitrogen in fresh wastewater originates from proteinaceous matter and urea. Organic form of nitrogen is changed to Ammonia through breakdown process by bacteria named ammonification. While sewage is traveling through pipes, organic nitrogen converted to ammonia through a process called hydrolysis. During ammonification more ammonium is generated than ammonia; however, the ratio of ammonium to ammonia generation depends on pH and temperature of wastewater. The age of wastewater can be indicated by the amount of ammonia present in the specific wastewater (Metcalf & Eddy, 2003). 2 On the other hand, nitrogen compounds in wastewater play a fundamental role in eutrophication and nitrite enrichment (Wuhrmann, K. 1964). Eutrophication reflects a rise in chemical nutrients (compounds containing nitrogen or phosphorus) in an ecosystem. It results in increase of aquatic plants and algae, dissolved oxygen depletion, increase in blooms of zooplankton, loss of desirable fish species, increases incidences of fish kills, decreases in water transparency, taste, and odour. It can happen in land or in water; nevertheless, the term is usually used to illustrate the increase in the ecosystem\u00E2\u0080\u0099s primary productivity which results in redundant plan growth, decay. Subsequently, impacts such as lack of oxygen and severe reduction in water quality, fish and other animal populations can occur in the ecosystem. Furthermore, high demand for nitrogen in agriculture and industry illustrates that human beings continue to transform the global N-cycle at a high rate (Galloway et al., 2008). Enormous amounts of anthropogenic nitrogen are lost to the environment and cause problems such as rise in fresh water nitrate levels and increase in nitrous oxide production, all of which contribute to global climate change (Duce et al., 2008). The mean concentration of ammonia, which is one of the fixed nitrogen compounds in sewage, for example, is about 40 mg/L NH 4- N and about 20 mg/L org. N. During biological degradation the organic nitrogen is transformed to ammonia. In industrial effluents ,the ammonia concentration is often much higher (Wiesmann, U. 1994) .Furthermore, a big contributor of nitrogen load to the main stream of wastewater treatment plants is an ammonia rich, side stream wastewater that is generated during dewatering of digested sludge (usually referred to as centrate). The centrate contains high concentrations of ammonia as high as 1500 mg/L and accounts for 15-20 % of total nitrogen loaded to the wastewater treatment plants. Therefore, nitrogen needs to be removed from both streams. In effort to reduce water body impairment, more stringent regulations regarding nutrient compounds, are being applied for point source discharges. 3 There are various methods for nitrogen removal, including conventional nitrification/denitrification process, land disposal, pond treatment and biological oxidation in trickling filters or with activated sludge (Wuhrmann, K. 1964). New processes and configurations to remove nitrogen from wastewater have been recently considered. Advanced processes such as Ammonia stripping, breakpoint chlorination, ion exchange, Anammox, de- ammonification, OLAND and nitrification-denitrification by methanotrophs are being developed (Verstraete & Philips, 1998; Metcalf & Eddy, 2003). The development of advance tools to examine and use nitrifiers have appeared in the domain of water and wastewater treatment. 16S rRNA-probes, nitrifier pheromones and online biosensors for ammonium and nitrate are examples of new tools. Moreover, it has been proved that nitrifiers can degraded certain chemicals by means of their radical generating potential which can be used to bring about indirect bio-catalysis. There are a number of bio-supplements which are documented and available in practice, to advance or protecting nitrifiers (Verstraete & Philips, 1998). Significant discoveries such as Anammox, ammonium oxidation by Crenarchaea (AOA) (K\u00C3\u00B6nneke et al., 2005; Francis et al., 2007), the interaction between these groups (Lam et al., 2007), nitrite oxidizing phototrophs (Griffin et al.,2007), nitrate reduction to dinitrogen gas by foraminifera (Risgaard-Petersen et al., 2006) and genome sequencing of several N-cycle organisms (Chain et al., 2003; Starkenburg et al., 2006; Strous et al., 2006; Arp et al., 2007; Stein et al., 2007) provide evidencethat there is a vast biodiversity and metabolic proficiency of nitrogen conversions conceal in the microbial world (Jetten, 2008). Knowledge of microbes involved in nitrogen transformations needs to be improved, to understand and eventually mitigate the negative effects of nitrogen pollution. Based on this background, this research focuses on one of the above mentioned recent discovered processes of the nitrogen cycle: the Anaerobic Ammonium Oxidation (Anammox). Elaboration of the Anammox process, from an unexplored part of biological nitrogen cycle, to text book such as Metcalf & Eddy has occurred since Anammox\u00E2\u0080\u0099s discovery in 1995. It is clear, now, that Anammox bacteria are one of the main role players in the global nitrogen cycle. 4 1.2 Objective of the study This research studied the partial nitrification and Anammox process. The application of the Partial Nitrification and Anammox process was investigated under two different methods for treating municipal dewatered digested sludge liquor (centrate): \u00EF\u0082\u00B7 In Chapter 3, the performance of partial nitrification in a continuous moving bed reactor, followed by Anammox in a hybrid reactor, was studied. \u00EF\u0082\u00B7 In Chapter 4, the performance of partial nitrification in a Sequencing Batch Reactor (SBR) followed by a fixed bed Anammox reactor and hybrid Anammox reactor was studied. The effect of Alkalinity on Partial Nitrification and Anammox process was found in this stage of experiments. \u00EF\u0082\u00B7 In Chapter 5, experiments were conducted to determine the greenhouse gas emission from Partial Nitrification/ Anammox. In this chapter, operational strategy to decrease green house gases was discussed. 1.3 Literature review 1.3.1 Conventional nitrification-denitrification Nitrification processes were special industrial interest until the end of the 19th century, where the process assesses the production of nitrate to make gun powder (Vandenabeele and Verstraete, 1989). Nitrification then has become a fundamental part of soil fertility and a valuable asset for environmental technology. In the early period of development, the main consideration of N-cycle microbiology was to learn and develop fertilizer efficiently in agriculture. The potential of nitrifiers and denitrifiers for nutrient removal from wastewater had not been recognized until the 1960s (Jetten et al. 2009).In the 1980s, the harmful contribution of nitrogen oxides in the atmosphere to destruction of the ozone layer and global warming was recognized. Therefore, the 5 role of nitrification and denitrification in the generation of these substances has become the focus of environmental researchers. The common practice for nitrogen removal is through conventional nitrification and denitrification, where denitrification is achieved by the addition of a carbon source. Nitrification is a two-step biological process, in which ammonia (NH4-N) is oxidized to nitrite (NO2-N) by ammonia oxidizing bacteria (AOB) or Nitrosomonas; then, nitrite is oxidized to nitrate (NO3-N) by nitrite oxidizing bacteria (NOB) or Nitrobacter (Metcalf & Eddy, Inc., 2003).Both Nitrosomonas and Nitrobacter are autotrophic bacteria which use CO2 as a carbon source for biosynthesis and oxidation of nitrogen compounds as the energy source, in order to convert ammonia to nitrate in present of oxygen( Equation1). Nitrifiers are strict aerobes, which means they need free dissolved oxygen to oxidize ammonia. Nitrification requires minimum of 1 mg/L of free dissolved oxygen; thus, under less than 0.5 mg/L, the growth rate is minimal. Nitrifiers, maximum specific growth rate also depends on temperature and pH (Anthonisen, AC 1976). According to previous studies by Downing et al, (1964); Hall, IR Loveless and Painter (1968 and 1983), at a pH in the range of 7-8.2, optimal nitrification rate is achievable. Low activity or no activity blow pH= 6.5 and above pH=10 was reported by Downlng et al, (1964.) and Knowles et al, (1965) indicated that an increase in temperature of 10 \u00C2\u00B0C cause about 3 times the rise in the growth rate. In denitrification, heterotrophic organisms oxidize nitrate to nitric oxide, nitrous oxide, and nitrogen gas in present of organic carbon as an energy source (Equation 2). NH3 + CO2 + 1.5 O2 + Ammonia Oxidizing Bacteria\u00E2\u0086\u0092 NO2- + H2O + H+ (1) NO2- + CO2 + 0.5 O2 + Nitrite Oxidizing Bacteria \u00E2\u0086\u0092 NO3- 5 CH3COOH + 8 NO3\u00E2\u0088\u0092 \u00E2\u0086\u0092 4 N2+ 10CO2+6H20+8OH- (2) Biological nitrogen removal involved both nitrification and denitrification. Alkalinity concentration is an important wastewater characteristic that affect the performance of biological nitrification processes. Alkalinity is needed to achieve complete nitrification (Metcalf & Eddy, 6 Inc., 2003). Although, nitrogen removal via conventional nitrification/denitrification has been practiced in industry for a long time, processes involve the addition of an external organic carbon source for denitrification. Carbon dioxide release a during the process and sensitive bacteria involving in nitrification/ denitrification, are the other downsides tothis process. Centrate treatment through conventional nitrification and denitrification with methanol is not sustainable, as it is costly and releases a high amount of CO2 (greenhouse gas). The new approach for nitrogen removal from centrate is through a new process called anaerobic ammonium oxidation (Anammox) (Strous et al., 1998). Anammox not only offers a cost effective solution for centrate treatment compared with conventional nitrification /denitrification, but it also relies on a different type of bacteria to drive the process. Anammox is a short cut to conventional nitrification/denitrification, where a mixture of ammonia and nitrite is converted to nitrogen gas without the need for organic carbon. 1.3.2 De-Ammonification De-ammonification is the process of ammonium conversion to nitrogen gas without the stochiometric need for the electron donor. In the so called aerobic de-ammonification process, the oxygen supply needs to be controlled carefully. Under very low oxygen pressure (1 kPa or ca. 0.2% O2 in the gas phase) autotrophic nitrifying sludge can produce nitrogen gas (Muller et al. 1995). Hippen et al in (1996) have described de-ammonification process for highly nitrogenous wastewater at the University of Hannover. The maximum rate of ammonia oxidation monitored was 58% at 0.3 kPa dissolved oxygen. However, a practical stable process design was not obtained (Verstraete & Philips 1998) for De-Ammonification. 1.3.3 Anammox 1.3.3.1. Anammox background The general opinion used to suppose that ammonium was an inert molecule under anoxic conditions until the end of 20th century; thus, oxygen was assumed a necessary substance to 7 activate ammonium metabolism as known for nitrifying bacteria (Jetten et al., 2009). However, Broda (1977) predicted the existence of microorganisms which are able to oxidize ammonium with nitrite and nitrate as the electron accepter, based on thermodynamic calculations. Before that, unexpected loss as of ammonium under anoxic conditions was reported by Richards (1965), in studies of a nitrogen balance under anoxic condition. After about thirty years, the Kluyver Laboratory of Biotechnology of Delft (1990) reported a new reaction in which ammonium is converted to nitrogen gas, under anoxic conditions, where nitrate serving as the electron acceptor (van de Graaf et al., 1990). However, it has been discovered later that nitrite is the key electron acceptor (Strous et al., 1997). In 1999,Strous et al. described Anammox bacteria for the first time by physically purifying Anammox cells from a laboratory enrichment culture. He illustrated that Anammox cells convert mixture of ammonium and nitrite into nitrogen gas in the absence of oxygen; Anammox cellular carbon is fixed from only carbon dioxide. \u00E2\u0080\u009CBrocadia anammoxidans\u00E2\u0080\u009D was the name of first Anammox bacterium, and it was given the status of \u00E2\u0080\u009CCandidatus\u00E2\u0080\u009D,because it was not pure according to classical microbiological standards. Anammox cells demonstrate complex cell architecture with a central compartment, similar to other members of the Planctomycetes. Anammox bacteria are phylogenetically related to Planctomycetes (Jetten et al., 2009). Five Anammox species have been indentified so far, with 16S rRNA gene sequence identities of the species ranging between 87% and 99% (Jetten et al., 2009). Four \u00E2\u0080\u009CCandidatus\u00E2\u0080\u009D Anammox species have been confirmed from activated sludge: \u00EF\u0082\u00B7 \u00E2\u0080\u009CKuenenia\u00E2\u0080\u009D (Schmid et al., 2000; Strous et al., 2006), \u00EF\u0082\u00B7 Brocadia\u00E2\u0080\u009D (Strous et al., 1999; Kuenen and Jetten, 2001;Kartal et al., 2008), \u00EF\u0082\u00B7 \u00E2\u0080\u009CAnammoxoglobus\u00E2\u0080\u009D (Kartal et al., 2007) and \u00E2\u0080\u009CJettenia\u00E2\u0080\u009D (Quan et al., 2008), \u00EF\u0082\u00B7 \u00E2\u0080\u009CCandidatus Scalindua\u00E2\u0080\u009D (Kuypers et al.,2003; Schmid et al., 2003; van de Vossenberg et al., 2008), The fifth Anammox genus has often found in natural habitats, especially in the sea floor and marine sediments, under oxygen minimum zones. (Dalsgaard et al., 2005; Penton et al., 2006; Schmid et al., 2007; Woebken et al., 2008). Graaf et al. (1996) demonstrated that the dominant micro-organism of the enrichment culture in Fluidized Bed Reactor (FBR) was Gram-negative, with an unusual and irregular morphology. 8 The cells were single cells or in pair with possibility of dividing latter. They have also observed the color of red for the Anammox culture. Figure 1. Anammox bacteria enriched on nonwoven fabric media at environmental lab (University of British Columbia), the color of the enriched cubes have turned out to red after 6 months The existence of Anammox bacteria has been established in many oxygen limited marine and freshwater systems, worldwide. In the marine ecosystem including oceans, seas, estuaries, marshes, rivers and large lakes over 50% of the N2 gas production may occur by Anammox bacteria( Jetten et al. 2009). As a case in point, in the Black sea, which is one of the largest anoxic basin in the world, hydrogenetic analysis of 16S ribosomal RNA gene sequences illustrates that Anammox microorganism are related to members of the order Planctomycetales. The consumption of ammonium diffusing upwards from the anoxic deep water occurs due to the Anammox process below the oxic zone (Kuypers, et al. 2003). With reference to hylogenetic analysis of 16S ribosomal RNA gene sequences, nutrient profiles, fluorescently labelled RNA probes,15N tracer experiments and the distribution of specific \u00E2\u0080\u0098ladderane\u00E2\u0080\u0099 membrane lipids for the first time, Anammox bacteria have been determined and directly linked to the removal of nitrite, nitrate and ammonium (fixed inorganic nitrogen) in the Black Sea ecosystem by Kuypers et al. ( 2003). The importance of Anammox in the oceanic nitrogen cycle was clarified due to the widespread occurrence of ammonium consumption in suboxic marine. Although the Black Sea is 9 characterized by a high Ammonium concentration in deep waters (up to 100\u00C2\u00B5M), only traces of fixed inorganic nitrogen exist in the suboxic (Kuypers et al. 2003). The phenomenon of apparent ammonium sink in the suboxic zone indicates the anaerobic process of oxidizing ammonium that occurs in presence of the Anammox (Thamdrup & Dalsgaard. 2002). This so-called \u00E2\u0080\u009CAnammox\u00E2\u0080\u009D bacteria (belonging to the order Planctomycetales) directly oxidizes ammonia to N2 with nitrite as the electron acceptor (Kuypers et al.2003). Oxygen absences blow 80m in the water body in the Black Sea; therefore, aerobic nitrification cannot account for the ammonium consumption. 1.3.3.2. Growth and metabolism of Anammox bacteria Fundamental knowledge of Anammox metabolism and gene explanation is highly recommended to optimize and improve the application of Anammox bacteria in the future. Anammox is slow growing bacteria, with a doubling time of 11-20 days (Jetten et al., 2009). According to Strous et al. (1997) Anammox bacteria are strict anaerobes and their metabolism inhibited above 2 \u00C2\u00B5M oxygen. Anammox bacteria obtain their energy for growth from chemolithotrophic conversion of ammonium and nitrite to N2; whereas, bicarbonate plays the role of a sole carbon source for synthesis of cell biomass, which constitute the microorganism autographs. Based on stochiometric calculations and formation of biomass and nitrate in an SBR reactor observed by Strous et al. (1998), it was hypothized that the reducing equivalents for the decrease in CO2 caused by the oxidation of nitrite to nitrate. The low growth rate of Anammox bacteria can be explained by relatively low metabolic activity (15\u00E2\u0080\u009380 \u00C2\u00B5mol of N2 formed per g dry weight of cells per min) (Jetten et al., 2009). The Anammox are chemolithoautotrophic bacteria; however, recent research has disclosed that Anammox bacteria might not be strict chemolithoautrophic specialists, and they could have a more flexible lifestyle. Next to ammonium, the microorganisms are able to use ferrous (Fe2+) and a variety of organic compounds such as carboxylic acids (formate, acetate, propionate, methylamines), as electron donors (Strous et al., 2006; Kartal et al., 2007b; 2008). Aside from nitrite, Fe3+, manganese oxides and nitrate are employed by Anammox bacteria as electron acceptors in their metabolism (Strous et al., 2006). The consumption of nitrate is very interesting, since the same compound in classical denitrification converted into N2 gas but through a different route. First nitrate reduces to nitrite 10 and then in presence of ammonium, alters to N2 by the Anammox mechanism (Kartal et al., 2007a). Therefore, Anammox bacteria are capable of disguising themselves as denitrifiers. 1.3.3.3 Ecology and environmental importance of Anammox bacteria 1.3.3.3.1 Detection of Anammox bacteria in the environment There are suitable available methods for the detection of Anammox bacteria and their activity in natural and man-made environments (Risgaard-Petersen et al., 2003; Schmid et al., 2005). One of the methods which is PCR amplification with general 16S rRNA gene-targeted primers and subsequent phylogenetic analysis of the product used to detect undescribed organisms. Nevertheless, Anammox bacteria might be inadequately represented in general 16S rRNA gene clone libraries because of several mismatches caused by the widely used universal primer set for 16S rRNA gene (Jetten et al., 2009). More specific primer such as Pla46F (a Planctomycete- specific forward primer) or amx386F (an Anammox specific primer) together with a general eubacterial reverse primer or a specific Anammox reverse primer (i.e. amx820R) can increase the amounts of Planctomycete or Anammox 16S rRNA gene sequences relatively (Schmid et al., 2000; 2007; Penton et al., 2006). There is a more functional application of PCR in which primers amplifying Anammox genes used to encode hydroxylamine/hydrazine oxidoreductase (HAO/HZO) proteins. This method illustrates that these genes are suitable targets for molecular ecological studies, on both aerobic and anaerobic ammonium-oxidizing bacteria (Quan et al., 2008; Schmid et al., 2008). Furthermore, rRNA and non-rRNA methods and combination of them are necessary for the purpose of evaluation of the contribution of the Anammox process to nitrogen cycling in any ecosystem. Another excellent apparatus to collect both quantitative and qualitative data of Anammox bacteria is Fluorescence in situ hybridization (FISH). Moreover, FISH can be utilized to approve the findings of colon libraries. As more validated Anammox sequences become applicable, probe designs will advance. Two other enhanced probing techniques which provide the measurement tools to evaluate Anammox activity and growth at single cell level ,are FISH- MAR and ISR probe (Schmid et al., 2001). Raman microscopy (CRM) which is a non-invasive technique used to indentify Anammox bacteria without pretreating the sample. P\u00C3\u00A4tzold et al. 11 (2008) used the resonance Raman effect of cytochrome to report the microbial distribution of nitrifiers and Anammox bacteria in microbial aggregates obtained from biological wastewater treatment. The unique ladderane lipids of Anammox can be utilized as a biomarker (Sinninghe Damst\u00C3\u00A9 et al., 2002; Boumann et al., 2006; Rattray et al., 2008). According to Schouten et al. (2004), lipids from Anammox bacteria are distinguished by substantially lower content 13 C than their carbon source. Consequently, the isotopic composition of Anammox lipids in environmental samples can be an additional confirmation of their origin. While the 13C content of Anammox ladderanes is about 45% depleted, compared to a carbon source, lipids from other autotrophic organisms generally are 20 to 30\u00E2\u0080\u00B0 depleted (Rattray et al., 2008). Moreover, the ladderane lipids method was used by Jaeschke et al. (2008) to identify past Anammox activity. Ladderane lipids analyses on fossil form Arabian Sea fossil suggested that the Anammox process complement a fundamental sink for fixed inorganic nitrogen over last glacial cycle (Jetten et al., 2009). 1.3.3.3.2 Anammox application in wastewater treatment The applications of Anammox bacteria, in combination with partial nitrification by aerobic ammonium-oxidizing bacteria, proposes an attractive alternative to current wastewater treatment system for the removal of fixed nitrogen compounds from wastewater (Jetten et al., 1997; 2001; 2002, Schmidt et al., 2003; Ahn, 2006; Op den Camp et al., 2006). There are several advantages to using Anammox, as opposed to conventional nitrification/ denitrification. 1- The cost of aeration will be much lower for partial nitrification and less sludge will be produced. 2- Denitrification, using Anammox, is carried out by autotrophic bacteria and does not require organic carbon (methanol) for denitrification. 3- Anammox is more environmentally friendly, as the bacteria consume carbon dioxide as carbon source, compared with conventional denitrification, which releases carbon dioxide (greenhouse gas) to the atmosphere. Despite of the fact that Anammox is an attractive option for the nitrogen removal, there are obstacles in the way of industrializing Anammox process. First of all, Anammox has a long doubling time of 11 to 20 days (Strous et al., 1998). Anammox bacteria are also sensitive to pH, temperature and the ratio of nitrite to ammonia which make the operation of the sytem for operators much more difficult. 12 Moreover, Anammox bacteria are washing out from the system; thus, support materials are needed. Anammox bacteria need nitrite as an electron acceptor for oxidizing ammonium anaerobicly. The purpose of design one-reactor and two-reactor systems is providing nitrite, the compound rarely found in wastewater, for Anammox bacteria. There are various reactor systems such as the CANON \u00E2\u0080\u009Ccompletely autotrophic removal of nitrogen over nitrite\u00E2\u0080\u009D, the DEMON pH controlled \u00E2\u0080\u009Cdeammonification\u00E2\u0080\u009D, and OLAND \u00E2\u0080\u009Coxygen limited autotrophic nitrification-denitrification\u00E2\u0080\u009D processes (Kuai and Verstraete, 1998; Third et al., 2001; 2005; Pynaert et al., 2004; Wett, 2006; Vlaeminck et al., 2007; 2008). The Anammox is a two step process and must be combined with a partial nitrification process, where ammonia is partially oxidized to nitrite. Partial nitrification produces a mixture of ammonia and nitrite which serve as the feed to bacteria responsible for the Anammox process. Partial nitrification involves a series of reactions: (1) from NH4+ to NH2OH (hydroxylamine), (2) from NH2OH to N2O, (3) from N2O to NO, and (4) NO to NO2-. The overall reaction of partial nitrification can be expressed by Equation 3: 1 NH4+ + 1 HCO3\u00E2\u0080\u0093 + 0.75 O2 \u00E2\u0086\u0092 0.5 NH4+ + 0.5 NO2\u00E2\u0080\u0093 + 1 CO2 + 1.5 H2O (3) Anammox reaction can be expressed as Equation 4: 1 NH4+ + 1.32 NO2- + 0.066 HCO3- + 0.13 H+ \u00E2\u0086\u0092 1.02 N2 + 0.26 NO3- + 0.066 CH2 O0.5N0.15 + 2.03 H2O (4) In the Anammox process, ammonium is used as electron donor for denitrification and nitrite could also serve as a suitable electron acceptor for the Anammox process, as illustrated in Figure 2, (Graaf et al. 1995). Anammox is an anoxic process in which oxygen causes complete inhibition of the anaerobic ammonium conversion (Strous et al.1997, Graaf et al. 1996). Because of the low growth rate of Anammox bacteria (.001 h-1), support material to attach biomass such 13 as biofilm or media is required; therefore, once there is sufficient amount of biomass accumulating in the system, complete conversion of ammonium occurs (Graaf et al. 1996). Figure 2.Anammox reaction Application of marine Anammox bacteria to remove nitrogen from high stream strength and salty wastewater and different reactor options are currently being studied (Windey et al., 2005; Kartal et al., 2006).Both highly enriched Anammox biomass and an OLAND type mixed AOB- Anammox culture can be adapted to high salt concentrations (up to 3% salt), with a gradual rise of salt content of the influent wastewater (Jetten et al., 2009). Furthermore, up-flow fixed-bed biofilm column reactors, with nonwoven fabric as a media to carry Anammox bacteria were designed to develop high rate Anammox biofilm reactors (Tsushima et al., 2007b). These are explained in Chapters 3 and 5. In an industrial scale, the first Anammox reactor in the world was started with volume of 75 m3 in Rottedam (NL, Abma et al., 2007; van der Star et al., 2007). The reactor which indicates stable performance at 750 kg-N d -1 was scaled up directly from laboratory to full-scale. This stability seems to be a result of the formation of Anammox granules with high densities and high settling velocities. 14 Theoretically, a favourable ratio of nitrite to ammonia is 1.32 for the Anammox reaction. There are several methods to oxidize adequate amounts of ammonia to nitrite, and avoid the formation of nitrate and reach partial nitrification: 1) Increasing free ammonia concentration and free nitric (Anthonisen et al. 1976 & Yamamoto, T. 2008) 2) Decreasing the dissolved oxygen (Wiesmann, 1994), 3) Operating the reactor at temperatures above 25\u00C2\u00BAC (Vazquez-Padin, J 2009). Once free ammonia rises in the reactor, the growth of Nitrite Oxidizing Bacteria (NOB) is limited because of their higher sensitivity to free ammonia inhibition than Ammonia Oxidizing Bacteria (AOB)( Anthonisen et al. 1976). NOB illustrated evidence of inhibition above 0.1 mg/L of free ammonia concentration observed by Anthonisen et al. (1976); they also reported that all nitrifying bacteria indicated inhibition above 0.2 mg/L of free nitric acid concentration. Vadivelu et al. (2006, 2007) investigated that the anabolism of the AOB and the NOB were inhibited completely at 1.3 mg/L and 0.1 mg/L of free ammonia and nitric acid concentrations, respectively. Moreover, the catabolism of the AOB was decreased to 50% at 1.3\u00E2\u0080\u00932.1 mg/L of free nitric acid. However, Turk and Mavinic\u00E2\u0080\u0099s (1989) study demonstrated that NOB can acclimate to inhibition of free ammonia and free nitric acid was suggested as the most potent, long- term inhibitor of NOB by Vadivelu et al. (2007) According to the literature, during pre-treatment of centrate for Anammox process named partial nitrification, the conversion of nitrite to nitrate should be prohibit and the amount of ammonia conversion should be limited to approximately 60%. To reach the ideal point, controlling dissolved oxygen at lower rate can be practiced, since NOB have a lower affinity for oxygen than AOB which cause nitrite accumulation in the reactor under low dissolved oxygen (DO) conditions (Garrido et al., 1997; Ruiz et al., 2003).Moreover, AOB grow faster than NOB above a temperature of 25 \u00C2\u00B0C; as a result, under a low sludge retention time, for example SRT= 1 day, NOB are washed from the system. Nevertheless, once DO control was used for partial nitrification, a significant amount of nitrate was produced since some AOB may be washed out under extremely short SRT. This causes a decrease in nitrite production rate (Yamamoto, T, et al 2008). Therefore, Yamamoto et al (2008) suggested a method of partial nitrification utilizing 15 inhibition of free ammonia and free nitric acid. He also reported (2006) stable partial nitrification in a swim-bed reactor by the inhibition of free nitric acid, in temperatures of 15 \u00C2\u00B0C and 30 \u00C2\u00B0C. Yamamoto et al. (2008) achieved the conversion efficiencies of NH4\u00E2\u0080\u0093N to NO2\u00E2\u0080\u0093N and to NO3\u00E2\u0080\u0093N at about 58% and <5%, respectively, in partial nitrification using inhibition of free ammonia; free nitric acid was applied to swine wastewater digester liquor, and stable treatment was maintained for 120 days. The effectiveness of this process for treatment of the centrate has been illustrated by Yamamoto, T. (2008); Gut et al.,( 2006); Fux et al., (2002); and van Dongen et al., (2001). The mixture of nitrite and ammonia which is partial nitrification effluent can be converted to nitrogen gas by Anammox bacteria (Egli, 2003). The slow growth rate of the Anammox bacteria requires new criteria for reactors to develop and maintain the Anammox culture (Gut, L.et al 2006). Several strategies have been implemented for cultivation of Anammox bacteria, such as Biofilm systems (moving-bed reactor, fixed bed reactor, fluidised bed reactor, gas-lift reactor) or sequential batch reactors (SBR)(Strous et al., 1997; Siegrist et al., 1998; Dapena-Mora et al., 2004). The partial nitrification/ Anammox moving bed biofilm system for partial nitrification was investigated and evaluated in Sweden at two pilot plants: laboratory-scale pilot plant at the Royal Institute of Technology, Stockholm (supplied with supernatant from Bromma WWTP) and a semi-industrial scale pilot plant at Himmerfja\u00C2\u00A8rden WWTP, supplied directly with the supernatant from dewatering of digested sludge (P\u00C5\u0082aza et al., 2002; Szatkowska, 2004; Trela et al., 2004; Gut, 2006). Anammox bacterial cultures were developed on Kaldnes rings, in pilot plants. Vazquez-Padin, J et al (2009) observed that the presence of organic matter up to 50 mg TOC/L activated the ammonia oxidation and allowed the achievement of an effluent with a composition containing nitrite to ammonia molar ratios higher than the stochiometric one. However, they reported that the capacity of ammonia oxidation decreased by higher concentration of organic matter, which lead to lower system efficiency at 1000mg TOC/L of organic matter. The 16 phenomena of the decrease of the ammonia-oxidation capacity was explained by the presence of the crowded cells of heterotrophs, which consumed transported oxygen from liquid bulk to the Anammox reactor and hindered their activities. According to Hanaki et al. (1990) ammonium oxidation efficiency dropped at higher COD concentration for the same SRT but once the COD concentration was controlled at constant levels in the feed, efficiency was returned by increasing the SRT. 17 2. Materials and methods 2.1 Feed Dewatering sludge liquor (centrate) from Lulu Island WWTP in Richmond, B.C., Canada was used for feeding the combined partial nitrification/Anammox process. The anaerobic digester at Lulu digests the combination of primary sludge and waste activated sludge at 38 \u00C2\u00B0C and operates at retention time of approximately 32 days. Centrate contained ammonia ranged from 900~1,000 mg N/L, total organic carbon (TOC) of 150 mg/L and ortho-phosphate of 70 mg P/L. The alkalinity and pH of centrate were 2500 mg/L (as CaCO3) and 7.8 respectively. 2.2 Apparatuses The Partial Nitrification (PN) continuous moving bed reactor: 8-liter plastic cylinder (25 cm I.D. & 17 cm height) filled 2.9 liters of plastic and non-woven fabric moving bed carriers as shown in Figure 3. (See Chapter 3) DO controller: Dissolved oxygen was controlled by a DO controller fabricated at UBC machine shop, as indicated in Figure 4. 18 Figure 3. Partial nitrification reactor on the right side, Anammox reactor on the left side Figure 4. Dissolved oxygen controller 19 The partial nitrification (PN) reactor in the sequencing batch reactor: a 5-liter cylindrical (10 cm I.D. & 60 cm height) (SBR) with the volumetric exchange ratio of 50 %as it shown in Figure 5 (See Chapter 3). Figure 5. Sequencing batch reactor The Anammox process in continuous moving bed biofilm reactor: 11-liter plastic cylinder (25 cm I.D. & 30 height) filled with 4 liters of plastic moving bed carriers (Kaldnes K1) as illustrated in Figure 6 (See Chapter 2). The Anammox process in Hybrid reactor followed by a clarifier: 11-liter plastic cylinder (25 cm I.D. & 30 height) filled with 4 liters of plastic moving bed carriers (Kaldnes K1) as illustrated in Figure 6 (See Chapter 3). The Anammox process in up flow fixed bed biofilm reactor: 3.5-liter plastic cylinder fixed bed reactor (5 cm I.D. & 40cm height) filled with 1.5 liters of non-woven fabric Media as indicated in Figure 6 (See Chapter 3). 20 Figure 6. On the right side the Anammox process in a hybrid reactor, on the left side the Anammox process in an up-flow fixed-bed biofilm reactor PH, Temperature and ORP Monitor: pH, temperature and ORP had been monitored by Oakton pH11 pH/mV/\u00C2\u00B0C meter as it shown in Figure 7. Figure 7.pH, Temperature and ORP monitor Long standing Aquarium Heater: In continuous moving biofilm reactors (Anammox and Partial Nitrification) and fixed bed Anammox reactor heater used to keep temperature at 30 to 35 \u00C2\u00BAC as shown in Figure 8. 21 Figure 8. Aquarium heater 2.3 Sample analysis Following the reactor treatment samples were preserved 2-3 times a week for the following analyses. For all initial untreated samples and treated samples after feeding to reactors, a portion of the total fraction was used for Biochemical Oxygen Demand (BOD5), Total Chemical Oxygen demand(TCOD) , Total Kjeldahl Nitrogen (TKN), Ammonium (NH4-N), Nitrite (NO2- N), Nitrate (NO3-N), TSS. Second portions of the samples were centrifuged at 4000 rpm for 10 mins in a Thermo IEC CL30 rotor and the supernatant filtered using 4.5 \u00C2\u00B5m fiberglass filter to separate the liquid from the solid. The filtrate was analyzed for soluble organic carbon (SOC). The remaining samples were diluted 5 times for alkalinity analysis. All analyses were conducted at the Environmental Engineering Laboratory of the Department of Civil Engineering, UBC using flow injection analysis (Lachat QuikChem 8000 Automated Ion Analyzer). The TS content was determined after a 24-h drying period at 105\u00E2\u0097\u00A6C. COD was determined colorimetrically, using a Hach DR/2000 direct reading spectrophotometer at 600nm. 22 NH3/NH4-N, NO2-N and NO3-N were determined by flow injection analysis of spectrophotometry (Quikchem 8000, Lachat). Total organic carbon (TOC) and total nitrogen (TN) were measured by a TOC/TN analyzer (IL TOC-TN, Lachat). Alkalinity and TSS were determined according to Standard Methods for Examination of Water and Wastewater (Clescerl et al., 2005, Section 2540). N2O off-gas from partial nitrification reactor was monitored by an infrared N2O Monitor (Bacharach, N2O monitor 3010). GC ECD was used for detecting N2O emission from the Anammox reactor. N2 gas was the stripping gas for the reactor. Nitric oxide was measured by a NO analyzer (NOA, Sievers 280i, GE), which applied the technology of ozone- chemiluminescence. Samples were taken by plastic gas-tight syringe from the head space of the reactors, for detection. 23 3. Partial nitrification followed by Anammox in continuous moving-bed biofilm reactors (MBBR) 3.1 Summary This chapter provides partial analytical data to understand whatwas necessary to have stable partial nitrification and Anammox reactions. The process was used to remove ammonia from centrate obtained from a full scale wastewater treatment plant. The partial nitrification was carried out in a continuous, moving-bed, biofilm reactor. The partial nitrification reactor successfully converted approximately 31.7% of ammonia to nitrite. The reasons for the low conversion of ammonium to nitrite were lack of alkalinity in the centrate, low nitrifiers growth rate, and low sludge retention time. Partially nitrified centrate was further fed to a continuous moving bed biofilm Anammox reactor, where the mixture of ammonia and nitrite was converted mainly to nitrogen gas. Subsequent Anammox treatment, after the partial nitrification, resulted in 38.8% additional ammonium removal and nitrite removal of 83.1%. As a result, total ammonia removal in the combined system reached to 79.1% and total nitrogen removal was 56.8 %. The study illustrated alkalinity was found neither controlling nor limiting factor in Anammox reaction. 3.2 Introduction Reject water has a high concentration of ammonium. The level of organic carbon in this type of the wastewater is low; therefore, rejected water is only slightly treated by biodegradation. (Zhang,Li et al., 2010) Partial nitrification/ Anammox process has been considered as an alternative nitrogen removal to conventional nitrification/denitrification in which the reaction does not require addition of H doner such as methanol(Zhang,Li et al., 2010; Fujii et al., 2002; Fux et al., 2002; Schmidt et al. 2003; van Dongen et al., 2001). As a result, the combination of Partial Nitrification and the Anammox process provides a promising method for nitrogen removal from wastewater with low carbon to nitrogen ratio, and a large quantity of ammonium ( Loosdrecht et al., 1998). 24 Stable PN in one aerobic reactor can be combined with anaerobic ammonium oxidation in another tank, to ensure total nitrogen removal through an autotrophic process 1) As a pre- treatment to the Anammox process, about 50% of the influent ammonium can be oxidized to nitrite through the PN process, reducing the amount of oxygen required by almost half 2)Additionally, because Anammox bacteria are autotrophic bacteria, the deammonification process may happen in two steps: the aerobic partial nitrification process and the Anammox process (Gut, L et al. 2006). To maintain a stable partial nitrification, it is necessary to enrich the ammonia oxidizing bacteria (AOB) and limit, inhibit and wash out the nitrite oxidizing bacteria (NOB) (Blackburne et al., 2008a; Peng and Zhu, 2006). Several operational parameters such as dissolved oxygen (DO) concentration, temperature, sludge retention time (SRT), substrate concentration, aeration duration and inhibitors have been proven to ban or washout NOB (Aslan et al., 2009; Peng and Zhu, 2006; Yuan et al., 2008). Current microbiological techniques are not designed to deal with slow growing nitrifiers and Anammox bacteria; however, utilizing biofilm to prevent bacteria washing out from the systems is one the best methods recently introduced. 3.2.1 Objective of this stage of research In this stage of the research, the Partial Nitrification (PN) and Anammox process in moving bed biofilm reactors were studied. The most important goal of this part of research was to understand the metabolic capacities of nitrifiers and Anammox bacteria. The effect of the following parameters on the performance of PN and Anammox were investigated: \u00EF\u0082\u00B7 Dissolved Oxygen in the PN reactor \u00EF\u0082\u00B7 Alkalinity in the PN and Anammox reactors \u00EF\u0082\u00B7 Nitrite to Ammonium ration in the Anammox reactor 25 3.3 Materials and methods 3.3.1 Feed Dewatering sludge liquor (centrate) from Lulu Island WWTP in Richmond, B.C., Canada was used for feeding the combined partial nitrification/Anammox process. The anaerobic digester at Lulu digests the combination of primary sludge and waste activated sludge at 38 \u00C2\u00B0C and operates at retention time of approximately 32 days. Centrate contained ammonia ranged from 900~1,000 mg N/L, total organic carbon (TOC) of 150 mg/L and ortho-phosphate of 70 mg P/L. The alkalinity and pH of centrate were 2500 mg/L (as CaCO3) and 7.8, respectively. Alum was added to centrate for the purpose of sludge precipitation before it was feed to the Partial Nitrification reactor. The effluent from PN (MBBR) was pumped to the Anammox reactor. 3.3.2 Experiment design Figure 9 illustrates the process schematic of the two stage, partial nitrification followed by Anammox, in continuous moving bed biofilm reactors. The partial nitrification (PN) reactor was composed of an 8-liter plastic cylinder (25 cm I.D. & 17 cm height) filled with 2.9 liters of plastic and non-woven fabric moving bed carriers as shown in Figure 3. The Anammox reactor was made of 11-liter plastic cylinder (25 cm I.D. & 30 height) filled with 4 liters of plastic moving bed carriers (Kaldnes K1). The centrate was first partially nitrified in the PN, and the effluent was fed to the Anammox reactor. In the partial nitrification (MBBR) system aeration was provided by a fine diffuser and mixing by an electrical mechanical stirrer. A dissolved oxygen (DO) was controlled by DO controller to keep oxygen level between 1 to 2 mg/L. The temperature was maintained at 30\u00C2\u00B0C to 35 \u00C2\u00B0C. Nitrifiers sludge seed was obtained from enhanced biological phosphorus removal (EBPR) Pilot plant located at the University of British Columbia, BC, Canada. The Anammox reactor contained suspended solids in the liquid and also biomass on the biofilm. The hydraulic retention time (HRT) was changed according to the Anammox performance to 26 prevent nitrite toxicity in the reactor. Temperature was maintained at 30 \u00C2\u00B0C to 35 \u00C2\u00B0C. The sludge seed was originally obtained from the University of Winnipeg\u00E2\u0080\u0099s laboratory and enriched in the reactor at environmental lab at UBC. Figure 9. Schematic of bench scale partial nitrification /Anammox in continuous moving bed biofilm reactors During 8 months period of experiment, the concentration of ammonium in the partial nitrification influent was increased gradually. In fact, the centrate had been diluted before it was fed to the PN reactor. The concentration of ammonium, nitrite, nitrate and alkalinity in the influent and effluent of the PN reactor had been measured for at least 2 times a week. pH, Temperature, DO and ORP had been monitored daily (See Appendix 1). The effluent of the PN reactor was pumped to Anammox reactor after it partially treated in the PN. The flow rate to the Anammox had been monitored and adjusted according to the performance of the Anammox bacteria. The level of nitrite in the Anammox reactor was measured and monitored almost every day to prevent nitrite toxicity in the Anammox reactor. Samples for ammonium, nitrite, nitrate and alkalinity in the influent and effluent of the 27 Anammox reactor had been taken for at least 2 times a week. PH, Temperature, and ORP had been monitored daily (See Appendix 1). Once the Nitrifiers and Anammox bacteria\u00E2\u0080\u0099s performance reached steady state, the effect of Alkalinity on both PN and Anammox reaction and pH on the Anammox process were studied. Furthermore, the effect of nitrite to ammonium ratio in PN effluent on the Anammox reactor was investigated. To control the pH at desired levels, sulphuric acidwas used. 3.3.3 Chemical analysis NH3/NH4+, NO2- and NO3- were determined by flow injection analysis of spectrophotometry (Quikchem 8000, Lachat). Total organic carbon (TOC) and total nitrogen (TN) were measured by a TOC/TN analyzer (IL TOC-TN, Lachat). Alkalinity, MLSS and TS were determined according to Standard Methods for Examination of Water and Wastewater (Clescerl et al., 2005, Section 2540). For the purpose of daily monitoring of nitrite, nitrate and ammonium to prevent nitrite toxicity in the Anammox reactor quick test kits were utilized, as shown in Figure 10. Figure 10. Ammonium, nitrate and nitrite test kits (UBC Environmental Lab) 28 3.4 Results and discussion As mentioned before, understanding the metabolic capacities of the nitrifiers and Anammox bacteria, to find design criteria and tune the operational conditions was the main purpose of this stage of research. This stage was the beginning of the understanding of what is necessary to design a stable, Anammox reactor system. 3.4.1 Performance of the partial nitrification in the continuous moving bed biofilm reactor The PN reactor converted more than 31% of ammonia in the centrate to nitrite. The effluent of PN reactor, shown in Figure 11, contained 59.7% ammonium, 31.7 % nitrite and 8.5 % nitrate and gaseous products such as nitrous oxide and nitrogen, as initial nitrogen load. The Ratio of Nitrite to Ammonium in the PN effluent was equal to 0.53. 59.7% 31.7% 8.5% Ammonium Concentration% Nitrite Concentration% Nitrate,Nitrous Oxide, Nitric Oxide & Nitrogen Gas Emission Figure 11. Ammonium, nitrite, nitrate, nitric oxide and nitrogen gas in the PN reactor 29 3.4.1.1The effect of dissolved oxygen on the performance of the partial nitrification reactor Achieving higher pollutant removal, with less energy consumption, has always been considered by wastewater treatment plant designers. There are various biological technologies and processes which have been developed for nitrogen removal from wastewater. Meanwhile, partial nitrification has been considered as one of the most cost effective and sustainable pre-treatment for the Anammox process. Compared with conventional nitrification/ denitrification, partial nitrification combined with Anammox process not only consumes 25% less oxygen in aeration step, but also decreases 40% of the carbon source cost in denitrification step (Turk and Mavinic, 1987; Turk and Mavinic, 1989). DO concentration and aeration duration are feasible control parameters (See Chapter 3) to have stable and more cost effective partial nitrification. As a result, in this stage of research, a DO controller (Figures 7) had been designed by electricians at UBC to control the level of DO less than 2 mg/L. DO concentration is also one of the important parameters which can inhibit and wash out NOB microorganism in the PN. In the PN reactor DO less than 2 mg/L perfectly controlled the growth of NOB since the production of nitrite was limited to less than 9 % of total ammonium load (Figure 11). Theoretically, the reaction of Anammox requires 1 mole of NH4+ and 1.32 mole of NO2- according to Equation 4. The goal of partial nitrification was to convert sufficient ammonium to nitrite to reach nitrite to ammonium ratio of 1.32, favourable for Anammox reaction. However, the partial nitrification was achieved with nitrite to ammonium ratio of 0.53 in this stage of the research. The low conversion of ammonium to nitrite can be explained by different parameters in general such as lack of alkalinity in the centrate, low nitrifiers growth rate, and low sludge retention time. Low nitrifiers growth rate in moving bed biofilm reactor was the reason for the results of PN in this research; this led the researcher to conduct a short term of the experiments to find the best method for the PN. The results of these experiments illustrated that the nitrifying sludge in the reactor is the most efficient and cost effective methods for the PN. Another reason could be the polymeric organic coagulant that remained in the water phase attached to the 30 nitrifiers\u00E2\u0080\u0099 biofilm, causing the decrease innitrifiers activity .Therefore, this preliminary research suggested that suspended solids should be removed physically, without the addition of chemicals. It was also shown in this research that energy savings, by low DO in PN would be technically feasible. The consumption of alkalinity had been monitored in PN reactor (See Appendix 1), and as expected, alkalinity had been consumed in the PN reactor. 3.4.2 Performance of the Anammox process in the continuous moving bed biofilm reactor During the 8 months of Anammox enrichment, the reactor content gradually turned red. The moving bed reactor enrichment cultures resulted in the growth of Anammox bacteria as biofilm aggregates. As such, nitrogen gas bubbles were observed between biofilms in the reactor, which was an indication of proper Anammox reaction. Subsequent Anammox treatment, after Partial Nitrification, resulted in 38.8% additional ammonium removal and nitrite removal of 83.1 %. As a result, total ammonia removal in the combined system reached 79.1% and total nitrogen removal was 56.8 %. As mentioned before, the reaction of Anammox requires 1 mole of NH4+ and 1.32 mole of NO2- according to Equation 4. Once PN reactor produced the adequate feed for Anammox reaction, the Anammox reactor performed more effectively. (See Appendix 1) Experimental work illustrated that once the Anammox reaction was working properly ,the pH of the reactor had increased. However, perfect pH for the Anammox reaction is 7 to 7.5. As a result, a pH controller which connected to both Anammox reactor and a bottle of .1 N sulphuric acid was designed to maintain the pH between to 7 to 7.5. 31 Alkalinity was monitored through 8 months experiments in the influent and effluent of the Anammox reactor. This showed that the Anammox reaction consumed a very little amount of alkalinity which matches perfectly with the Anammox reaction formula (Equation 4). This stage of the research provided the beginning of our understanding of what is necessary to have stable partial nitrification, in order to achieve perfect Anammox reaction. 32 4. Partial nitrification in sequencing batch reactor followed by Anammox 4.1 Summary This chapter presents the operational strategy for nitrogen removal in a two-stage, partial nitrification coupled with anaerobic ammonium oxidation (Anammox) process. The process was used to remove ammonia from centrate obtained from a full scale, wastewater treatment plant. The partial nitrification was carried out in a sequencing batch reactor (SBR) .The partial nitrification reactor successfully converted approximately 49.5\u00C2\u00B11.0% of ammonia to nitrite. Alkalinity was investigated as a limiting factor to convert more ammonia to nitrite in partial nitrification. Moreover, under higher dissolved oxygen required cycle time for partial nitrification reaction reduces for centrate treatment. In fact, for the same volume shorter time was needed for partial nitrification process once the SBR was operated under higher dissolved oxygen. Partially nitrified centrate was further treated in two Anammox reactors, where the mixture of ammonia and nitrite was converted mainly to nitrogen gas. Anammox treatment was carried out in two different Anammox reactors: a moving bed Hybrid reactor and Up Flow Fixed-Bed biofilm reactor. The Hybrid Anammox reactor removed an average of 55.8% of NH4- N, versus 48.3% NH4-N removal in the Up Flow Fixed-Bed reactor. Nitrite removal in the Hybrid and Fixed-Bed Anammox reactors averaged 80.8% and 62.5%, respectively. The study illustrated that, in both Anammox reactors, the best Ammonia removal happens in Nitrite to Ammonium ratio between 1.35 and 1.45. As such, alkalinity was found to neither control nor limit the Anammox reaction. 4.2 Introduction New technologies have been developed to deal with high nitrogen loads; most of the enhanced technologies are based on the Anammox process. The First step of the process is producing adequate influent for the Anammox reaction. Theoretically, a favourable ratio of nitrite to ammonium for the Anammox process is 1: 1. 32; therefore, ammonium has to be partially oxidized to nitrite in the first step. An economic proven way for treatment of nitrogen rich effluent is partial nitrification which reduces the dissolved oxygen and external organic carbon requirements, compared to the conventional nitrification / denitrification process (Pambrun et al 33 2006). To maintain a long-term stable partial nitrification, nitrite accumulation is one of the most serious issues. The common method for the partial nitritation is the SHARON process which is based on a chemostat operating at a high temperature (35 \u00E2\u0097\u00A6C) without biomass retention (Ganigue et al., 2007). In SHARON, by controlling sludge retention time and hydraulic retention time at equal values, to 1.5 days, nitrite oxidizing bacteria (NOB) are washed out of the system to prohibit nitrate production (Ganigu et al., 2007). Nonetheless, sequencing batch reactors or biofilm airlift reactors can be an alternative technology, where nitrite oxidizing bacteria are out competed from the process by limitation of dissolved oxygen or inhibition by free ammonia and/or free nitrous acid. (Garrido et al., 1997; Ruiz et al., 2003; Ganigue et al., 2007). According to Ganigue\u00C2\u00B4 et al (2007) sequencing batch reactor (SBR) is shown a feasible technology to achieve adequate influent for the Anammox reactor, since SBR technology is more flexible and controllable. In addition, sludge retention time (SRT) ranging from 3 to 10 days may enhanced process performance and make the system more resistant to possible loading shocks.(Ganigue et al., 2007). There are different strategies to operate sequencing batch reactors: 1) Short feeding event at the beginning of the cycle, which is one of the simplest cycle designs and it is efficient for low to medium nitrogen loads treatments (Gal\u00C3\u00AD et al,. 2007; Pambrun et al.,2006).2) Step-feed strategy, based on different feeding event which is suitable in systems which have various reaction phases or once dealing with higher nitrogen concentration in the batch reactor( Fux et al., 2003) . 3) Fed-batch strategy, where the influent is supplied through the entire cycle used in full-scale SBR plants treating high nitrogen loads (Fux, C. 2006). However, an efficient cycle definition depends on three important parameters, first, wastewater characteristics, second, the goal of the process and third, the technical requirements/ limitations. One of the main goals of this step of the research was evaluating SBR process with short feeding event at the beginning of the cycle for partial nitrification, treating high-ammonium content centrate from the Lulu Island waste treatment plant. 34 A second step to complete nitrogen removal is the Anammox process. Anammox has many advantages, such as minimal green house gases production, saving energy and high efficiency compared with the conventional biological nitrogen removal; however, slow growth rate of the Anammox bacteria is a challenging issue to be solved. The application of Anammox bacteria in bioreactor requires strictly controlled environments, nitrite to ammonia ratio and reactor configuration (Zhang, L et al., 2010). In order to address the issue of long doubling time, approximately 11 day (Strous et al., 1998), a long cultivation to generate a sufficient amount of Anammox sludge is required. Therefore, many researchers have started to define suitable design criteria for the Anammox sludge. The use of biomass carrier for the attachment of slow growing Anammox sludge, to prevent the bacteria being washed out from the system,seems a promising option to many researchers. The feasibility of non woven fabric carrier and plastic biofilm to cultivate Anammox sludge was investigated, using up-flow fixed-bed and hybrid reactors. 4.2.1 Objective of this study In this study, the Partial Nitrification (PN) was carried out in the Sequencing Batch Reactor (SBR) which followed by the Anammox process in two Hybrid and Up Flow Fixed-Bed reactors. The following objectives are summarized: \u00EF\u0082\u00B7 Evaluate SBR process with short feeding event at the beginning of the cycle for Partial Nitrification \u00EF\u0082\u00B7 Study the feasibility of the Anammox application in the Hybrid and Up Flow Fixed Bed reactor The effect of following parameters on the Partial Nitrification and Anammox reactors were investigated: \u00EF\u0082\u00B7 The Level of dissolved oxygen concentration in the PN reactor \u00EF\u0082\u00B7 pH and Alkalinity in the PN reactor \u00EF\u0082\u00B7 Feeding Pattern in the PN process \u00EF\u0082\u00B7 The ratio of Nitrite to Ammonium on the Anammox process 35 \u00EF\u0082\u00B7 Alkalinity in the Anammox reactors 4.3 Materials and methods 4.3.1 Feed Dewatering sludge liquor (centrate) from Lulu Island WWTP in Richmond, B.C., Canada was used for feeding the combined partial nitrification/Anammox process. The anaerobic digester at Lulu digests the combination of primary sludge and waste activated sludge at 38 \u00C2\u00B0C and operates at a retention time of approximately 32 days. Centrate contained ammonia ranged from 900~1,000 mg N/L, total organic carbon (TOC) of 150 mg/L and ortho-phosphate of 70 mg P/L. The alkalinity and pH of centrate were 2500 mg/L (as CaCO3) and 7.8, respectively. Alum was added to the centrate for the purpose of sludge precipitation, before it was feed to the Partial Nitrification reactor. The effluent from PN (SBR) was diluted and pumped the Anammox reactors. 4.3.2 Experimental design Figure 12 illustrates the process schematic of two stage partial nitrification in the SBR followed by Anammox in two reactors: 1) Hybrid reactor, 2) Up-Flow Fixed Bed reactor. The partial nitrification (PN) reactor was composed of a 5-liter cylindrical (10 cm I.D. & 60 cm height) sequencing batch reactor (SBR) with the volumetric exchange ratio of 50 % (Figure 5). The hybrid Anammox reactor was made of 11-liter plastic cylinder (25 cm I.D. & 30 height) filled with 4 liters of plastic moving bed carriers (Kaldnes K1). The Up-Flow Fixed-Bed Anammox reactor was composed of 3.5-liter plastic cylinder fixed bed reactor (5 cm I.D. & 40cm height) filled with 1.5 liters of non-woven fabric media, as indicated in Figure 6. The centrate was first partially nitrified in the PN, and the effluent was transferred to a transfer tank and then diluted and fed to the Anammox reactor. In the SBR, aeration was provided by a fine air diffuser, and mixing of the liquor was by an electrical/mechanical stirrer. A laptop computer loaded with LabView software was used to 36 control and monitor the system. The SBR was operated at a cycle of 8 hr: 10 min of feeding, 7 hr and 10 min aeration, 30 min settling and 10 min decant. The dissolved oxygen (DO) and temperature were maintained at 2 mg/L and 20\u00C2\u00B12 \u00C2\u00B0C, respectively. The sludge retention time (SRT) was kept at 10 days, to maintain mixed-liquor suspended solids (MLSS) at a concentration of 1,650 mg/L. Sludge seed was obtained from the enhanced biological phosphorus removal (EBPR) pilot plant, located at the University of British Columbia (UBC), BC, and Canada. The hybrid Anammox reactor contained 1,300 mg/L solids, accounting for suspended solids in the liquid and also biomass on the biofilm. The hydraulic retention time (HRT) and temperature were maintained at 26 hr and 30\u00C2\u00B12 \u00C2\u00B0C, respectively. A settler removed the bio-solids from the effluent and returned almost all of them to the Anammox reactor. The sludge seed was originally obtained from the University of Winnipeg and enriched in the reactor for more than 6months before the experiment. The up-flow fix-bed reactor contained Anammox sludge which was cultivated on the fabric biofilm in previous stage. The average of HRT was equal to 7.78 in the up flow fixed bed reactor, which gradually was decreased according to the Anammox reaction. During the experiments, samples were taken 3 times a week, each time twice in the morning and afternoon, from reactors in order to determine NH3/NH4+, NO2- and NO3- , TOC, TKN, MLVSS and alkalinity. 37 Figure 12. Schematic of bench scale partial nitrification in sequencing batch reactor followed by Anammox in two reactors In the PN reactor, Nitrite to Ammonia ratio base line was determined at initial pH=7.8, DO 1.5~2.5 mg/L and 20\u00C2\u00B0C. Once the base line was determined, the impact of controlled operating parameters including DO (0.5, 1, 2, and 4 mg/L), pH (6, 6.6, 7.2, and 7.8) and feeding regime on the PN performance were investigated. Hydrochloric acid and sodium hydroxide were used to control the pH at desired levels. To study the effect of feeding pattern on ammonium oxidation rate in the PN reactor, four experiments were conducted. The total feed volume in each cycle of partial nitrification reactor was 2.5 liters. In the first experiment 100 % of total feed volume (2.5 L) was pumped into the reactor in 10 min; whereas, in the second one 60% of total feed volume was pumped into the reactor in 6 minutes and the remaining 40% was pumped slowly in 40 minutes. Regarding the third experiment, 30% of the total feed volume was loaded at 3 minutes and the rest of the 38 operating capacity introduced to the reactor in 70 minutes. In the last experiment, 100% of the feed was pumped to the partial nitrification reactor slowly and evenly at a rate of 25 ml/min within one hour. The effluent of the PN reactor was pumped to the Anammox reactor while it had been partially treated. The flow rate to the Anammox had been monitored and adjusted according to performance of the Anammox bacteria. The level of nitrite in the Anammox reactor was measured and monitored every day to prevent nitrite toxicity in the Anammox reactors. Samples for ammonium, nitrite, nitrate and alkalinity in the influent and effluent of the Anammox reactor had been taken at least 2 times a week. pH, Temperature, and ORP had been monitored daily (See Appendix 3). For the Anammox reactors the concentration of ammonium plus nitrite was controlled at 100mg/L of N. Nitrite to ammonia ratio less than1 in the influent was considered as a base line. After that, parameters including nitrite to ammonia ratio (1-1.25, 1.25-1.35, 1.35-1.45 and more than 1.45) and external Alkalinity were studied, where NaHCO3 and NaNO2 was added to the Anammox feed to control Nitrite to ammonium ratio and alkalinity at desired levels in the Anammox reactors. 4.3.3 Chemical analysis NH3/NH4+, NO2- and NO3- were determined by flow injection analysis of spectrophotometry (Quikchem 8000, Lachat). Total organic carbon (TOC), total soluble organic carbon (SOC) and total nitrogen (TN) were measured by a TOC/TN analyzer (IL TOC-TN, Lachat). Alkalinity, MLSS and TS were determined according to Standard Methods for Examination of Water and Wastewater (Clescerl et al., 2005, Section 2540). For the purpose of daily monitoring of nitrite, nitrate and ammonium to prevent nitrite toxicity in the Anammox reactors quick test kits were utilized, as shown in Figure 10. 39 4.4 Results and discussion 4.4.1 Performance of the partial nitrification/Anammox process The Partial Nitrification reactor (SBR) successfully converted more than 45% of the ammonia in the centrate to nitrite, after partial nitrification (PN). The effluent of PN reactor contained 45.1% ammonium, 45.1% nitrite and 1.9% nitrate as initial nitrogen load. The Hybrid Anammox reactor removed an average of 55.8% of NH4-N versus 48.3% NH4-N removal in the fixed bed reactor. Nitrite removal in the hybrid and fixed bed Anammox reactor averaged 80.8% and 62.5%, respectively. 4.4.2 Partial nitrification in the sequencing batch reactor According to Anammox reaction equation (Equation 4), the reaction of Anammox requires 1 mole of NH4+ and 1.32 mole of NO2-. The main objective of partial nitrification was to produce stable effluent with the appropriate nitrite to ammonium ratio for the Anammox step. However, lack of alkalinity in centrate prevented partial nitrification to reach this ideal ratio.Ammonium oxidation rate (AOR) slowed down over the time due to alkalinity limitation and the system hardly achieved the ideal point (Figure 13). As a result, In the SBR reactor, the nitrite to ammonia ratio equal to 1 was used a base point for comparing nitrogen conversion rates at different operation conditions. To determine the base point, pH was monitored in the process. Under base line condition, pH=7.8, DO=1.5~2.5 mg/L and 20\u00C2\u00B0C ,after approximately 300 min of aeration, ammonia to nitrite ratio reached 1. Figure 13 indicates the typical time profile of nitrogen species in the partial nitrification reactor under baseline conditions. In Figure 14, pH changes are shown over an 8 hour life cycle in the PN. Ammonia nitrogen in the centrate was mainly converted nitrite so that the effluent of PN reactor contained 47.3% nitrite and 1.4%% nitrate, as it is shown in Figure 13. Figure 14 indicates the pH profile during the PN reactor cycle. When the pH decreased to 5.8, nitrite concentration levelled off and ammonium to nitrite ratio reached 1. From this point forward, NH4-N barely converted to NO2-N under base line conditions. 40 Figure 13.Nitrogen species in the partial nitrification reactor over an 8-hour Cycle under base line conditions 41 Figure 14. pH measurement in the partial nitrification reactor over an 8 hour cycle under base line conditions 4.4.2.1 Partial nitrification under dissolved oxygen- DO controlled condition The SBR was operated under controlled dissolved oxygen between 0.5 to 4 mg/L, to investigate the effect of DO concentration on Ammonium Oxidation Rate (AOR). Figure 15 indicates the nitrogen species in partial nitrification reactor under DO equal to 0.3-0.5 mg/L. As it can be seen clearly, under low DO condition, after 450 min, the SBR reached an ideal base point of nitrite to ammonium ratio equal to 1. However, Figure 16 shows that once SBR was operated under DO=3-4 mg/L conditions, the base point were achieved at 160 min. 42 Figure 15. Nitrogen species in the partial nitrification reactor over an 8-hour cycle, level of dissolved oxygen controlled between 0.3 and 0.7 mg/L 43 Figure 16. Nitrogen species in the partial nitrification reactor over an 8-hour cycle, level of dissolved oxygen controlled between 3.5 and 4.5 mg/L Higher DO resulted in higher average Ammonium Oxidation Rate (AOR). AOR was measured as 36.6 NH4+-N/hr/g biomass at DO of 4 mg/L, decreasing to AOR of 17.1 NH4+-N/hr/g biomass at DO of 0.5 mg/L. As a result, higher DO in SBR reactor reduces the required cycle time of partial nitrification used for centrate treatment. Nevertheless, operating the PN reactor at a higher dissolved oxygen may raise the concern of nitrate production by Nitrite Oxidizing Bacteria (NOB), thus decreasing the efficiency of a subsequent Anammox treatment. Ammonium oxidizing bacteria (AOB) have been shown to have a higher affinity for oxygen than nitrite oxidation bacteria (NOB); therefore, high DO condition may promote the growth of both AOB and NOB (Schmidt and Bock, 1997; Jayamohan et al., 1988). It is generally accepted that for low ammonia wastewaters, a relatively low DO (<1 mg/L) has to be maintained to attain successful partial nitrification (Zeng et al., 2003; Wyffels et al., 2004). However, for treatment 44 of high ammonia wastewaters, (such as centrate), the growth of Nitrite Oxidizing Bacteria (NOB) at high DO is not a concern. As an example, the full scale partial nitrification at Dokhaven-Sluisjesdijk WWTP was operated at a DO level of 3 mg/L and nitrite was hardly converted to nitrate in long term treatment (Kampschreur et al., 2008). Bernet\u00E2\u0080\u0099s et al. (2005) reported free ammonia as the main factor inhibiting the growth of NOB even at higher DO values. High concentration of nitrite (higher than 200 mg/L) has also been considered toxic to organisms including NOB (Meinhold et al., 1999; Wyffels et al., 2004). 4.4.2.2 Partial nitrification under pH-controlled conditions In the partial nitrification reactor, Ammonium oxidation rates showed sensitivity to the pH level. As it is shown in Figure 17, once SBR operated under controlled pH at 7.2 after approximately 200 min, the reaction reached base point of nitrite to ammonium equal to 1; whereas, neither in a pH controlled at 6.6 nor 6, was the base point achieved (Figure 18, 19). Specific Ammonium oxidation rate (AOR) slowed down from 26.4 NH4+-N/hr/g biomass at pH 7.2 to 10.1 NH4+-N/hr/g biomass at pH 6. Alkalinity destruction, due to acid addition, for low level pH control experiments probably led to limited nitrification. 45 Figure 17. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; pH controlled at 7.2 by additional sodium hydroxide 46 Figure 18. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; pH controlled at 6.6 by additional hydrochloric acid 47 Figure 19. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; pH controlled at 6 by additional hydrochloric acid 4.4.2.3 Partial nitrification under continuous feeding conditions Figure 20 indicates that the PN reactor reached the base point after approximately 240 minutes of aeration, while centrate was pumped to the reactor evenly and slowly at the rate of 25 ml/min in 100 minutes. On the other hand, once the PN was fed at the rate of 250 ml/min in 10 minutes, the nitrite to ammonium ratio in the reactor was equal to 1 after 350 minutes (Figure 23). Figure 21 and 22 confirmed the point that the ammonium oxidation rate increased when feed was pumped into the reactor slowly and evenly. 48 Figure 20. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed slowly at the rate of 25 ml/min in 100 minutes 49 Figure 21. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed fast at the rate of 250 ml/min for 3 minutes, then centrate was pumped slowly at the rate of 25 ml/min for 70 minutes 50 Figure 22. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed fast at the rate of 250 ml/min for 6 minutes, then centrate was pumped slowly at the rate of 25 ml/min for 40 minutes (how come nitrate and nitrate and nitrite are fluctuating ) 51 Figure 23. Nitrogen species in the partial nitrification reactor over an 8-hour cycle; the SBR was fed fast at the rate of 250 ml/min for 10 minutes When continuous slow feeding was applied to the PN reactor, the biomass was exposed to reduced ammonium concentration and alkalinity was provided more evenly for the reaction; whereas, pH levels were hardly changed during each cycle. Distribution of alkalinity druing the experiment resulted in higher AOR, which is suggested by researchers as a practical operation strategy to reduce the partial nitrification cycle. 52 4.4.3 Anammox in hybrid reactor and up-flow fixed-bed reactor In the Anammox process, ammonium is used as electron donor for denitrification and nitrite could also serve as a suitable electron acceptor. As a result, nitrite to ammonia ratio in the influent plays an important role in the Anammox reaction. However, the slow growth rate of Anammox bacteria is another fundamental parameter in nitrogen species removal from the centrate. To compare results of both reactors, nitrite to ammonia ratio equal to 1(R=1) in the Anammox influent was considered as a base line. According to Equation 4 (Chapter 1) Anammox reaction needs 0.066 mole of HCO3- for each mole NH4+ to be converted to N2. Therefore, alkalinity remaining in the PN effluent is enough for the Anammox reaction. Under base line conditions, R=1, T=30\u00C2\u00B0C, HRT= 26 hours, in the Hybrid Anammox reactor, average of ammonium and nitrite removal was 55.8% and 80.8%, respectively. In the up-flow fixed-bed Anammox reactor with HRT= 7.78, average of 65.2% of NO2-N removal was achieved versus 48.26% NH4-N removal. Experiments were conducted at controlled nitrite to ammonium ratios, to investigate the most suitable ratio for the Anammox reaction. As it shown in Figure 24, the best ratio for ammonium removal in the hybrid reactor is between 1.35 and 1.45; however, for the up-flow fixed-bed reactor, R between 1.25 and 1.35 had the best average ammonium removal (Figure 27). The best average of total nitrogen removal in the hybrid Anammox reactor was achieved once R was controlled in the range of 1 to 1.25 (Figure 26) ;whereas, up-flow fixed-bed reactor showed the same result as ammonium removal in which R was maintained between 1.25 and 1.35 (Figure 29). 53 Figure 25 and 28; indicate average of nitrite removal in the hybrid Anammox and up-flow fixed- bed Anammox reactors in 5 different nitrite to ammonium ratios. Nitrite removal in the up-flow fixed bed reactor showed that the best ratio was again, 1.25 to 1.35. Druing the experiments, the up-flow fixed-bed reactor showed more stability than the hybrid reactor despite, lower hydraulic retention times compared with the hybrid reactor. Figure 24. Average of ammonium removals in the hybrid Anammox reactor in 5 different nitrite to ammonium ratios 54 Figure 25. Average of nitrite removals in the hybrid Anammox reactor in 5 different nitrite to ammonium ratios 55 Figure 26. Average of total nitrogen removals in the hybrid Anammox reactor in 5 different nitrite to ammonium ratios 56 Figure 27. Average of ammonium removals in the up-flow fixed-bed Anammox reactor in 5 different nitrite to ammonium ratios 57 Figure 28. Average of nitrite Removals in the up-flow fixed-bed Anammox reactor in 5 different nitrite to ammonium ratios 58 Figure 29. Average of total nitrogen removals in the up-flow fixed-bed Anammox reactor in 5 different nitrite to ammonium ratios Soluble organic carbon measurements in the influent and effluent of the hybrid and up-flow fixed-bed reactor illustrated no significant concentration difference which is an indicator of no heterotrophic reaction in both reactors. These experiments also were conducted at controlled alkalinity; however, there was no evidence that showed Anammox reaction depends on alkalinity. 59 5. Greenhouse gases (nitrous oxide and nitric oxide) emission from partial nitrification and Anammox system 5.1 Summary This chapter presents the operational strategy for reducing nitrous oxide (N2O) and nitric oxide (NO) emissions from a two-stage, partial nitrification coupled with anaerobic ammonium oxidation (Anammox) process. The process was used to remove ammonia from centrate obtained from a full scale wastewater treatment plant. The partial nitrification was carried out in a sequencing batch reactor (SBR), followed by Anammox treatment in a moving bed biofilm reactor. The partial nitrification reactor successfully converted approximately 49.5\u00C2\u00B11.0% of ammonia to nitrite. Partially nitrified centrate was further treated in an Anammox reactor where the mixture of ammonia and nitrite was converted mainly to nitrogen gas resulting in total nitrogen removal of 53.6%. The emissions from partial nitrification were, 2.6\u00C2\u00B10.2% N2O and 0.6\u00C2\u00B10.3% NO as nitrogen load ; Anammox, with 0.15% N2O and 0.0002% NO, showed relatively lower emissions compared to partial nitrification. In the partial nitrification reactor, higher dissolved oxygen (DO) decreased N2O emission by 67% without impacting NO emission. Under pH controlled conditions, lower pH dramatically affected N2O and NO emissions from the PN reactor, where N2O emission at pH=6.6 was 36% higher than pH=7.8. The Feeding regime into the PN reactor did not significantly affect N2O emission; however, it reduced NO emission by approximately 10%. 5.2 Introduction Nitrogen discharge regulations are becoming more stringent in North America and many wastewater treatment plants are striving to reduce their nitrogen discharge to the water bodies. A big contributor of nitrogen load to the main stream of wastewater treatment plants (WWTP) is the ammonia rich side stream wastewater, usually referred to as centrate, that is generated during dewatering of digested sludge. The centrate contains high concentrations of ammonia as high as 1500 mg/L and accounts for 15-30 % of total nitrogen loaded to the wastewater treatment plants. The common practice for side stream centrate treatment is through conventional-nitrification and denitrification, where denitrification is achieved by the addition of methanol (Zhiquan Yang et al., 2009). Centrate treatment through conventional nitrification and denitrification with 60 methanol is not sustainable, as it is costly and releases high amount of CO2 (Greenhouse gas) to the atmosphere. The new approach for nitrogen management from centrate is through a new process called anaerobic ammonium oxidation (Anammox) (Strous et al., 1998). Anammox offers a cost effective solution for centrate treatment, as opposed to conventional nitrification /denitrification, and relies on different type of bacteria to drive the process. Anammox is a short cut to conventional nitrification/denitrification, where mixture of ammonia and nitrite is converted to nitrogen gas, without the need for organic carbon. There are several advantages of using Anammox, as opposed to conventional nitrification/denitrification. 1) The cost of aeration will be much lower for partial nitrification and less sludge will be produced. 2) Denitrification using Anammox is carried out by autotrophic bacteria and does not require organic carbon (methanol) for denitrification. 3) Anammox is more environmentally friendly as the bacteria consume carbon dioxide as carbon source as opposed to conventional denitrification, which releases carbon dioxide (Greenhouse gas) to the atmosphere. Although nitrogen gas is the theoretical gaseous product of partial nitrification/Anammox (PN/Anammox) process, N2O and NO emissions have been reported in practice from partial nitrification Anammox reactors (Zumft et al., 1993; Zheng et al., 1994; Stuven et al., 2001; Kampschreur et al., 2008). Kampschreur et al. (2008) reported N2O emission of 1.7% and 0.3% as the initial ammonia from a full scale partial nitrification and Anammox reactor, respectively, while NO emissions were 0.2% and 0.003% of ammonium load. Van der Star et al. (2007) reported negligible N2O emission from the Anammox reactor. 5.2.1 Objective of this study Although emissions from PN/Anammox process have been quantified, there is no research that reports the strategies to reduce N2O during the treatment. This is particularly important due to the fact that N2O is one of the greenhouse gases and its global warming potential is approximately 300 times the impact of carbon dioxide (ICCP, 2007). In this study, N2O and NO emissions from a bench scale partial nitrification sequencing batch reactor (SBR), coupled with a biofilm Anammox reactor treating dewatered digested sludge liquor (centrate), were examined. The specific objectives of this study were: 61 \u00EF\u0082\u00B7 Quantify N2O and NO emissions from both partial nitrification and Anammox reactor under various operating conditions \u00EF\u0082\u00B7 Define a practical operational strategy to reduce N2O and NO emission from partial nitrification and the Anammox process. 5.3 Material and methods 5.3.1 Feed Dewatering sludge liquor (centrate) from Lulu Island WWTP in Richmond, B.C., Canada was used for feeding the combined partial nitrification/Anammox process. The anaerobic digester at Lulu digests the combination of primary sludge and waste activated sludge at 38 \u00C2\u00B0C and operates at a retention time of approximately 32 days. Centrate contained ammonia ranged from 900~1,000 mg N/L, total organic carbon (TOC) of 150 mg/L and ortho-phosphate of 70 mg P/L. The alkalinity and pH of centrate were 2500 mg/L (as CaCO3) and 7.8, respectively. Alum was added to centrate for the purpose of sludge precipitation before it was feed to the Partial Nitrification reactor. The effluent from PN (SBR) was diluted and pumped to the Anammox reactors. 5.3.2 Experiment design Figure 30 shows the process schematic of the two stage partial nitrification-Anammox process. The partial nitrification (PN) reactor was composed of a 5-liters cylindrical (10 cm I.D. & 60 cm height) sequencing batch reactor (SBR) with the volumetric exchange ratio of 50 %. The Anammox reactor was made of 11-liter plastic cylinder (25 cm I.D. & 30 height) filled with 4 liters of plastic moving bed carriers (Kaldness K1). The centrate was first partially nitrified in the SBR, and the effluent was fed to the Anammox reactor. In the SBR, aeration was provided by a fine air diffuser, and mixing of the liquor was by an electrical/mechanical stirrer. A notebook computer loaded with LabView Signal Express software was used for monitoring temperature, pH and controlling dissolved oxygen (DO). LabView Signal Express software is commercially 62 available interactive software for acquiring, analysing and controlling the process signals. The SBR was operated at a cycle of 8 hr: 10 min of feeding, 7 hr and 10 min aeration, 30 min settling and 10 min decant. The dissolved oxygen (DO) and temperature were maintained at 2 mg/L and 20\u00C2\u00B12 \u00C2\u00B0C, respectively. The sludge retention time (SRT) was kept at 10 days to maintain mixed- liquor suspended solids (MLSS) at concentration of 1,650 mg/L. Sludge seed was obtained from the enhanced biological phosphorus removal (EBPR) pilot plant located at the University of British Columbia (UBC), BC, and Canada. Figure 30. Schematic of bench scale partial nitrification/Anammox process The Anammox reactor contained 1,300 mg/L solids, accounting for suspended solids in the liquid and also biomass on the biofilm. The hydraulic retention time (HRT) and temperature were maintained at 26 hr and 30\u00C2\u00B12 \u00C2\u00B0C, respectively. A settler removed the bio-solids from the effluent and returned all of them to the Anammox reactor. The sludge seed was originally obtained from the University of Winnipeg laboratory and enriched in the reactor for more than 6 months before the experiment. During 10 months operation, samples were taken twice a week from the reactors, in order to determine NH3/NH4+, NO2- and NO3- , TOC, TKN, MLVSS and alkalinity. 63 In the PN reactor, N2O emission base line was determined at initial pH=7.8, DO=1.5~2.5 mg/L and 20\u00C2\u00B0C; whereas in the Anammox reactor pH=7, and temperature of 30\u00C2\u00B12\u00C2\u00B0C was used to determine baseline emissions. For the Anammox reactor, due to the relatively small amount of N2O and NO emissions, the measurements were only applied to two operating conditions: with additional N2 as a stripping gas, and without additional N2 gas. Once the base line was determined, the impact of controlled operating parameters including DO (0.5, 1, 2, and 4 mg/L) and pH (6, 6.6, 7.2, and 7.8) on N2O and NO emissions from partial nitrification were investigated. Hydrochloric acid and Sodium hydroxide were used to control the pH at desired levels. To study the effect of feeding pattern on N2O and NO emissions from PN reactor, four experiments were conducted. The total feed volume in each cycle of partial nitrification reactor was 2.5 liters. In the first experiment 100 % of total feed volume (2.5 L) was pumped into the reactor in 10 min; whereas, in the second one 60% of total feed volume was pumped into the reactor in 6 minutes and the remaining 40% was pumped slowly in 40 minutes. Regarding to third experiment, 30% of the total feed volume was loaded at 3 minutes and the rest of the operating capacity introduced to the reactor in 70 minutes. In the last experiment, 100% of the feed was pumped to the partial nitrification reactor slowly and evenly at a rate of 25 ml/min within one hour. 5.3.3 Chemical analyses NH3/NH4+, NO2- and NO3- were determined by flow injection analysis of spectrophotometry (Quikchem 8000, Lachat). Total organic carbon (TOC) and total nitrogen (TN) were measured by a TOC/TN analyzer (IL TOC-TN, Lachat). Alkalinity, MLSS and TS were determined according to Standard Methods for Examination of Water and Wastewater (Clescerl et al., 2005, Section 2540). 64 5.3.3.1 N2O and NO analysis N2O off-gas from partial nitrification reactor was monitored by an infrared N2O Monitor (Bacharach, N2O monitor 3010). The off-gas was pumped at a flow rate of 100 mL/min by a rotary pump from the head space of the reactor to the monitoring system. In order to reduce the interference of moisture, off-gas was passed through an ice-chilled flask to condense moisture before entering the N2O analyzer (Lo., 2008). GC ECD was used for detecting N2O emission from the Anammox reactor. N2 gas was the stripping gas for the reactor; a100 \u00C2\u00B5L headspace sample was collected in a gas-tight syringe for GC ECD analysis. The operating conditions for the GC (HP-6890 GC ECD) were: column length of 0 .9144 m, 0.32 mm diameter with coating of 3 um of J&W carbonplate; carrier gas-He, 10psi, 40mL/min; oven temp: 100\u00C2\u00B0C. Nitric oxide was measured by a NO analyzer (NOA, Sievers 280i, GE), which applied the technology of ozone-chemiluminescence. Samples were taken by a plastic, gas-tight,syringe from the head space of reactors for detection. 5.4 Results and discussion 5.4.1 Performance of the partial nitrification/Anammox process The reactor successfully converted more than 50% of ammonia in the centrate to nitrite after partial nitrification (PN). The effluent of PN reactor contained 45.1\u00C2\u00B11.0 % ammonium, 45.1\u00C2\u00B11.0 % nitrite and 1.9\u00C2\u00B10.3% nitrate as initial nitrogen load. Subsequent Anammox treatment resulted in 35.4% additional ammonium removal, resulting in 84.9% total ammonia removal in the combined system. Total nitrogen removal in the combined partial nitrification/Anammox reached approximately 52.2%. The nitrogen mass balance showed that approximately 15.1% of ammonium, 9.4% of nitrite and 23.3% of nitrate, as total nitrogen load, were carried over to the final effluent. This result is comparable to the full scale partial nitrification/Anammox at Dokhaven-Sluisjesdijk Wastewater Treatment Plant in Netherlands (Kampschreur et al., 2008). 65 5.4.2 N2O and NO emissions 5.4.2.1 Partial nitrification under base line conditions Theoretically, the reaction of Anammox requires 1 mole of NH4+ and 1.32 mole of NO2- according to Equation 4. The goal of partial nitrification was to convert sufficient ammonium to nitrite to reach nitrite to ammonium ratio of 1.32, favourable for the Anammox reaction. However, a lack of alkalinity in the centrate prevented partial nitrification to reach this ideal point (Equation 4). Due to alkalinity limitation, ammonium oxidation rate (AOR) slowed down over the time and the system barely achieved the ideal point (Figure 31). Nevertheless, the partial nitrification process was operated without alkalinity adjustment in this study. Instead, pH was monitored in the process to determine such a point. In the PN reactor, nitrite to ammonia ratio equal to 1 was used a base point for comparing nitrogen conversion rates at various operation conditions. Under the base line condition, after approximately 300 min of aeration, ammonia to nitrite ratio reached 1. Figure 32 to 35 illustrate the typical time profile of nitrogen species, pH, N2O and NO emission under baseline conditions. Ammonia nitrogen in the centrate was mainly converted to nitrite, so that the effluent of PN reactor contained 47.3\u00C2\u00B10.9% nitrite and 1.4\u00C2\u00B10.2% nitrate. A nitrogen mass balance in the PN reactor revealed that only 1% of ammonium was converted to nitrogen gas, which might be due to denitrification and/or ammonia being stripped out from the reactor. The remaining nitrogen was emitted from the reactor as N2O (2.5\u00C2\u00B10.2% of nitrogen load) and NO (0.6\u00C2\u00B10.3% of nitrogen load). As it is shown by Figure 33 and 34, the concentration of N2O and NO in the reactor, off gas peaked at 180 ppm (as N2O) and 175 ppm (as NO) respectively. N2O concentration seems to have a correlation with the increasing nitrite concentration (Figure 34). Figure 32 indicates the pH profile during the PN reactor cycle. When the pH decreased to 5.8, the nitrite concentration levelled off and the ammonium to nitrite ratio reached 1. From this point forward, the N2O profile sharply dropped while NO concentration increased rapidly (Figure 34). The decrease in N2O might be due to inhibition of hydroxylamine oxidation under lower pH conditions leading to lower N2O production rate. In The same way, the increase in NO 66 production might be the result of low pH, which inhibited the activity of NO oxidation and caused the accumulation of NO. Figure 31. Nitrogen species in the partial nitrification reactor under base line conditions 67 Figure 32. pH measurement in the partial nitrification reactor 68 Figure 33.N2O emission from partial nitrification reactor under base line conditions 69 Figure 34.NO emission from partial nitrification reactor under base line conditions 5.4.2.2 Partial nitrification under dissolved oxygen- DO controlled condition The experiments were conducted at controlled dissolved oxygen between, 0.5 to 4 mg/L. Higher DO resulted in a higher average Ammonium Oxidation Rate (AOR). AOR was measured as 36.6 NH4+-N/hr/g biomass at DO of 4 mg/L, decreasing to AOR of 17.1 NH4+-N/hr/g biomass at DO of 0.5 mg/L. In contrast, higher DO caused lower N2O concentration in the PN reactor off-gas; whereas, NO was not affected by DO level. This suggests that the rate of N2O to NO oxidation is faster than hydroxylamine to N2O oxidation, at higher DO. On the other hand, lower DO reduced AOR and restrained N2O conversion to NO, which caused N2O accumulation in the reactor. The result of these experiments, under DO controlled conditions, suggests that higher DO not only has the potential of reducing N2O emission but also increases the ammonium oxidation rate and reduces the required cycle time of partial nitrification used for centrate treatment. 70 Although operating the PN reactor at higher dissolved oxygen may raise the concern of nitrate production by Nitrite Oxidizing Bacteria (NOB), decreasing the efficiency of subsequent Anammox treatment. Ammonium oxidizing bacteria (AOB) have been shown to have a higher affinity for oxygen than nitrite oxidation bacteria (NOB); therefore, high DO condition may promote the growth of both AOB and NOB (Schmidt and Bock, 1997; Jayamohan et al., 1988). It is generally accepted that, for low ammonia wastewaters, a relatively low DO (<1 mg/L) has to be maintained to attain successful partial nitrification (Zeng et al., 2003; Wyffels et al., 2004). However, for treatment of high ammonia wastewaters, such as centrate, the growth of Nitrite Oxidizing Bacteria (NOB) at high DO is not a concern. As an example, the full scale partial nitrification at Dokhaven-Sluisjesdijk WWTP was operated at a DO level of 3 mg/L and nitrite was hardly converted to nitrate in long term treatment (Kampschreur et al., 2008). Bernet\u00E2\u0080\u0099s et al. (2005) reported free ammonia as the main factor inhibiting the growth of NOB even at higher DO values. High concentration of nitrite (higher than 200 mg/L) has also been considered toxic to organisms, including NOB (Meinhold et al., 1999; Wyffels et al., 2004). 5.4.2.3 Partial nitrification under pH-controlled conditions Both N2O and NO emissions in the partial nitrification reactor were sensitive to pH. Specific Ammonium oxygen rate (AOR) decreasedfrom 26.4 NH4+-N/hr/g biomass at pH 7.8 to 10.1 NH4+-N/hr/g biomass, at pH 6. In this experiment, the system could not reach the base point of nitrite to ammonia ratio equal to 1 at low pH (pH=6.6 and 6.0). Alkalinity destruction due to acid addition for low level pH control experiments, led to limited nitrification. Under low pH conditions both, N2O and NO emissions increased. N2O emission increased from 1.4% as nitrogen load at pH 7.8 to more than 3.9% at pH less than 6.6. NO emission was 0.7% as nitrogen load at pH 7.8 and rose sharply to 3.9%, when the pH dropped to 6.0. The increased level of N2O emission at lower pH may be attributed to lower solubility of N2O in solution at lower pH; this resulted in N2O being stripped out of the liquid (Lo et al. 2008). 71 5.4.2.4 Partial nitrification under continuous feeding conditions Results from continuous feeding to the PN reactor illustrate that pumping feed slowly and evenly reduces NO emission. There is no evidence to show the impact of feeding rate on N2O emission (Table 1). During continuous a feeding at the rate of 25ml/min, NO off-gas reduced by 10% compared to NO emissions at feeding rate at 250 ml/min. When continuous slow feeding was applied to the PN reactor, the biomass was exposed to reduced ammonium concentration and alkalinity was provided more evenly for the reaction; whereas, pH levels were hardly changed during each cycle. As this condition resulted in lower NO emission, it can be implied that NO oxidation is relatively sensitive to the concentration of free ammonia, where higher free ammonia results in higher NO emission. Table 1. N2O and NO emissions from partial nitrification in different conditions Conditions Time to the point* (min) NO2/NH3 N2O(%) NO(%) MLSS(mg/L) DO (mg/L) 0.5 450 1.00 4.2 1.0 1740 1 300 1.00 1.9 1.0 1760 2 280 1.00 2.0 0.9 1800 4 210 1.00 1.4 1.0 1760 PH 7.8 300 1.00 1.4 0.7 1520 7.2 350 1.00 2.8 1.0 1620 6.6 420 0.41** 3.9 2.4 1200 6.0 420 0.35** 3.4 3.9 1200 Continuous feed (%) 100 240 1.00 2.2 0.1 1800 70 240 1.00 2.2 0.2 40 240 1.00 2.5 0.5 0 280 1.00 2.0 0.9 1800 Base line 297\u00C2\u00B112 1.00 2.5\u00C2\u00B10.2 0.6\u00C2\u00B10.3 1,650\u00C2\u00B1227 *: The elapsed time to reach NO2-/NH4+ = 1. **: The nitrification rates were relatively slow. After 7 hours (420 min) aeration, NO2-/NH4+ were still less than 1.0. 72 5.4.2.5 Anammox Relatively low N2O and NO emissions were detected from the Anammox reactor. N2O and NO emission were monitored under two conditions. In the first series of experiments, the stripped gas was N2 gas, produced by the Anammox reaction; this resulted in N2O emission of 0.15\u00C2\u00B10.02% as initial ammonia load in the centrate and no detectable amount of NO . This result agrees with the measurements at Dokhaven-Sluisjesdijk WWTP, where 0.21% N2O and 0.0001% NO were emitted from the Anammox reactor (Kampschreur et al., 2008). In the second series of the experiments, external N2 gas was introduced into Anammox reactor which increased N2O emission to 1.21\u00C2\u00B1.2 %. There is no research that reports N2O and NO produced from the Anammox metabolic pathway. The N2O emission might be due to dissolved N2O carryover from partial nitrification effluent to Anammox reactor, or produced by some denitrifiers growing in the Anammox reactor. In terms of reducing greenhouse gas, Anammox can be considered as a better process, compared to conventional nitrification denitrification processes. 73 6. Conclusions Nitrogen is a fundamental substances in the synthesis of protein (Metcalf & Eddy, 2003) and in the wastewater, ammonia(NH3), ammonium (NH4+), nitrogen gas, nitrite ion (NO2-) and nitrate ion (NO3-)are the most common and significant forms of nitrogen. Nitrogen compounds in wastewater play a crucial role in eutrophication and nitrite enrichment (Wuhrmann, K. 1964). As a result, more stringent regulations regarding nutrient compounds, are being applied for point source discharges; nitrogen exist in the wastewater in any form needs to be treated before to the water body. In effort to reduce water body impairment, this research studied the Partial Nitrification and Anammox process. Partial nitrification/ Anammox process has been considered as an option for nitrogen removal instead of conventional nitrification/denitrification (Zhang,Li et al., 2010; Fujii et al., 2002; Fux et al., 2002; Schmidt et al. 2003; van Dongen et al., 2001). The combination of partial nitrification and the Anammox process provides a promising method for nitrogen removal from wastewater with low carbon to nitrogen ratio, and a large quantity of ammonium (Loosdrecht et al., 1998). The application of the partial nitrification and Anammox in a continuous moving bed reactor followed by Anammox in a hybrid reactor was investigated in the first stage of the research. In this stage, analytical data was provided to understand what was necessary to have stable partial nitrification and Anammox reactions. The process was used to remove ammonia from centrate obtained from a full scale wastewater treatment plant. The partial nitrification system, which was carried out in a continuous, moving-bed, biofilm reactor, successfully converted approximately 31.7% of ammonia to nitrite. Lack of alkalinity in the centrate, low nitrifiers growth rate, and low sludge retention time were main reasons for the low conversion of ammonium to nitrite. The Anammox reactor that was set up after PN reactor resulted in 38.8% additional ammonium removal and nitrite removal of 83.1%. As a result, total ammonia removal in the combined system reached to 79.1% and total nitrogen removal was 56.8 %. The study illustrated alkalinity was found neither controlling nor limiting factor in Anammox reaction. 74 Furthermore, in the second stage of experiments, the performance of partial nitrification in a Sequencing Batch Reactor (SBR) was studied. The feasibility of operating the Anammox process in the up-flow fixed-bed reactor and hybrid Anammox reactor was also investigated in this stage. The results illustrate that the partial nitrification reactor successfully converted approximately 49.5\u00C2\u00B11.0% of ammonia to nitrite. Alkalinity was investigated as a limiting factor to convert more ammonia to nitrite in partial nitrification. The SBR was operated under controlled dissolved oxygen between 0.5 to 4 mg/L, to investigate the effect of DO concentration on Ammonium Oxidation Rate (AOR). Higher DO resulted in higher average Ammonium Oxidation Rate (AOR). AOR was measured as 36.6 NH4+-N/hr/g biomass at DO of 4 mg/L, decreasing to AOR of 17.1 NH4+-N/hr/g biomass at DO of 0.5 mg/L. Under low DO condition, after 450 min, the SBR reached an ideal base point of nitrite to ammonium ratio equal to 1. However, results showed that once SBR was operated under DO=3- 4 mg/L conditions, the base point were achieved at 160 min. As a result, under higher dissolved oxygen required cycle time for partial nitrification reaction reduces for centrate treatment. In fact, for the same volume shorter time was needed for partial nitrification process once the SBR was operated under higher dissolved oxygen. Ammonium oxidation rates in the SBR indicated sensitivity to the pH level. When SBR operated under controlled pH at 7.2 after approximately 200 min, the reaction reached base point of nitrite to ammonium equal to 1; whereas, neither in a pH controlled at 6.6 nor 6, was the base point achieved. The effect of feeding pattern on the SBR system was studied. When the centrate was pumped to the reactor evenly and slowly at the rate of 25 ml/min in 100 minutes, results indicated that the PN reactor reached the base point after approximately 240 minutes of aeration. On the other hand, once the PN was fed at the rate of 250 ml/min in 10 minutes, the nitrite to ammonium ratio in the reactor was equal to 1 after 350 minutes. As a result, ammonium oxidation rate increased when feed was pumped into the reactor slowly and evenly. When continuous slow feeding was applied to the PN reactor, the biomass was exposed to reduced ammonium concentration and 75 alkalinity was provided more evenly for the reaction; whereas, pH levels were hardly changed during each cycle. Distribution of alkalinity druing the experiment resulted in higher AOR, which is suggested by researchers as a practical operation strategy to reduce the partial nitrification cycle. Partially nitrified centrate was further treated in two Anammox reactors, where the mixture of ammonia and nitrite was converted mainly to nitrogen gas. Anammox treatment was carried out in two different Anammox reactors: a moving bed Hybrid reactor and Up-Flow Fixed-Bed biofilm reactor. The Hybrid Anammox reactor removed an average of 55.8% of NH4-N, versus 48.3% NH4-N removal in the Up Flow Fixed-Bed reactor. Nitrite removal in the Hybrid and Fixed-Bed Anammox reactors averaged 80.8% and 62.5%, respectively. The study illustrated that, in both Anammox reactors, the best Ammonia removal happens in Nitrite to Ammonium ratio between 1.35 and 1.45. As such, alkalinity was found to neither control nor limit the Anammox reaction. In third stage of the experiments, the amount of N2O and NO emissions from both partial nitrification and Anammox reactor under various operating conditions were measured. A practical operational strategy to reduce N2O and NO emission from partial nitrification and the Anammox process was discovered by researchers. The emissions from partial nitrification were 2.6\u00C2\u00B10.2% N2O and 0.6\u00C2\u00B10.3% NO as nitrogen load; Anammox, with 0.15% N2O and non detected amount of NO, showed relatively lower emissions compared to partial nitrification. In the partial nitrification reactor, higher dissolved oxygen (DO) decreased N2O emission by 67% without impacting NO emission. Under pH controlled conditions, lower pH dramatically affected N2O and NO emissions from the PN reactor, where N2O emission at pH=6.6 was 36% higher than pH=7.8. The Feeding regime into the PN reactor did not significantly affect N2O emission; however, it reduced NO emission by approximately 10%. N2O emission was affected by DO, pH and feeding pattern in the partial nitrification reactor. The results suggest strategies for N2O and NO emissions control as follow: \u00EF\u0082\u00B7 In the partial nitrification process, a higher DO in the solution results in a lower N2O emission. NO was not significantly affected by DO. 76 \u00EF\u0082\u00B7 A higher pH level in the partial nitrification reactor caused a lower N2O and NO emission. \u00EF\u0082\u00B7 Continuous slow feeding to the partial nitrification reactor did not affect N2O emission. However, NO emission decreased with a slower rate of feeding. Using conditions of a higher DO and higher pH are possible operating strategies, which could successfully reduce the emission of nitrous oxide and nitric oxide in a partial nitrification system. 6.1 Recommendation for the future research Anammox process is a relatively new technology in the wastewater treatment field especially in North America. Therefore, more research needs to be done to industrialize the process. Following are some of factors which need to be considered for future research: \u00EF\u0082\u00B7 Anammox bacteria are sensitive to temperature, considering the cold climate in Canada, temperature can be a cost effective obstacle in a way to have a full scale reactor. 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Journal of Bioscience and Bioengineering 111( 3), 306-311. 88 Date Comments on the process Flow(ml/min) pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 04-Dec-08 22.00 7.88 05-Dec-08 7+ 27 20.00 200.0 06-Dec-08 07-Dec-08 08-Dec-08 21.00 7.80 213.0 09-Dec-08 seeded with Sludge 10-Dec-08 11-Dec-08 21.00 7.90 272.0 12-Dec-08 13-Dec-08 14-Dec-08 air is 763 ml/min- n2 in the feed 15-Dec-08 feed orp after one day storage, n2 in feed 21.00 8.30 -243.00 266.0 16-Dec-08 17-Dec-08 21.00 8.00 -210.00 135.0 18-Dec-08 19-Dec-08 20-Dec-08 21-Dec-08 22-Dec-08 23-Dec-08 24-Dec-08 feed line to PN ractor 12ml/min, RC line 70 ml/min, 45 minute 25-Dec-08 26-Dec-08 27-Dec-08 28-Dec-08 29-Dec-08 12.00 7.90 -3.30 30-Dec-08 31-Dec-08 12.00 7.84 10.00 181.0 01-Jan-09 02-Jan-09 12.00 7.94 -120.00 173.0 03-Jan-09 04-Jan-09 05-Jan-09timer 1 one hour on (64ml/ min) timer 2 120 min on (108) ml/min 06-Jan-09 timer 1 3 hour on (64ml/ min) timer 2 120 min on (108) ml/min 07-Jan-09 08-Jan-09 timer 1- 20 minutes on (50ml/ min) timer 2 120 min on (108) 12.50 7.80 15.00 09-Jan-09 12.00 7.80 -60.00 178.0 10-Jan-09 12.00 7.90 -230.00 200.0 11-Jan-09 12.00 7.80 -201.00 228.0 12-Jan-09 RC changed from 8 to 24 12.00 7.80 -200.00 215.0 13-Jan-09 good Anammox activity suspcted because of gas production 12.00 7.56 213.0 14-Jan-09 15-Jan-09feed line to PN ractor 7.25 ml/min, RC 6.4 ml/min, 40 T-3.5 to PN 16-Jan-09 17-Jan-09 18-Jan-09 19-Jan-09 20-Jan-09 R1-I is recycle 7.00 7.90 -180.00 252.0 21-Jan-09 7.00 7.90 244.0 22-Jan-09 35 T-3.5 added to the PN 7.00 7.90 213.0 23-Jan-09 7.00 7.90 206.0 24-Jan-09 25-Jan-09 26-Jan-09 7.00 7.90 196.0 27-Jan-09 7.00 7.90 205.0 28-Jan-09 Rpm increased to 168 7.00 7.90 204.0 29-Jan-09 7.00 7.90 211.0 30-Jan-09 7.00 7.90 195.0 31-Jan-09 Centrate Characteristics Appendix 1. Raw data of the partial nitrification followed by Anammox in the continuous moving-bed biofilm reactors (MBBR) 89 Date Comments on the process Flow(ml/min) pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 01-Feb-09 7.00 7.90 193.0 02-Feb-09 7.00 7.90 189.00 760 03-Feb-09 8.00 194 780 04-Feb-09Influent increased feed 12 ml/min rc 11.5 ml/min, ammonia feed 300 05-Feb-09 206 780 06-Feb-09 204 800 07-Feb-09 08-Feb-09 DO = 10.5 % = 1.25 mg/L 09-Feb-09 12.00 297 1060 10-Feb-09 12.00 7.90 284 2220 11-Feb-09 330 1180 12-Feb-09 338 1200 13-Feb-09 Air flow increased 140 = 2170 ml/min 339 1220 14-Feb-09 15-Feb-09 16-Feb-09 367 1300 17-Feb-09 330 1400 18-Feb-09 8.10 330 1240 19-Feb-09 8.00 333 1270 20-Feb-09 7.85 330 1280 21-Feb-09 22-Feb-09 23-Feb-09 pH is R1 has decreased! DO set poit decrease 6.9%=0.5 mg/l 8.03 314 1220 24-Feb-09 pH is R2 has increased1DO set poit decrease 6.8% mg/l 8.02 334 1300 25-Feb-09 8.00 352 1340 26-Feb-09 27-Feb-09 28-Feb-09 01-Mar-09 02-Mar-09 Separated R1 fron R2, mixed Nano2 with centrate 337 1220 03-Mar-09 2.00 6.64 997 3640 04-Mar-09 feed flow increased to 6.5 ml/min 6.50 6.70 1000 3200 05-Mar-09 250 T-5 is added to R1 1080 06-Mar-09 Nitrite TOXICITY 07-Mar-09 Operated batch 08-Mar-09 Operated batch 09-Mar-09 Operated batch 10-Mar-09 Operated batch 11-Mar-09 Operated batch 12-Mar-09 300 T-5 is added to R2 5.50 5.90 200.00 13-Mar-09 18-Jul-00 14-Mar-09 15-Mar-09 16-Mar-09 288 3.46 0.8 2.65 17-Mar-09 217 1.33 0.3 0.993 18-Mar-09 900 19-Mar-09 20-Mar-09 DO = 30 % = 1.7 mg/L 217 1.56 0.2 1.32 21-Mar-09 (heater reactor 2 was broken) 290 1.63 0.2 1.41 860 22-Mar-09 305 3.57 1.4 2.22 23-Mar-09 24-Mar-09 267.5 8.84 1.8 7.04 800 25-Mar-09 26-Mar-09 270 2.41 1.4 1.33 2.8 740 27-Mar-09 28-Mar-09 29-Mar-09 30-Mar-09 360 8.57 0.6 8.09 8.7 900 31-Mar-09 249 7.12 0.5 6.77 7.2 880 Centrate Characteristics 90 Date Comments on the process Flow(ml/min) pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 01-Apr-09 02-Apr-09 239 6.3 0.8 5.7 6.5 03-Apr-09 273 1.01 0.4 0.708 1.1 940 04-Apr-09 05-Apr-09 the mixture of R2 wa broken 274 1.92 0.8 1.32 2.1 06-Apr-09 225 2.89 1.2 2.02 3.2 1060 07-Apr-09 08-Apr-09 09-Apr-09 217 1.71 0.2 1.53 800 10-Apr-09 215 1.72 0.5 1.26 11-Apr-09 pomp which transfers f2 to f1 was clogged and feeded mannually 199 1.47 0.4 1.09 12-Apr-09 13-Apr-09 14-Apr-09the pomp fixed and all tube and connectors have been changed 188 1.58 0.4 1.16 15-Apr-09 16-Apr-09 233 2.34 0.6 1.73 850 17-Apr-09 260 1.87 0.5 1.38 18-Apr-09 19-Apr-09 Do controller does not work properly 266 2.51 0.3 2.21 2.5 20-Apr-09 21-Apr-09 the flow rate from R2 to R1 has been incresed to 15ml/min 4.25 201 2.51 0.3 2.2 2.5 22-Apr-09 6126.55 179 2.1 0.7 1.4 2.1 720 23-Apr-09 24-Apr-09 25-Apr-09 26-Apr-09 27-Apr-09 182 5.78 2.3 3.55 5.8 28-Apr-09 364 2.45 1.3 1.12 2.5 1460 29-Apr-09Flow rate ,R2-R1 decreased to 8ml/min,300ml Anmmox sluge added to R1 389 2.44 1.3 1.14 2.5 30-Apr-09Flow rate ,R2-R1 increased t to 10ml/min(8ml H2SO4 added to ) 378 1.87 0.8 1.1 1.9 01-May-09 349 4.71 2.8 1.98 4.7 1320 02-May-09 03-May-09 337 2.53 1.0 1.5 2.5 04-May-09 341 1.29 0.2 1.1 1.3 1430 05-May-09 377 1.6 0.4 1.18 1.6 06-May-09 381 0.47 0.746 1340 07-May-09 08-May-09 378 3.31 0.6 2.68 3.3 1360 09-May-09 435 1.67 0.2 1.46 1.7 10-May-09Flow rate ,from Feed to R2 increased to 17 ml/minR2-R1 increased t to 16ml/min 373 2.78 0.9 1.89 2.8 11-May-09 368 1.05 0.1 0.923 1.1 12-May-09 426 1.32 0.3 1.05 1.3 1360 13-May-09 481 14-May-09 Dilution has changed to 500 mg/L Ammonia per liter 1700 15-May-09 329 16-May-09 17-May-09 18-May-09 19-May-09 357 2.21 0.3 1.89 20-May-09 375 1.62 0.1 1.54 1360 21-May-09 379 1.01 1.46 22-May-09 23-May-09 385 4.04 0.6 3.44 24-May-09 25-May-09 26-May-09 354 0.612 1.04 1240 27-May-09 28-May-09 29-May-09 3.22 0.1 3.14 30-May-09 31-May-09 Dilution has changed to 500 mg/L Ammonia per liter Centrate Characteristics 91 Date Comments on the process Flow(ml/min) pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 01-Jun-09 0.951 1.26 02-Jun-09 4.27 0.2 4.04 03-Jun-09 04-Jun-09 1.43 0.5 0.907 05-Jun-09 1.69 0.5 1.24 06-Jun-09 07-Jun-09 08-Jun-09 421 1.47 0.7 0.793 1480 09-Jun-09 10-Jun-09 447 1.75 0.4 1.38 2020 11-Jun-09 454 1.27 0.2 1.07 12-Jun-09 441 1.21 0.2 1.03 13-Jun-09 14-Jun-09 15-Jun-09 16-Jun-09 452 0.914 0.1 0.854 1600 17-Jun-09 18-Jun-09 2060 19-Jun-09 549 1.23 0.2 1.04 20-Jun-09 21-Jun-09 22-Jun-09 344 1.78 0.4 1.37 23-Jun-09 24-Jun-09 25-Jun-09 Air flow increased 5 535 1.63 0.2 1.48 1740 26-Jun-09 27-Jun-09 28-Jun-09 29-Jun-09 437 3.66 1.3 2.36 30-Jun-09 01-Jul-09 02-Jul-09 03-Jul-09 506 0.897 0.1 0.802 1680 04-Jul-09 05-Jul-09 06-Jul-09 07-Jul-09 623 2.98 1.0 1.96 2020 08-Jul-09 09-Jul-09 591 3.11 1.6 1.56 10-Jul-09 11-Jul-09 12-Jul-09 13-Jul-09 PH conroller diconent from R1 514 5.22 2.6 2.63 14-Jul-09 PH conroller applied to R1 15-Jul-09 566 1880 16-Jul-09 17-Jul-09 18-Jul-09 19-Jul-09 20-Jul-09 Flow from R2 to R1 has been stopped and PN-SBR applied to loop insead of R2.R2 flow rate has been change d to 2mL/min 21-Jul-09 First day of PN applied to system instead of R2 507 1 0.5 0.764 1950 22-Jul-09 23-Jul-09 533.55 2.535 1.2 1.305 24-Jul-09 25-Jul-09 26-Jul-09 27-Jul-09Set point for PH controller for Anammox reactor has been change to 7.7 601 1.95 3.11 2050 28-Jul-09 540 2.72 3.39 1790 29-Jul-09 Flow rate from feed to R2 and from R2 to R1 have been changed to 16 ml/min and 15m/min respectively. Centrate Characteristics 92 Date Comments on the process Flow(ml/min) pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 01-Aug-09 02-Aug-09 03-Aug-09 04-Aug-09 521 3.52 13.3 1800 05-Aug-09 06-Aug-09 PH Set point for PN change to 6.2 562 2.54 2.1 0.676 2.8 1960 07-Aug-09 08-Aug-09 503 09-Aug-09 10-Aug-09 Consider commend 484 1.26 1.4 0 1.4 1710 11-Aug-09 12-Aug-09 451 1.18 1.0 0.332 1.3 1570 13-Aug-09 14-Aug-09 Anammox pH controller is turned on again 476 0 0.24 2170 15-Aug-09 16-Aug-09 17-Aug-09Nitrite in nammox reactor was so high,R1I had been stopped for 1 hour.10 ml acid added to R1. 565 4.19 2.67 2100 18-Aug-09 19-Aug-09 20-Aug-09 461 1750 21-Aug-09 22-Aug-09 23-Aug-09 24-Aug-09 25-Aug-09 531 1990 26-Aug-09 27-Aug-09 28-Aug-09 1870 Centrate Characteristics 93 Date pH ORP temp Do % mixing RPM NH3-N NOX NO3-N NO2-N 04-Dec-08 05-Dec-08 27.1 27.7 28.0 296.0 9.7 3.1 6.6 06-Dec-08 07-Dec-08 08-Dec-08 7.6 10.0 30.5 19.4 192.0 45.6 1.7 43.9 09-Dec-08 10-Dec-08 11-Dec-08 7.8 15.0 28.6 18.8 40.0 234.0 35.0 1.4 33.6 12-Dec-08 13-Dec-08 14-Dec-08 15-Dec-08 9.8 43.0 234.0 23.5 0.3 23.2 16-Dec-08 17-Dec-08 7.5 67.0 31.7 18.0 106.0 45.7 2.9 42.8 18-Dec-08 19-Dec-08 20-Dec-08 21-Dec-08 22-Dec-08 23-Dec-08 24-Dec-08 25-Dec-08 26-Dec-08 27-Dec-08 28-Dec-08 29-Dec-08 7.2 96.8 32.5 8.9 160.0 30-Dec-08 31-Dec-08 6.7 91.0 32.5 28.0 160.0 86.6 107.0 5.0 102.0 01-Jan-09 02-Jan-09 6.9 76.8 33.7 21.0 160.0 64.0 97.0 7.0 90.0 03-Jan-09 04-Jan-09 05-Jan-09 06-Jan-09 07-Jan-09 08-Jan-09 7.2 85.0 32.8 15.0 162.0 09-Jan-09 7.1 110.0 34.0 13.4 162.0 10-Jan-09 6.7 144.0 34.0 14.1 162.0 86.6 9.2 0.5 8.7 11-Jan-09 7.1 99.3 36.0 14.5 162.0 102.0 8.1 0.6 7.5 12-Jan-09 7.0 111.3 34.7 14.1 162.0 109.0 9.3 0.5 8.8 13-Jan-09 7.2 90.7 36.0 14.4 162.0 141.0 6.7 1.1 5.6 14-Jan-09 15-Jan-09 16-Jan-09 17-Jan-09 18-Jan-09 19-Jan-09 20-Jan-09 6.4 110.0 33.4 15.0 114.0 134.0 110.0 2.0 21-Jan-09 6.6 73.4 33.6 14.5 114.0 140.0 107.0 2.0 22-Jan-09 6.8 63.9 35.0 14.6 114.0 101.0 1.4 99.6 23-Jan-09 6.7 64.0 33.6 14.3 114.0 102.0 2.0 100.0 24-Jan-09 25-Jan-09 26-Jan-09 6.7 32.0 14.0 114.0 104.0 5.9 98.1 27-Jan-09 7.1 32.6 14.0 114.0 91.2 5.0 86.2 28-Jan-09 6.9 32.0 14.0 168.0 95.3 5.0 90.3 29-Jan-09 6.5 127.1 30.7 14.0 168.0 30-Jan-09 6.7 64.0 32.9 14.0 168.0 97.9 8.2 89.7 31-Jan-09 Partial Nitrification Effluent Partial Nitrification Reactor 94 Date pH ORP temp Do % mixing RPM NH3-N NOX NO3-N NO2-N 02-Feb-09 6.4 119.0 32.0 14.0 168.0 105.0 19.3 85.7 03-Feb-09 6.4 112.6 30.3 103.0 43.4 59.6 04-Feb-09 05-Feb-09 7.6 45.2 31.9 43.6 42.0 1.7 06-Feb-09 61.4 12.8 48.6 07-Feb-09 08-Feb-09 09-Feb-09 6.8 102.5 33.9 132.0 57.2 74.8 10-Feb-09 6.5 105.0 33.9 147.0 68.8 78.2 11-Feb-09 7.0 55.5 33.8 136.0 61.9 74.1 12-Feb-09 7.4 47.3 32..6 112.0 47.6 64.4 13-Feb-09 7.2 80.2 32.3 11.0 120.0 51.4 68.6 14-Feb-09 15-Feb-09 16-Feb-09 7.0 88.7 31.6 11.6 149.0 73.2 75.8 17-Feb-09 7.5 44.4 32.6 11.0 127.0 53.5 73.5 18-Feb-09 6.2 161.0 31.1 12.2 159.0 77.2 81.8 19-Feb-09 6.9 24? 35.0 9.6 151.0 81.9 69.1 20-Feb-09 6.5 127.5 32.1 10.5 154.0 86.2 67.8 21-Feb-09 22-Feb-09 23-Feb-09 6.4 117.0 32.0 24-Feb-09 7.5 3.0 32.4 6.9 25-Feb-09 6.7 70.0 31.8 26-Feb-09 27-Feb-09 28-Feb-09 01-Mar-09 02-Mar-09 6.9 69.0 33.4 13%-16% 03-Mar-09 04-Mar-09 05-Mar-09 06-Mar-09 07-Mar-09 08-Mar-09 09-Mar-09 10-Mar-09 11-Mar-09 12-Mar-09 13-Mar-09 14-Mar-09 15-Mar-09 16-Mar-09 165.0 102.9 62.1 17-Mar-09 69.4 59.2 10.2 18-Mar-09 7.5 108.4 33.5 19-Mar-09 7.5 39.0 31.3 20-Mar-09 7.5 52.8 32.2 53.1 37.0 16.1 21-Mar-09 7.7 81.6 25? 63.2 57.2 6.0 22-Mar-09 7.5 95.3 23.4 31.2 136.0 96.1 39.9 23-Mar-09 7.7 82.0 24.3 24-Mar-09 7.4 91.0 31.6 41.6 117.0 31.9 85.1 25-Mar-09 26-Mar-09 6.4 133.7 30.7 49=.9mg/L 49.7 60.5 4.5 27-Mar-09 28-Mar-09 6.5 131.9 32.2 29-Mar-09 30-Mar-09 7.0 123.1 31.7 49.9=.3 94.2 8.0 88.2 31-Mar-09 6.2 167.9 32.8 74.4=.9 94.6 69.6 42.7 Partial Nitrification Reactor Partial Nitrification Effluent 95 Date pH ORP temp Do % mixing RPM NH3-N NOX NO3-N NO2-N 02-Apr-09 6.4 140.0 32.2 74.4=.6 106.0 29.2 84.2 03-Apr-09 6.3 138.8 32.2 79.2=.8 109.0 44.1 76.1 04-Apr-09 05-Apr-09 48.8 21.8 32.5 06-Apr-09 7.7 78.5 31.3 27.1 9.4 20.1 07-Apr-09 7.7 67.0 30.8 35.5=.8 08-Apr-09 09-Apr-09 7.3 114.0 33.3 78.0 12.4 65.6 10-Apr-09 6.5 131.5 36.6 0.8 113.0 22.4 90.6 11-Apr-09 6.7 153.2 30.3 0.8 112.0 20.2 91.8 12-Apr-09 13-Apr-09 14-Apr-09 118.0 31.7 86.3 15-Apr-09 16-Apr-09 7.1 111.3 29.5 0.8 102.0 33.0 69.0 17-Apr-09 7.3 109.7 40.1 0.8 101.0 20.9 80.1 18-Apr-09 19-Apr-09 7.1 124.2 32.1 0.4 108.0 13.1 95.0 20-Apr-09 21-Apr-09 6.6 146.4 37.7 0.9 103.0 39.0 64.4 22-Apr-09 7.4 81.6 33.5 0.5 51.9 28.6 23.6 23-Apr-09 24-Apr-09 25-Apr-09 6.6 90.2 32.2 1.1 26-Apr-09 27-Apr-09 84.9 83.5 2.3 28-Apr-09 7.8 52.1 34.1 1.3 104.0 75.9 28.9 29-Apr-09 7.8 43.0 30.7 121.0 60.7 60.9 30-Apr-09 7.6 52.0 31.7 0.8 143.0 46.0 97.5 01-May-09 7.4 17.7 32.3 1.8 137.0 37.5 99.9 02-May-09 03-May-09 7.5 29.4 30.4 1.8 125.0 22.2 103.0 04-May-09 7.3 28.0 29.4 1.5 147.0 23.2 124.0 05-May-09 7.5 44.4 37.0 0.8 132.0 21.2 111.0 06-May-09 7.3 66.9 34.7 0.5 150.0 27.4 123.0 07-May-09 7.5 95.0 31.4 08-May-09 7.0 102.4 35.2 1.4 156.0 3.0 153.0 09-May-09 7.5 40.1 31.5 1.6 150.0 2.0 148.0 10-May-09 7.5 45.9 34.3 0.3 139.0 1.0 138.0 11-May-09 6.9 101.8 33.3 0.6 158.0 2.0 156.0 12-May-09 7.3 21.5? 33.7 0.5 169.0 5.1 164.0 13-May-09 14-May-09 6.9 73.0 34.8 15-May-09 7.4 31.7 35.0 16-May-09 17-May-09 18-May-09 19-May-09 5.9 134.0 34.4 172.0 173.0 20-May-09 180.0 1.0 179.0 21-May-09 6.4 27.1 172.0 1.0 171.0 22-May-09 7.3 35.7 23-May-09 7.3 68.0 34.3 0.9 176.0 1.0 175.0 24-May-09 25-May-09 26-May-09 6.5 147.6 33.4 2.0 166.0 1.0 165.0 27-May-09 28-May-09 29-May-09 114.0 2.0 112.0 30-May-09 Partial Nitrification Reactor Partial Nitrification Effluent 96 Date pH ORP temp Do % mixing RPM NH3-N NOX NO3-N NO2-N 02-Jun-09 03-Jun-09 212.0 16.0 196.0 04-Jun-09 7.2 85.0 36.9 200.0 13.0 187.0 05-Jun-09 06-Jun-09 7.1 35.5 2.1 07-Jun-09 6.8 4.5 33.5 1.8 167.0 7.0 160.0 08-Jun-09 09-Jun-09 6.9 32.9 185.0 10.0 175.0 10-Jun-09 7.2 28.7 161.0 5.0 156.0 11-Jun-09 7.1 32.3 172.0 8.0 164.0 12-Jun-09 13-Jun-09 14-Jun-09 6.8 36.9 15-Jun-09 7.5 34.6 155.0 5.0 150.0 16-Jun-09 17-Jun-09 6.4 70.0 38.8 4.2 18-Jun-09 167.0 11.0 156.0 19-Jun-09 20-Jun-09 21-Jun-09 6.8 140.3 25.7 4.0 204.0 25.0 179.0 22-Jun-09 7.1 37.7 2.9 23-Jun-09 24-Jun-09 8.0 27.7 33.1 2.0 150.0 8.0 142.0 25-Jun-09 7.1 36.6 1.8 26-Jun-09 27-Jun-09 7.6 29.9 28-Jun-09 153.0 8.0 145.0 29-Jun-09 6.3 240.0 41.3 3.1 30-Jun-09 01-Jul-09 7.4 89.7 39.4 3.3 02-Jul-09 7.0 118.6 38.0 4.0 207.0 27.0 180.0 03-Jul-09 04-Jul-09 05-Jul-09 6.9 107.1 35.7 06-Jul-09 7.4 135.0 40.0 236.0 37.0 199.0 07-Jul-09 08-Jul-09 7.4 67.9 40.0 3.3 157.0 11.0 146.0 09-Jul-09 10-Jul-09 11-Jul-09 12-Jul-09 8.4 66.6 34.1 6.2 98.3 0.8 97.5 13-Jul-09 7.2 107.9 29.7 5.7 14-Jul-09 7.2 69.3 32.6 3.8 466.0 81.0 385.0 15-Jul-09 8.0 54.0 33.0 3.3 16-Jul-09 7.1 104.7 32.4 17-Jul-09 7.8 37.6 28.1 3.0 18-Jul-09 19-Jul-09 6.5 135.0 28.0 3.3 20-Jul-09 139.3 9.0 130.3 21-Jul-09 22-Jul-09 203.2 4.0 199.2 23-Jul-09 24-Jul-09 25-Jul-09 26-Jul-09 266.0 267.0 27-Jul-09 270.0 270.0 28-Jul-09 29-Jul-09 234.0 234.0 30-Jul-09 237.0 237.0 Partial Nitrification Reactor Partial Nitrification Effluent 97 Date pH ORP temp Do % mixing RPM NH3-N NOX NO3-N NO2-N 02-Aug-09 03-Aug-09 269.0 270.0 04-Aug-09 05-Aug-09 244.0 261.0 06-Aug-09 07-Aug-09 08-Aug-09 09-Aug-09 273.0 291.0 10-Aug-09 11-Aug-09 214.0 226.0 12-Aug-09 13-Aug-09 256.0 273.0 14-Aug-09 15-Aug-09 16-Aug-09 270.0 281.0 Partial Nitrification Reactor Partial Nitrification Effluent 98 Date pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 04-Dec-08 05-Dec-08 4.5 3.7 0.8 06-Dec-08 07-Dec-08 08-Dec-08 2.6 1.0 1.6 09-Dec-08 10-Dec-08 11-Dec-08 1.5 1.5 0.0 12-Dec-08 13-Dec-08 14-Dec-08 15-Dec-08 2.0 0.3 1.7 16-Dec-08 17-Dec-08 3.0 0.9 2.2 18-Dec-08 19-Dec-08 20-Dec-08 21-Dec-08 22-Dec-08 23-Dec-08 24-Dec-08 25-Dec-08 26-Dec-08 27-Dec-08 28-Dec-08 29-Dec-08 30-Dec-08 31-Dec-08 1.1 1.1 01-Jan-09 02-Jan-09 4.7 2.4 2.3 03-Jan-09 04-Jan-09 05-Jan-09 06-Jan-09 07-Jan-09 08-Jan-09 09-Jan-09 10-Jan-09 154.0 3.5 0.2 3.4 11-Jan-09 186.0 3.0 0.1 2.9 12-Jan-09 169.0 3.5 0.2 3.3 13-Jan-09 171.0 4.0 0.3 3.7 14-Jan-09 15-Jan-09 16-Jan-09 17-Jan-09 18-Jan-09 19-Jan-09 20-Jan-09 6.4 110.6 134.0 110.0 2.0 108.0 21-Jan-09 6.6 76.4 140.0 107.0 2.0 105.0 22-Jan-09 6.8 63.9 112.0 101.0 1.4 99.6 23-Jan-09 6.7 64.0 116.0 102.0 2.0 100.0 24-Jan-09 25-Jan-09 26-Jan-09 6.7 104.0 112.0 104.0 5.9 98.1 27-Jan-09 7.1 77.0 117.0 91.2 5.0 86.2 28-Jan-09 6.9 64.0 122.0 95.3 5.0 90.3 29-Jan-09 6.5 127.0 113.0 60.0 30-Jan-09 6.7 62.0 101.0 97.9 8.2 89.7 120.0 31-Jan-09 Anammox Reactor influent 99 Date pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 02-Feb-09 7.0 52.0 103.0 87.7 10.2 77.5 03-Feb-09 6.5 119.0 97.8 105.0 19.3 85.7 60.0 04-Feb-09 6.5 110.8 99.4 103.0 43.4 59.6 70.0 05-Feb-09 06-Feb-09 148.0 43.6 42.0 1.7 380.0 07-Feb-09 135.0 61.4 12.8 48.6 340.0 08-Feb-09 09-Feb-09 10-Feb-09 154.0 132.0 57.2 74.8 210.0 11-Feb-09 6.5 105.0 152.0 147.0 68.8 78.2 110.0 12-Feb-09 176.0 136.0 61.9 74.1 60.0 13-Feb-09 193.0 112.0 47.6 64.4 400.0 14-Feb-09 197.0 120.0 51.4 68.6 280.0 15-Feb-09 16-Feb-09 17-Feb-09 206.0 149.0 73.2 75.8 180.0 18-Feb-09 189.0 127.0 53.5 73.5 380.0 19-Feb-09 152.0 159.0 77.2 81.8 80.0 20-Feb-09 178.0 151.0 81.9 69.1 110.0 21-Feb-09 162.0 154.0 86.2 67.8 90.0 22-Feb-09 23-Feb-09 24-Feb-09 191.0 70.0 25-Feb-09 229.0 600.0 26-Feb-09 182.0 120.0 27-Feb-09 28-Feb-09 01-Mar-09 02-Mar-09 03-Mar-09 187.0 270.0 04-Mar-09 05-Mar-09 06-Mar-09 07-Mar-09 08-Mar-09 09-Mar-09 10-Mar-09 11-Mar-09 12-Mar-09 13-Mar-09 14-Mar-09 15-Mar-09 16-Mar-09 17-Mar-09 163.0 165.0 102.9 62.1 18-Mar-09 69.4 59.2 10.2 19-Mar-09 154.0 322.0 20-Mar-09 21-Mar-09 190.0 53.1 37.0 16.1 22-Mar-09 190.3 63.2 57.2 6.0 560.0 23-Mar-09 200.8 136.0 96.1 39.9 24-Mar-09 25-Mar-09 180.3 117.0 31.9 85.1 380.0 26-Mar-09 27-Mar-09 145.5 49.7 60.5 4.5 65.1 100.0 28-Mar-09 29-Mar-09 30-Mar-09 31-Mar-09 214.0 94.2 8.0 88.2 96.2 300.0 Anammox Reactor influent 100 Date pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 02-Apr-09 126.0 94.6 69.6 42.7 112.3 50.0 03-Apr-09 04-Apr-09 120.0 106.0 29.2 84.2 113.4 05-Apr-09 123.0 109.0 44.1 76.1 120.2 70.0 06-Apr-09 07-Apr-09 207.0 48.8 21.8 32.5 54.3 08-Apr-09 212.0 27.1 9.4 20.1 560.0 09-Apr-09 10-Apr-09 11-Apr-09 123.0 78.0 12.4 65.6 290.0 12-Apr-09 115.0 113.0 22.4 90.6 13-Apr-09 107.0 112.0 20.2 91.8 14-Apr-09 15-Apr-09 16-Apr-09 99.5 118.0 31.7 86.3 17-Apr-09 18-Apr-09 133.0 102.0 33.0 69.0 215.0 19-Apr-09 153.0 101.0 20.9 80.1 20-Apr-09 21-Apr-09 136.0 108.0 13.1 95.0 108.1 22-Apr-09 23-Apr-09 90.2 103.0 39.0 64.4 103.4 24-Apr-09 121.0 51.9 28.6 23.6 52.2 320.0 25-Apr-09 26-Apr-09 27-Apr-09 28-Apr-09 29-Apr-09 97.6 84.9 83.5 2.3 85.7 30-Apr-09 238.0 104.0 75.9 28.9 104.8 640.0 01-May-09 254.0 121.0 60.7 60.9 121.6 02-May-09 233.0 143.0 46.0 97.5 143.5 03-May-09 197.0 137.0 37.5 99.9 137.4 300.0 04-May-09 05-May-09 223.0 125.0 22.2 103.0 125.2 06-May-09 127.0 147.0 23.2 124.0 147.2 310.0 07-May-09 243.0 132.0 21.2 111.0 132.2 08-May-09 226.0 150.0 27.4 123.0 150.4 300.0 09-May-09 10-May-09 205.0 156.0 3.0 153.0 156.0 230.0 11-May-09 258.0 150.0 2.0 148.0 150.0 12-May-09 257.0 139.0 1.0 138.0 139.0 13-May-09 211.0 158.0 2.0 156.0 158.0 142.0 14-May-09 257.0 169.0 5.1 164.0 169.1 15-May-09 286.0 16-May-09 400.0 17-May-09 221.0 18-May-09 19-May-09 20-May-09 21-May-09 180.0 172.0 173.0 22-May-09 156.0 180.0 1.0 179.0 60.0 23-May-09 178.0 172.0 1.0 171.0 24-May-09 25-May-09 211.0 176.0 1.0 175.0 26-May-09 27-May-09 28-May-09 176.0 166.0 1.0 165.0 80.0 29-May-09 30-May-09 Anammox Reactor influent 101 Date pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 02-Jun-09 03-Jun-09 04-Jun-09 168.0 7.0 161.0 05-Jun-09 35.6 27.1 8.5 06-Jun-09 07-Jun-09 212.0 16.0 196.0 08-Jun-09 200.0 13.0 187.0 09-Jun-09 10-Jun-09 11-Jun-09 232.0 167.0 7.0 160.0 180.0 12-Jun-09 13-Jun-09 241.0 185.0 10.0 175.0 180.0 14-Jun-09 288.0 161.0 5.0 156.0 15-Jun-09 279.0 172.0 8.0 164.0 16-Jun-09 17-Jun-09 18-Jun-09 19-Jun-09 287.0 155.0 5.0 150.0 440.0 20-Jun-09 21-Jun-09 720.0 22-Jun-09 413.0 167.0 11.0 156.0 23-Jun-09 24-Jun-09 25-Jun-09 255.0 204.0 25.0 179.0 26-Jun-09 27-Jun-09 28-Jun-09 337.0 150.0 8.0 142.0 700.0 29-Jun-09 30-Jun-09 01-Jul-09 02-Jul-09 337.0 153.0 8.0 145.0 03-Jul-09 04-Jul-09 05-Jul-09 06-Jul-09 259.0 207.0 27.0 180.0 170.0 07-Jul-09 08-Jul-09 09-Jul-09 10-Jul-09 336.0 236.0 37.0 199.0 370.0 11-Jul-09 12-Jul-09 383.0 157.0 11.0 146.0 13-Jul-09 14-Jul-09 15-Jul-09 16-Jul-09 386.0 98.3 0.8 97.5 17-Jul-09 18-Jul-09 317.0 466.0 81.0 385.0 450.0 19-Jul-09 20-Jul-09 21-Jul-09 22-Jul-09 23-Jul-09 24-Jul-09 136.7 139.3 9.0 130.3 130.0 25-Jul-09 26-Jul-09 220.2 203.2 4.0 199.2 27-Jul-09 28-Jul-09 29-Jul-09 30-Jul-09 284.0 266.0 267.0 200.0 Anammox Reactor influent 102 Date pH ORP NH3-N Nox-N NO3-N NO2-N Corrected Nox Alk, (mg/L)CaCO3 02-Aug-09 273.0 234.0 234.0 220.0 03-Aug-09 284.0 237.0 237.0 04-Aug-09 05-Aug-09 06-Aug-09 07-Aug-09 277.0 269.0 270.0 490.0 08-Aug-09 09-Aug-09 274.0 244.0 261.0 180.0 10-Aug-09 11-Aug-09 12-Aug-09 13-Aug-09 255.0 273.0 291.0 14-Aug-09 15-Aug-09 251.0 214.0 226.0 120.0 16-Aug-09 17-Aug-09 261.0 256.0 273.0 130.0 18-Aug-09 19-Aug-09 20-Aug-09 276.0 270.0 281.0 120.0 21-Aug-09 281.0 22-Aug-09 23-Aug-09 254.0 120.0 24-Aug-09 25-Aug-09 26-Aug-09 27-Aug-09 28-Aug-09 215.0 120.0 29-Aug-09 30-Aug-09 31-Aug-09 134.0 Anammox Reactor influent 103 Date NH3-N N0x NO3-N NO2-N Corrected NOx PO4-P BOD COD Alk, (mg/L)CaCO3 04-Dec-08 05-Dec-08 267.0 10.4 6.6 3.8 06-Dec-08 07-Dec-08 08-Dec-08 200.0 35.6 0.1 35.5 09-Dec-08 10-Dec-08 11-Dec-08 244.0 24.3 1.3 23.0 12-Dec-08 13-Dec-08 14-Dec-08 15-Dec-08 246.0 22.6 1.4 21.2 16-Dec-08 17-Dec-08 110.0 35.0 3.0 32.0 18-Dec-08 19-Dec-08 20-Dec-08 21-Dec-08 22-Dec-08 23-Dec-08 24-Dec-08 25-Dec-08 26-Dec-08 27-Dec-08 28-Dec-08 29-Dec-08 64.9 43.2 5.5 37.7 30-Dec-08 31-Dec-08 01-Jan-09 02-Jan-09 94.2 41.0 5.6 35.4 03-Jan-09 04-Jan-09 05-Jan-09 06-Jan-09 07-Jan-09 08-Jan-09 09-Jan-09 10-Jan-09 134.0 3.1 0.2 2.9 11-Jan-09 155.0 2.7 0.2 2.5 12-Jan-09 162.0 3.0 0.2 2.8 13-Jan-09 167.0 3.7 0.3 3.4 14-Jan-09 15-Jan-09 16-Jan-09 17-Jan-09 18-Jan-09 19-Jan-09 20-Jan-09 91.0 38.3 4.7 33.6 21-Jan-09 85.4 40.5 6.1 34.4 22-Jan-09 69.9 23-Jan-09 54.6 24-Jan-09 25-Jan-09 26-Jan-09 54.6 25.2 11.1 14.1 27-Jan-09 49.4 11.8 8.8 3.0 28-Jan-09 50.5 12.3 9.0 3.3 29-Jan-09 50.6 180.0 30-Jan-09 38.3 14.5 12.7 1.8 140.0 31-Jan-09 Anammox Recator Effluent 104 Date NH3-N N0x NO3-N NO2-N Corrected NOx PO4-P BOD COD Alk, (mg/L)CaCO3 02-Feb-09 46.0 14.2 12.8 1.4 03-Feb-09 37.4 18.5 17.1 1.4 80.0 04-Feb-09 40.9 31.0 29.4 1.6 130.0 05-Feb-09 06-Feb-09 95.4 48.8 31.9 16.9 280.0 07-Feb-09 107.0 26.5 22.1 4.4 340.0 08-Feb-09 09-Feb-09 10-Feb-09 80.8 55.9 23.9 32.0 180.0 11-Feb-09 72.5 53.0 31.4 21.6 115.0 12-Feb-09 96.7 70.9 33.2 37.7 160.0 13-Feb-09 112.0 51.7 36.1 15.6 280.0 14-Feb-09 155.0 38.2 33.0 5.2 460.0 15-Feb-09 16-Feb-09 17-Feb-09 141.0 66.2 46.3 19.9 240.0 18-Feb-09 122.0 53.5 32.3 21.2 280.0 19-Feb-09 94.6 45.4 28.3 17.1 220.0 20-Feb-09 92.0 66.4 63.0 3.4 240.0 21-Feb-09 102.0 67.8 65.4 2.4 170.0 22-Feb-09 23-Feb-09 24-Feb-09 153.0 120.0 25-Feb-09 154.0 330.0 26-Feb-09 131.0 240.0 27-Feb-09 28-Feb-09 01-Mar-09 02-Mar-09 03-Mar-09 115.0 220.0 04-Mar-09 123.0 05-Mar-09 297.0 2200.0 06-Mar-09 70.9 07-Mar-09 837.0 08-Mar-09 09-Mar-09 10-Mar-09 11-Mar-09 12-Mar-09 13-Mar-09 14-Mar-09 15-Mar-09 16-Mar-09 17-Mar-09 152.0 142.0 129.6 12.4 36.8 18-Mar-09 153.3 69.0 64.4 4.6 29.4 19-Mar-09 402.0 20-Mar-09 21-Mar-09 170.5 28.4 26.7 1.7 29.6 22-Mar-09 181.8 36.0 33.8 2.2 27.0 460.0 23-Mar-09 177.5 47.9 42.9 5.0 32.1 24-Mar-09 25-Mar-09 176.0 32.1 21.5 10.6 34.1 500.0 26-Mar-09 27-Mar-09 107.0 23.8 30.1 1.4 31.4 24.5 160.0 28-Mar-09 29-Mar-09 30-Mar-09 31-Mar-09 125.5 29.0 18.5 15.2 33.7 26.0 270.0 Anammox Recator Effluent 105 Date NH3-N N0x NO3-N NO2-N Corrected NOx PO4-P BOD COD Alk, (mg/L)CaCO3 02-Apr-09 65.3 33.8 30.8 10.8 41.6 29.2 120.0 03-Apr-09 04-Apr-09 65.4 43.5 44.4 10.4 54.8 29.2 05-Apr-09 69.1 44.5 48.9 8.0 56.9 28.8 100.0 06-Apr-09 07-Apr-09 221.0 18.5 19.4 4.1 23.4 24.8 08-Apr-09 213.0 9.3 8.2 3.2 11.4 29.0 690.0 09-Apr-09 10-Apr-09 11-Apr-09 123.0 18.6 7.5 11.1 24.9 420.0 12-Apr-09 54.4 23.7 16.3 7.4 24.9 13-Apr-09 51.5 30.3 18.9 11.4 25.5 14-Apr-09 15-Apr-09 16-Apr-09 26.8 8.0 4.6 3.4 24.1 17-Apr-09 18-Apr-09 51.4 29.0 22.8 6.2 23.1 350.0 19-Apr-09 74.6 20.9 17.8 3.1 23.9 20-Apr-09 21-Apr-09 75.7 24.8 20.0 5.0 25.0 27.0 22-Apr-09 23-Apr-09 51.8 38.9 33.7 5.5 39.2 21.2 24-Apr-09 71.4 34.3 30.6 4.0 34.6 19.6 190.0 25-Apr-09 26-Apr-09 27-Apr-09 28-Apr-09 29-Apr-09 88.7 80.8 79.8 1.8 81.6 30-Apr-09 185.0 77.5 75.1 3.2 78.3 01-May-09 204.0 87.6 69.2 19.1 88.3 500.0 02-May-09 178.0 56.4 51.3 5.6 56.9 03-May-09 152.0 52.3 45.9 6.9 52.8 430.0 04-May-09 05-May-09 131.0 47.6 40.6 7.4 48.0 06-May-09 127.0 49.0 35.2 14.2 49.4 240.0 07-May-09 128.0 39.6 32.4 7.6 39.9 08-May-09 105.0 54.6 47.7 7.3 55.1 140.0 09-May-09 114.0 10-May-09 135.0 46.7 30.2 16.9 47.1 180.0 11-May-09 153.0 30.1 21.7 8.6 30.4 12-May-09 108.0 26.8 20.0 7.1 27.1 13-May-09 87.0 32.2 24.3 8.2 32.5 160.0 14-May-09 177.0 43.0 35.0 8.5 43.5 15-May-09 16-May-09 500.0 17-May-09 103.0 18-May-09 19-May-09 20-May-09 21-May-09 27.4 17.5 10.0 27.4 22-May-09 86.6 35.2 24.7 10.5 35.2 90.0 23-May-09 63.9 32.0 23.8 8.3 32.0 24-May-09 25-May-09 98.3 40.5 22.8 17.7 40.5 26-May-09 27-May-09 28-May-09 69.0 28.7 22.6 6.1 28.7 120.0 29-May-09 30-May-09 Anammox Recator Effluent 106 Date NH3-N N0x NO3-N NO2-N Corrected NOx PO4-P BOD COD Alk, (mg/L)CaCO3 02-Jun-09 03-Jun-09 04-Jun-09 25.6 20.3 5.3 25.6 05-Jun-09 35.6 27.1 8.5 06-Jun-09 07-Jun-09 47.8 32.9 14.9 08-Jun-09 48.3 33.4 14.9 48.3 09-Jun-09 10-Jun-09 11-Jun-09 64.9 1.5 0.7 0.8 1.5 100.0 12-Jun-09 13-Jun-09 85.3 43.8 31.7 12.1 43.8 120.0 14-Jun-09 115.0 41.1 28.0 13.1 41.1 15-Jun-09 129.0 41.7 23.5 18.2 41.7 16-Jun-09 17-Jun-09 18-Jun-09 19-Jun-09 107.0 27.0 19.9 7.1 27.0 220.0 20-Jun-09 21-Jun-09 920.0 22-Jun-09 209.0 28.9 16.7 12.2 28.9 23-Jun-09 24-Jun-09 25-Jun-09 159.0 33.5 20.5 13.0 33.5 26-Jun-09 27-Jun-09 28-Jun-09 216.0 35.5 22.6 12.9 35.5 570.0 29-Jun-09 30-Jun-09 01-Jul-09 02-Jul-09 195.0 37.7 28.7 9.0 37.7 03-Jul-09 04-Jul-09 05-Jul-09 210.0 06-Jul-09 96.5 28.8 25.2 3.6 28.8 07-Jul-09 08-Jul-09 09-Jul-09 10-Jul-09 136.0 54.4 39.9 14.5 54.4 220.0 11-Jul-09 12-Jul-09 178.0 30.5 24.0 6.5 30.5 13-Jul-09 14-Jul-09 15-Jul-09 16-Jul-09 299.0 32.6 12.3 20.3 32.6 17-Jul-09 18-Jul-09 173.0 40.8 30.5 10.3 40.8 310.0 19-Jul-09 20-Jul-09 21-Jul-09 22-Jul-09 23-Jul-09 24-Jul-09 64.6 17.8 13.7 4.1 17.8 100.0 25-Jul-09 26-Jul-09 27-Jul-09 67.8 40.2 27.6 12.6 40.2 28-Jul-09 29-Jul-09 30-Jul-09 94.7 39.3 33.4 10.5 43.9 200.0 Anammox Recator Effluent 107 Date NH3-N N0x NO3-N NO2-N Corrected NOx PO4-P BOD COD Alk, (mg/L)CaCO3 02-Aug-09 98.2 28.7 24.6 7.5 32.1 03-Aug-09 04-Aug-09 05-Aug-09 06-Aug-09 91.6 31.4 26.6 8.5 35.1 180.0 07-Aug-09 08-Aug-09 101.0 34.0 36.2 2.3 38.5 120.0 09-Aug-09 10-Aug-09 11-Aug-09 12-Aug-09 84.4 38.3 36.9 6.0 42.9 13-Aug-09 14-Aug-09 84.8 41.5 38.5 7.8 46.3 130.0 15-Aug-09 16-Aug-09 72.0 22.0 20.7 3.9 24.6 110.0 17-Aug-09 18-Aug-09 19-Aug-09 93.3 23.2 22.2 3.8 26.0 170.0 20-Aug-09 92.8 21-Aug-09 22-Aug-09 86.8 110.0 23-Aug-09 24-Aug-09 25-Aug-09 26-Aug-09 27-Aug-09 79.1 120.0 28-Aug-09 29-Aug-09 30-Aug-09 100.0 Anammox Recator Effluent 108 Appendix 2.Raw data of partial nitrification in the sequencing batch reactor Partial Nitrification in the Sequencing Batch Reactor Result DO = 0.5 -1.5 mg/L Aeration rate = 3 LPM Time sample# min NH4+ NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 6 1100.00 1100.00 5.81 3.26 2.60 0.00 1106 7.90 9:30 7 0 481.00 481.00 537.00 495.00 42.86 1.03 1019 5.70 9:40 8 10 832.00 832.00 229.00 220.00 9.18 0.26 1061 7.60 10:15 9 45 755.00 755.00 262.00 249.00 13.27 0.33 1017 7.90 11:00 10 90 759.00 759.00 351.00 329.00 22.45 0.43 1110 7.80 11:45 11 135 603.00 603.00 417.00 387.00 30.61 0.64 1021 7.70 12:30 12 180 536.00 556.00 440.00 407.00 33.67 0.73 997 7.40 1:05 13 205 457.00 520.00 482.00 442.00 40.82 0.85 1003 6.90 1:40 14 250 506.00 506.00 509.00 465.00 44.90 0.92 1016 6.30 2:15 15 285 385.00 485.00 521.00 467.00 55.10 0.96 1007 5.90 2:50 16 320 433.00 456.00 510.00 460.00 51.02 1.01 967 5.70 3:15 17 345 456.00 445.00 513.00 466.00 47.96 1.05 959 5.70 4:00 18 390 399.00 435.00 514.00 467.00 47.96 1.07 950 5.70 4:50 5.70 effluent 19.00 463.00 463.00 546.00 496.00 51.02 1.07 1010 5.70 109 DO = 1.5 -2.5 mg/L Aeration rate = 2.5 LPM Time sample# min NH4+ NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 1 979 979 7.50 2.50 5.10 0.00 987 7.80 9:30 2 0 480 480 529.00 507.00 22.45 1.06 1009 5.90 9:40 3 10 751 751 238.00 217.00 21.43 0.29 989 7.50 10:15 4 45 758 758 256.00 235.00 21.43 0.31 1014 7.90 11:00 5 90 660 660 302.00 279.00 23.47 0.42 962 7.80 11:45 6 135 593 593 349.00 328.00 21.43 0.55 942 7.60 12:30 7 180 527 527 417.00 395.00 22.45 0.75 944 7.40 1:05 8 205 497 497 454.00 434.00 20.41 0.87 951 7.10 1:40 9 250 442 442 509.00 487.00 22.45 1.10 951 6.60 2:15 10 285 437 437 506.00 490.00 16.33 1.12 943 5.90 2:50 11 320 450 463 491.00 471.00 20.41 1.05 941 5.70 3:15 12 345 455 484 493.00 474.00 19.39 1.04 948 5.60 4:00 13 390 435 435 497.00 477.00 20.41 1.10 932 5.60 4:50 440 5.60 effluent 13 435 435 0.00 0.00 435 5.60 110 DO = 0.3 - 0.7 mg/L Aeration rate = 2.5 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 1 995 7.67 7.07 0.60 0.01 1003 8.10 9:30 2 0 469 542 540 2 1.15 1011 7.40 9:40 3 10 705 252 244 8 0.35 957 7.70 10:15 4 45 681 242 232 10 0.34 923 7.70 11:00 5 90 642 280 274 6 0.43 922 7.80 11:45 6 135 613 309 304 5 0.50 922 7.70 12:30 7 180 597 340 330 10 0.55 937 7.70 1:15 8 225 568 368 365 3 0.64 936 7.50 2:00 9 270 518 410 388 22 0.75 928 7.40 2:45 10 315 495 417 397 20 0.80 912 7.20 3:30 11 360 486 420 417 3 0.86 906 7.00 4:15 12 405 477 442 432 10 0.91 919 6.80 5:00 13 450 445 470 448 22 1.01 915 6.50 5:30 14 480 440 471 451 20 1.03 911 6.20 5:45 15 495 432 468 455 13 1.05 900 6.00 6:20 16 530 428 481 465 16 1.09 909 5.70 6:50 17 560 431 485 468 17 1.09 916 5.60 effluent 17 431 485 472 13 1.10 916 5.60 111 DO = 3.5 - 4.5 mg/L Aeration rate = 3 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 1 1020 8.74 8.08 0.66 0.01 1029 8.10 10:00 2 0 505 516.00 516.00 0.00 1.02 1021 5.70 10:10 3 10 766 237.00 226.00 11.00 0.30 1003 7.80 10:45 4 45 731 281.00 273.00 8.00 0.37 1012 8.10 11:30 5 90 648 360.00 351.00 9.00 0.54 1008 7.80 12:00 6 120 538 408.00 408.00 0.00 0.76 946 7.70 12:30 7 150 485 460.00 460.00 0.00 0.95 945 7.10 1:00 8 180 450 510.00 510.00 0.00 1.13 960 6.40 1:20 9 200 445 515.00 515.00 0.00 1.16 960 6.00 1:40 10 220 430 522.00 522.00 0.00 1.21 952 5.80 2:00 11 240 425 526.00 520.00 6.00 1.22 951 5.70 2:20 12 260 410 532.00 530.00 2.00 1.29 942 5.60 effluent 410 532.00 530.00 2.00 1.29 942 5.60 112 pH=7.8 DO = 1.5 - 2.5 mg/L Aeration rate = 2 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 1 1090 15 0 14.60 0.00 1105 8.10 9:30 2 0 475 440 426 14.00 0.90 915 5.70 9:40 3 10 689 214 210 4.00 0.30 903 7.80 10:15 4 45 667 230 218 12.00 0.33 897 7.80 11:00 5 90 637 256 238 18.00 0.37 893 7.80 11:45 6 135 604 292 284 8.00 0.47 896 7.80 12:30 7 180 559 342 324 18.00 0.58 901 7.80 1:00 8 210 536 374 356 18.00 0.66 910 7.80 1:30 9 240 497 408 390 18.00 0.78 905 7.80 2:00 10 270 467 446 420 26.00 0.90 913 7.80 2:30 11 300 436 482 440 42.00 1.01 918 7.80 3:00 12 330 391 512 464 48.00 1.19 903 7.80 3:30 13 360 368 556 504 52.00 1.37 924 7.80 4:15 14 405 315 594 534 60.00 1.70 909 7.80 4:45 15 435 272 652 564 88.00 2.07 924 7.80 effluent 15.00 272 652 564 88.00 2.07 924 7.80 113 pH=7.2 DO = 1.5 - 2.5 mg/L Aeration rate = 2.5 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 16 904 6 6 0.80 0.01 910 7.90 9:30 17 0 405 489 486 3.00 1.20 894 5.70 9:40 18 10 621 262 250 12.00 0.40 883 7.20 10:15 19 45 574 270 266 4.00 0.46 844 7.20 11:00 20 90 527 296 292 4.00 0.55 823 7.20 11:45 21 135 495 338 334 4.00 0.67 833 7.20 12:30 22 180 463 389 385 4.00 0.83 852 7.20 1:00 23 210 432 436 428 8.00 0.99 868 7.20 1:30 24 240 415 440 435 5.00 1.05 855 7.20 2:00 25 270 397 454 448 6.00 1.13 851 7.20 2:30 26 300 378 467 460 7.00 1.22 845 7.20 3:00 27 330 364 500 492 8.00 1.35 864 7.20 3:45 28 375 351 530 510 20.00 1.45 881 7.20 4:30 29 420 331 558 539 19.00 1.63 889 7.20 effluent 29.00 331 558 539 19.00 1.63 889 7.20 114 pH=6.6 DO = 1.5 - 2.5 mg/L Aeration rate = 2 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 16 970 8.00 12.00 -4.00 0.01 978 7.80 9:30 17 0 514 454 422 32 0.82 968 5.70 9:40 18 10 741 232 216 16 0.29 973 6.60 10:15 19 45 738 230 214 16 0.29 968 6.60 11:00 20 90 740 226 210 16 0.28 966 6.60 11:45 21 135 724 246 229 17 0.32 970 6.60 12:30 22 180 726 248 231 17 0.32 974 6.60 1:00 23 210 714 248 231 17 0.32 962 6.60 1:30 24 240 704 262 244 18 0.35 966 6.60 2:00 25 270 700 272 253 19 0.36 972 6.60 2:30 26 300 692 276 257 19 0.37 968 6.60 3:00 27 330 680 290 270 20 0.40 970 6.60 3:45 28 375 678 294 273 21 0.40 972 6.60 4:30 29 420 671 298 277 21 0.41 969 6.60 effluent 29.00 672 298 277 21 0.41 970 6.60 115 pH=6 DO = 1.5 - 2.5 mg/L Aeration rate = 0.25 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 16 987 3.00 2.78 0.22 0.00 990 8.00 11:00 17 0 534 457 408 49 0.76 991 5.70 11:10 18 10 742 248 214 34 0.29 990 6.00 12:00 19 60 765 223 204 19 0.27 988 6.00 12:45 20 105 754 232 211 21 0.28 986 6.00 1:30 21 150 738 248 226 22 0.31 986 6.00 2:15 22 195 735 250 230 20 0.31 985 6.00 3:00 23 240 732 253 231 22 0.32 985 6.00 3:45 24 285 729 257 236 21 0.32 986 6.00 4:30 25 330 720 268 243 25 0.34 988 6.00 5:15 26 375 718 267 244 23 0.34 985 6.00 6:00 27 420 715 272 250 22 0.35 987 6.00 effluent 29.00 715 272 250 22 0.35 987 6.00 116 pH=6 DO = 1.5 - 2.5 mg/L Aeration rate = 0.25 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 16 987 3.00 2.78 0.22 0.00 990 8.00 11:00 17 0 534 457 408 49 0.76 991 5.70 11:10 18 10 742 248 214 34 0.29 990 6.00 12:00 19 60 765 223 204 19 0.27 988 6.00 12:45 20 105 754 232 211 21 0.28 986 6.00 1:30 21 150 738 248 226 22 0.31 986 6.00 2:15 22 195 735 250 230 20 0.31 985 6.00 3:00 23 240 732 253 231 22 0.32 985 6.00 3:45 24 285 729 257 236 21 0.32 986 6.00 4:30 25 330 720 268 243 25 0.34 988 6.00 5:15 26 375 718 267 244 23 0.34 985 6.00 6:00 27 420 715 272 250 22 0.35 987 6.00 effluent 29.00 715 272 250 22 0.35 987 6.00 117 Continuous feeding (100 % of total feed volume (2.5 L) was pumped into the reactor in 10 min) DO = 1.5 - 2.5 mg/L Aeration rate = 1.5 LPM before 10:30; after 10:30 = 2.5 LPM Feeding rate was =250ml/min Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 1 1040 4.57 5.06 -0.49 0.00 1045 7.80 10:30 2 0 463 526.00 539.00 -13.00 1.16 989 6.20 10:40 3 10 555 405.00 403.00 2.00 0.73 960 7.15 11:15 4 35 644 382.00 369.00 13.00 0.57 1026 7.60 11:45 5 65 559 374.00 366.00 8.00 0.65 933 7.76 12:15 6 95 559 401.00 391.00 10.00 0.86 960 7.65 12:45 7 125 455 483.00 395.00 88.00 0.84 938 7.65 13:15 8 155 471 463.00 457.00 6.00 0.96 934 7.40 13:45 9 185 475 460.00 448.00 12.00 1.00 935 7.20 14:15 10 215 448 497.00 506.00 -9.00 1.12 945 6.92 14:45 11 245 450 481.00 485.00 -4.00 1.01 931 6.52 15:15 12 275 480 486.00 479.00 7.00 1.02 966 6.13 15:45 13 305 470 501.00 495.00 6.00 1.12 971 5.84 16:15 14 335 442 506.00 503.00 3.00 1.05 948 5.73 16:45 15 365 478 532.00 466.00 66.00 1.12 1010 17:15 16 395 417 483.00 473.00 10.00 1.13 900 effluent 16 30 417 483.00 473.00 10.00 1.13 900 5.60 118 Continuous feeding (100 % of total feed volume (2.5 L) was pumped into the reactor in 2 hour) DO = 1.5 - 2.5 mg/L Aeration rate = 1.5 LPM before 10:30; after 10:30 = 2.5 LPM Feeding stopped at 12:00; feeding rate was 25ml/min of the feeding pump controller Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 995 8.60 8.00 0.60 0.01 1004 7.80 9:30 1 0 508 489.00 447.00 42.00 0.88 997 5.70 9:45 2 5 497 490.00 445.00 45.00 0.90 987 6.30 10:00 3 30 513 477.00 435.00 42.00 0.85 990 6.70 10:30 4 60 550 440.00 423.00 17.00 0.77 990 7.30 11:00 5 90 558 432.00 414.00 18.00 0.74 990 7.40 11:30 6 120 571 418.00 397.00 21.00 0.70 989 7.60 12:00 7 150 591 395.00 378.00 17.00 0.64 986 7.60 12:30 8 180 567 419.00 403.00 16.00 0.71 986 7.60 1:00 9 210 524 457.00 440.00 17.00 0.84 981 7.40 1:30 10 240 492 497.00 491.00 6.00 1.00 989 7.20 2:00 11 270 455 540.00 518.00 22.00 1.14 995 7.00 2:30 12 300 405 574.00 559.00 15.00 1.38 979 6.70 3:00 13 330 381 604.00 584.00 20.00 1.53 985 6.30 3:30 14 360 365 621.00 600.00 21.00 1.64 986 5.90 4:00 15.00 5.80 effluent 14.00 463 590.00 536.00 54.00 1.16 1053 5.60 119 Continuous feeding (60% of total feed volume was pumped into the reactor in 6 minutes and the remaining 40% was pumped slowly in 40 minutes) DO = 1.5 - 2.5 mg/L Aeration rate = 2.5 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 931 3.03 3.20 -0.17 0.00 934 7.80 10:30 1 0 587 385.00 386.00 -1.00 0.66 972 10:40 2 10 647 257.00 250.00 7.00 0.39 904 7.64 11:15 3 30 623 296.00 292.00 4.00 0.47 919 8.07 11:45 4 90 704 312.00 307.00 5.00 0.44 1016 7.90 12:15 5 120 637 345.00 342.00 3.00 0.54 982 7.67 12:45 6 150 576 379.00 376.00 3.00 0.65 955 7.52 13:15 7 180 565 417.00 410.00 7.00 0.73 982 7.36 13:45 8 210 478 449.00 447.00 2.00 0.94 927 7.18 14:15 9 240 504 479.00 469.00 10.00 0.93 983 6.86 14:45 10 270 507 495.00 489.00 6.00 0.96 1002 6.65 15:15 11 300 497 489.00 473.00 16.00 0.95 986 6.22 15:45 12 330 473 529.00 515.00 14.00 1.09 1002 6.05 16:15 13 360 489 514.00 502.00 12.00 1.03 1003 5.92 16:45 14 390 478 531.00 511.00 20.00 1.07 1009 5.80 17:15 15 420 515 538.00 514.00 24.00 1.00 1053 5.79 effluent 15.00 515 538.00 514.00 24.00 1.00 1053 5.79 120 Continuous feeding (30% of total feed volume was pumped into the reactor in 3 minutes and the remaining 70% was pumped slowly in 70 minutes) DO = 1.5 - 2.5 mg/L Aeration rate = 2.5 LPM Time sample# min NH4+ NOX NO2 NO3 NO2/NH4+ NH4+N02+NO3 PH influent 1 916 1.33 4.75 -4.75 0.01 916 7.80 9:30 2 0 498 471 373.00 -371.67 0.75 499 5.70 9:33 3 3 596 338.00 302.00 36.00 0.51 934 7.00 10:00 4 30 629 392.00 342.00 50.00 0.54 1021 7.50 10:30 5 60 638 427.00 359.00 68.00 0.56 1065 7.50 11:00 6 90 621 360.00 300.00 60.00 0.48 981 7.52 11:30 7 120 663 375.00 345.00 30.00 0.52 1038 7.55 12:00 8 150 606 357.00 343.00 14.00 0.57 963 7.53 12:30 9 180 552 397.00 385.00 12.00 0.70 949 7.40 1:00 10 210 563 416.00 397.00 19.00 0.71 979 7.20 1:30 11 240 508 452.00 439.00 13.00 0.86 960 6.88 2:00 12 270 489 483.00 448.00 35.00 0.92 972 6.46 2:30 13 300 471 487.00 440.00 47.00 0.93 958 6.10 3:00 14 330 488 469.00 483.00 -14.00 0.99 957 5.90 3:30 15 360 462 477.00 492.00 -15.00 1.06 939 5.73 4:00 16.00 390 457 449 383.00 66.00 0.84 906 5.62 effluent 29.00 457 449 383.00 66.00 0.84 906 5.62 121 Sample Number TOC(mg/L) SOC(mg/L) NH3-N Nox-N NO3-N NO2-N Corrected Nox NO2-N/NH4-N Alak(mg/L CaCO3) 1 60.9 42.3 8.7 33.6 42.31 0.55 2 41.7 35.5 11.1 24.7 35.78 0.59 3 35.1 65 48.1 8.4 39.7 48.10 0.61 100 4 50.2 38.6 7.3 31.5 38.78 0.63 5 17 14 80.3 63.3 13.0 50.8 63.77 0.63 6 18 16 77.3 67.3 15.8 52.1 67.87 0.67 7 55.5 53 12.8 40.2 53.01 0.72 8 46.9 44.4 9.6 35 44.64 0.75 9 44.6 42.9 9.4 33.7 43.14 0.76 10 50 48.4 9.7 38.7 48.41 0.77 11 46.6 44.6 8.1 36.5 44.61 0.78 12 44.8 50.5 51.8 11.4 40.4 51.81 0.80 13 37.7 37.1 6.4 30.7 37.11 0.81 14 22.9 49.7 46 10.3 40.6 50.90 0.82 15 43.4 51 15.5 35.7 51.17 0.82 16 30.8 50.3 49.4 7.0 42.4 49.40 0.84 17 43.7 54 16.2 38 54.18 0.87 18 32.6 50.8 51 6.2 44.8 51.00 0.88 19 35.6 32.6 1.2 31.4 32.60 0.88 20 42.4 53 15.1 38.1 53.17 0.90 21 42.9 54.8 16.2 38.8 54.98 0.90 22 41.8 52 14.3 37.9 52.16 0.91 23 43.4 53.1 19.2 39.5 58.74 0.91 24 25.7 48 49.1 5.0 44.1 49.10 0.92 25 38.5 53.6 17.9 35.7 53.60 0.93 26 36.9 52.7 18.4 34.3 52.70 0.93 27 18 14 54 64.1 13.4 50.7 64.10 0.94 28 43.1 56.5 16.2 40.5 56.68 0.94 29 46.6 52.1 8.4 43.8 52.19 0.94 30 37.7 56.4 20.9 35.5 56.40 0.94 31 14 12 43.8 55.2 14.1 41.3 55.35 0.94 32 43 54.8 14.1 40.9 54.95 0.95 33 45.3 50.1 6.9 43.3 50.18 0.96 34 45.7 53.6 9.9 43.8 53.71 0.96 35 38.5 52.2 15.3 37.1 52.37 0.96 36 43.1 54.7 13.2 41.6 54.85 0.97 37 35.1 42.9 9.1 34 43.13 0.97 38 44.6 51.4 8.0 43.5 51.49 0.98 39 14 16 48.8 58.4 11.1 47.7 58.80 0.98 40 45.4 56.5 11.9 44.7 56.63 0.98 41 16 14 50.7 60.5 10.7 50.2 60.88 0.99 42 44.7 51 6.7 44.4 51.07 0.99 43 24.1 51.4 58.5 7.4 51.1 58.50 0.99 44 34.4 43.9 9.8 34.2 44.01 0.99 45 39.7 51.7 16.8 39.8 56.63 1.00 46 47.8 62 13.8 48.2 62.00 1.01 47 14 12 41.3 55.2 13.7 41.7 55.35 1.01 48 23.5 50.9 61.6 9.8 51.8 61.60 1.02 49 12 34 43.8 9.2 34.7 43.90 1.02 50 33 39.7 47 6.3 40.7 47.00 1.03 Influent Characteristics Appendix 3. Data of the hybrid and the up-flow fixed-bed Anammox reactors 122 Sample Number TOC(mg/L) SOC(mg/L) NH3-N Nox-N NO3-N NO2-N Corrected Nox NO2-N/NH4-N Alaklinity(mg CaCO3) 51 25 15 53.8 68.1 12.8 55.3 68.10 1.03 52 46.5 62 13.9 48.1 62.00 1.03 53 33 43.8 9.7 34.2 43.91 1.04 54 44.7 63.2 15.1 48.1 63.20 1.08 55 11 32.7 44.5 9.4 35.2 44.60 1.08 56 13 11 41.7 56.3 11.3 45.1 56.42 1.08 57 42.5 58.3 12.0 46.4 58.43 1.09 58 44.1 51 2.6 48.4 51.00 1.10 59 40.9 58.5 12.3 46.2 58.51 1.13 60 19 12 48.5 59.2 4.5 54.8 59.31 1.13 61 41.2 59 12.2 46.8 59.01 1.14 62 32.6 52.2 15.3 37.1 52.37 1.14 63 25 19 58.4 70 3.1 66.9 70.03 1.15 64 41.1 64 16.2 48.3 64.52 1.18 65 42.9 64.8 14.0 51.2 65.25 1.19 66 14 13 46.9 58.4 2.5 56 58.46 1.19 67 40.1 60.3 11.7 48.6 60.31 1.21 68 34.4 59.1 17.2 41.9 59.12 1.22 69 36.9 62.4 19.6 45.2 64.83 1.22 70 36.9 62.4 19.6 45.2 64.83 1.22 71 23.3 15 38.3 62.9 17.5 47.2 64.70 1.23 72 48.1 79.5 22.5 59.8 82.29 1.24 73 37.6 57.2 14.3 47.1 61.39 1.25 74 38.6 60.4 11.8 48.6 60.41 1.26 75 47.5 72 13.3 60.1 73.37 1.27 76 36.6 57.8 16.1 46.4 62.52 1.27 77 17.1 11 31.1 54.2 13.9 40.3 54.20 1.30 78 14 48.7 65.4 2.3 63.2 65.46 1.30 79 36.6 65.2 20.2 47.5 67.71 1.30 80 36.6 65.2 20.2 47.5 67.71 1.30 81 36.5 57.1 13.7 47.4 61.12 1.30 44 82 13 47.2 64.5 3.3 61.3 64.59 1.30 83 16.1 11.8 31.6 51.1 9.9 41.2 51.10 1.30 40 84 38.3 64 14.2 50.1 64.28 1.31 85 25 19 51.2 69.3 2.3 67 69.33 1.31 86 36 59.3 11.6 47.7 59.31 1.33 87 40.9 64.2 10.3 54.2 64.53 1.33 88 42.7 63.9 7.4 56.7 64.14 1.33 175 89 35.4 64.5 19.6 47.3 66.93 1.34 90 35.4 64.5 19.6 47.3 66.93 1.34 91 43.5 75.1 18.6 58.2 76.77 1.34 92 33.9 58.5 15.0 45.4 60.35 1.34 93 45.6 73.5 13.7 61.2 74.91 1.34 94 25.4 38.3 67.5 16.1 51.7 67.82 1.35 95 15.3 12.3 32.6 54.9 10.8 44.1 54.90 1.35 40 96 12.3 34.3 61.5 16.8 46.4 63.23 1.35 97 15.4 12.2 36.7 67.3 17.6 49.7 67.30 1.35 98 15.3 47.1 73.5 10.8 63.8 74.61 1.35 99 39.2 67.3 14.2 53.1 67.31 1.35 100 12.7 34.5 62.4 17.4 46.8 64.19 1.36 Influent Characteristics 123 Sample Number TOC(mg/L) SOC(mg/L) NH3-N Nox-N NO3-N NO2-N Corrected Nox NO2-N/NH4-N Alaklinity(mg CaCO3) 101 20.1 12.6 36.7 67.2 17.4 49.8 67.20 1.36 102 39.8 69.9 15.6 54.3 69.90 1.36 103 40.3 64.4 9.6 55.1 64.71 1.37 104 38.2 66.6 13.9 52.7 66.61 1.38 105 17.6 17.6 48.4 74.6 8.5 67 75.47 1.38 106 24 17 48.1 70.1 3.5 66.6 70.14 1.38 107 44.3 73.4 12.7 62 74.71 1.40 108 18.8 12.4 35.8 67.6 17.2 50.4 67.60 1.41 109 26.3 52.2 15.3 37.1 52.37 1.41 110 38.3 69.2 15.0 54.2 69.20 1.42 111 34.2 55 6.5 48.5 55.00 1.42 112 19 13 41.4 62.5 3.3 59.2 62.54 1.43 113 23 15.00 42.2 61.45 1.1 60.35 61.48 1.43 114 36.1 71.5 19.5 52 71.50 1.44 115 40 60.8 2.9 58 60.89 1.45 116 34.5 66.4 18.6 50.1 68.71 1.45 117 16 12 38.8 59 2.7 56.4 59.07 1.45 118 36 66.6 14.2 52.4 66.61 1.46 119 15.2 44.5 75.2 11.0 65.3 76.34 1.47 120 12.7 29.9 56.1 12.2 43.9 56.10 1.47 40 121 14 12 38.3 59 2.7 56.4 59.07 1.47 122 ? 41.4 63.1 2.0 61.1 63.12 1.48 123 33.3 64.4 17.4 49.2 66.55 1.48 124 24 17 45.1 70.1 3.3 66.8 70.14 1.48 125 39.2 64.6 6.5 58.3 64.81 1.49 126 25.1 37.1 64.1 9.1 55.2 64.28 1.49 127 16.1 11.3 29.2 55.9 12.2 43.7 55.90 1.50 128 30.4 60.2 16.8 45.5 62.28 1.50 129 39.2 64.2 5.5 58.9 64.38 1.50 130 18 15 40 61.6 1.0 60.6 61.61 1.52 131 18.4 14.4 31.5 56.1 8.3 47.8 56.10 1.52 132 37.2 66.4 9.8 56.8 66.60 1.53 133 18.2 10.8 30.4 56.1 9.6 46.5 56.10 1.53 134 15.3 32 56.4 7.3 49.1 56.40 1.53 40 135 14.6 10.5 29.7 56.3 10.6 45.7 56.30 1.54 136 25.1 17.6 34.2 59 6.1 52.9 59.00 1.55 137 35.7 65.5 10.2 55.6 65.83 1.56 138 18.4 14.6 31.1 47.7 48.5 47.70 1.56 139 29.3 60.4 16.4 46 62.44 1.57 140 17.7 14.6 28 56.2 11.4 44.8 56.20 1.60 48 141 18.2 12.2 28.9 49 2.7 46.3 49.00 1.60 142 32.7 71.5 19.1 52.4 71.50 1.60 143 28.6 60.9 16.9 46.1 62.99 1.61 144 35.6 59.7 1.8 57.9 59.70 1.63 145 31.1 60 9.1 50.9 60.00 1.64 146 14.5 10.8 27.3 57.1 12.1 45 57.10 1.65 71.5 147 35.2 67.4 9.5 58.1 67.59 1.65 148 17.5 10.8 28.2 56.2 9.5 46.7 56.20 1.66 71.5 149 17.5 10.6 28.1 56.3 9.6 46.7 56.30 1.66 71.5 150 31.1 59.6 7.8 51.8 59.60 1.67 Influent Characteristics 124 Sample Number TOC(mg/L) SOC(mg/L) NH3-N Nox-N NO3-N NO2-N Corrected Nox NO2-N/NH4-N Alaklinity(mg CaCO3) 151 33.6 59.3 3.2 56.1 59.30 1.67 152 25.1 14.4 30 47.2 50.7 47.20 1.69 153 30 59 8.3 50.7 59.00 1.69 154 36.5 67.2 5.6 61.7 67.31 1.69 155 36.6 67.5 5.4 62.2 67.61 1.70 156 28.5 48 48.5 48.00 1.70 157 29.3 60.4 10.1 50.3 60.40 1.72 158 17.7 10.8 27.2 50.7 4.0 46.7 50.70 1.72 159 27.5 57.2 9.8 47.4 57.20 1.72 160 14 12 36.1 66.6 4.3 62.4 66.72 1.73 161 33.9 59 0.4 58.6 59.00 1.73 162 30.4 70.7 17.8 52.9 70.70 1.74 163 29.9 70.4 17.9 52.5 70.40 1.76 164 29.1 48.3 51.2 48.30 1.76 165 28.4 65.1 13.1 52 65.10 1.83 166 34.7 68.4 4.2 64.3 68.48 1.85 167 29.9 124 66.9 57.1 124.00 1.91 168 27.8 70.7 17.6 53.1 70.70 1.91 169 29.4 109 51.9 57.1 109.00 1.94 170 17.6 15.2 29.3 59.3 1.6 57.7 59.30 1.97 171 27.5 70.2 15.5 54.7 70.20 1.99 172 28.6 100 42.7 57.3 100.00 2.00 Influent Characteristics 125 Sample Number Flow Rate(ml/min) HRT (hr) pH ORP Temp 1 9.00 2 8.00 22.9 7.13 -86.1 30.1 3 12.00 15.3 4 7.00 7.15 -83.0 30.8 5 14.90 12.3 6 14.90 12.3 7.03 -126.2 30.5 7 9.00 20.4 6.73 -86.4 30.1 8 7.00 7.02 -82.0 31.4 9 7.00 26.2 6.76 -80.0 30 10 9.00 20.4 6.88 -96.0 28.1 11 9.00 20.4 6.58 -123.8 28.2 12 10.50 17.5 6.78 -116.5 28.9 13 9.00 7.01 -108.0 28.8 14 10.50 15 6.00 30.6 6.93 -148 32.2 16 10.50 17.5 17 6.00 30.6 6.91 -152.2 33.5 18 10.50 17.5 7.07 -102.8 29.7 19 9.00 6.83 -92.1 28.6 20 6.00 30.6 6.93 -148 32.2 21 6.00 30.6 6.91 -152.2 33.5 22 6.00 30.6 6.91 -152.2 33.5 23 6.50 28.2 6.97 -146.7 32.4 24 12.50 14.7 6.95 -122.4 29.8 25 6.50 28.2 6.86 -147.1 31.4 26 6.50 28.2 27 14.90 12.3 28 6.00 30.6 6.81 -147.3 32.6 29 6.00 30.6 30 6.50 28.2 31 6.00 30.6 6.87 -146.1 31 32 6.00 30.6 6.87 -146.1 31 33 6.00 30.6 6.96 -145.2 31.1 34 6.00 30.6 35 6.00 30.6 6.82 -154.8 31.3 36 6.00 30.6 6.87 -146.1 31 37 7.00 26.2 6.75 -82.7 28.3 38 6.00 30.6 39 14.90 12.3 7.06 -125.6 31.1 40 6.00 30.6 6.81 -147.3 32.6 41 14.90 12.3 6.75 -127.1 29.7 42 6.00 30.6 6.96 -145.2 31.1 43 14.50 12.6 7.7 -62.8 26.9 44 6.00 30.6 7.02 -158.7 30.4 45 6.50 28.2 46 7.00 26.2 7.13 -141.9 28 47 6.00 30.6 6.87 -146.1 31 48 14.50 12.6 7.85 -99.7 49 6.00 30.6 7.02 -158.7 30.4 50 14.90 12.3 Anammox Hybrid Reactor 126 Sample Number Flow Rate(ml/min) HRT (hr) pH ORP Temp 51 14.90 12.3 52 7.00 26.2 7.13 -141.9 28 53 6.00 30.6 7.02 -158.7 30.4 54 7.00 26.2 7.13 -141.9 28 55 6.00 30.6 7.02 -158.7 30.4 56 6.00 30.6 6.81 -147.3 32.6 57 6.00 30.6 6.81 -147.3 32.6 58 12.50 59 6.50 28.2 60 19.50 9.4 61 6.50 28.2 62 6.00 30.6 6.82 -154.8 31.3 63 6.00 30.6 7.29 -135.1 30.9 64 6.00 30.6 7.01 -133.3 32.3 65 6.00 30.6 66 19.50 9.4 67 6.50 28.2 6.9 -173.4 32.8 68 6.50 28.2 69 7.00 26.2 7.18 -155.1 30 70 7.00 26.2 7.52 -126.6 29 71 6.50 28.2 72 7.00 26.2 73 6.50 28.2 74 6.50 28.2 75 6.50 28.2 76 6.50 28.2 77 7.00 26.2 78 10.00 18.3 6.74 -158.5 29.5 79 7.00 26.2 7.18 -155.1 30 80 7.00 26.2 7.52 -126.6 29 81 6.50 28.2 6.84 -147.3 32.6 82 10.00 18.3 6.74 -158.5 29.5 83 7.00 26.2 7.14 -146.2 29.8 84 6.50 28.2 85 6.00 30.6 7.29 -135.1 30.9 86 6.50 28.2 87 6.00 30.6 88 6.00 30.6 7.04 -138.8 32.1 89 7.00 26.2 7.18 -155.1 30 90 7.00 26.2 7.52 -126.6 29 91 7.00 26.2 92 7.00 26.2 7.39 -140.5 30 93 6.50 28.2 94 6.50 28.2 6.9 -138.7 31.5 95 7.00 26.2 7.14 -146.2 29.8 96 6.50 28.2 7.05 -149.9 31 97 7.00 26.2 6.88 -145.1 29.9 98 6.50 28.2 99 6.50 28.2 100 6.50 28.2 Anammox Hybrid Reactor 127 Sample Number Flow Rate(ml/min) HRT (hr) pH ORP Temp 101 7.00 26.2 6.88 -145.1 29.9 102 6.00 30.6 103 6.00 30.6 104 6.50 28.2 105 6.50 28.2 106 6.00 30.6 107 6.50 28.2 108 7.00 26.2 6.88 -145.1 29.9 109 6.00 30.6 6.82 -154.8 31.3 110 6.00 30.6 6.9 31.5 -138.7 111 6.50 28.2 112 6.00 30.6 7.33 -104 31.8 113 6.00 30.6 7.17 -126.1 31 114 6.00 30.6 115 6.00 30.6 116 7.00 26.2 7.39 -140.5 30 117 19.50 9.4 118 6.50 28.2 7.4 -141.6 29.1 119 6.50 28.2 120 7.00 26.2 7.14 -146.2 29.8 121 19.50 9.4 7.08 -129 31.2 122 6.00 30.6 7.33 -104 31.8 123 7.00 26.2 7.39 -140.5 30 124 6.00 30.6 125 6.00 30.6 126 6.50 28.2 7.16 -129.9 29.4 127 7.00 26.2 128 7.00 26.2 7.32 -142 28 129 6.00 30.6 130 6.00 30.6 7.32 -132.4 30.9 131 6.50 28.2 132 6.50 28.2 133 7.00 26.2 134 6.50 28.2 6.98 -149.6 29.2 135 7.00 26.2 136 6.50 28.2 137 6.00 30.6 138 6.50 28.2 139 7.00 26.2 7.32 -142 28 140 7.00 26.2 7.17 30.2 141 6.50 28.2 142 6.00 30.6 6.98 -132.6 31.6 143 7.00 26.2 7.32 -142 28 144 6.50 28.2 145 7.00 26.2 7.43 -130.2 28.5 146 7.00 26.2 147 6.50 28.2 148 7.00 26.2 149 7.00 26.2 150 7.00 26.2 7.43 -130.2 28.5 Anammox Hybrid Reactor 128 Sample Number Flow Rate(ml/min) HRT (hr) pH ORP Temp 151 6.50 28.2 152 6.50 28.2 153 6.50 28.2 154 6.50 28.2 155 6.50 28.2 156 6.50 28.2 6.87 -153.5 30.8 157 7.00 26.2 7.43 -130.2 28.5 158 6.50 28.2 159 7.00 26.2 160 22.50 8.1 6.95 -146.2 29.7 161 6.50 28.2 162 6.00 30.6 163 6.00 30.6 7.16 29.4 -129.9 164 6.50 28.2 165 6.00 30.6 166 6.50 28.2 167 6.00 30.6 7.01 32.3 -133.3 168 6.00 30.6 169 6.00 30.6 170 6.50 28.2 171 6.00 30.6 6.95 30.1 -137.6 172 6.00 30.6 7.23 24.3 -88.7 Anammox Hybrid Reactor 129 Sample Number TOC(mg/L) SOC(mg/L) NH4-N NOx NO3-N NO2-N Corrected NOx Alak(mg/L CaCO3) 1 21.00 13.00 9.71 3.30 13.01 2 18.50 12.40 9.61 3.03 12.64 3 35.50 34.30 17.40 6.30 11.10 17.40 115.00 4 21.70 12.50 9.83 2.92 12.75 5 16.00 15.00 45.90 38.20 13.07 25.60 38.67 6 15.00 15.00 49.50 38.40 10.06 28.70 38.76 7 25.80 15.20 8.46 6.75 15.21 8 20.40 13.70 10.00 3.95 13.95 9 14.80 14.20 9.50 4.94 14.44 10 29.10 11.50 9.61 1.90 11.51 11 35.30 13.40 9.66 3.75 13.41 12 19.80 26.20 24.70 12.51 12.20 24.71 13 23.90 16.30 12.36 3.95 16.31 14 21.80 29.60 21.00 12.03 8.97 21.00 15 18.40 24.30 26.20 0.56 26.76 16 24.00 30.10 25.40 10.70 14.70 25.40 17 20.20 23.00 23.52 1.69 25.21 18 21.70 34.90 26.80 10.20 16.60 26.80 19 30.20 21.90 12.08 9.83 21.91 20 18.50 24.30 26.21 0.56 26.76 21 19.10 22.70 23.42 1.48 24.90 22 19.60 22.20 22.85 1.50 24.35 23 20.90 23.50 31.37 1.51 32.88 24 20.50 26.60 18.90 11.42 7.48 18.90 25 15.00 31.30 29.90 1.40 31.30 26 14.70 29.80 28.45 1.35 29.80 27 71.00 15.00 31.90 32.00 11.10 21.30 32.40 28 16.90 22.50 23.01 1.65 24.66 29 18.20 22.40 22.00 2.47 24.47 300.00 30 14.70 33.30 31.91 1.39 33.30 31 14.00 13.00 17.80 23.10 23.20 2.08 25.28 32 16.60 23.30 23.54 1.97 25.51 33 17.30 21.20 21.16 2.03 23.19 34 17.50 23.40 22.99 2.57 25.56 35 15.20 24.90 26.81 0.61 27.42 36 17.00 24.30 24.80 1.83 26.63 37 14.90 11.10 10.35 1.01 11.36 38 17.70 22.50 22.09 2.49 24.58 39 15.00 15.00 25.70 29.10 8.71 20.70 29.41 40 16.00 22.70 23.20 1.68 24.88 41 17.00 14.00 30.00 32.80 10.68 22.50 33.18 42 17.50 20.70 20.68 1.96 22.64 43 30.50 40.40 26.80 5.00 21.80 26.80 44 13.10 19.50 21.21 0.28 21.49 45 20.20 24.40 32.04 1.94 33.98 46 27.50 48.40 27.20 21.20 48.40 47 13.00 12.00 18.00 23.10 23.31 1.98 25.29 48 21.90 38.00 30.60 5.70 24.90 30.60 49 12.00 13.80 19.00 20.25 0.65 20.90 50 63.00 31.80 32.00 6.10 25.90 32.00 Hybrid Anammox Reactor Effluent 130 Sample Number TOC(mg/L) SOC(mg/L) NH4-N NOx NO3-N NO2-N Corrected NOx Alak(mg/L CaCO3) 51 45.00 14.00 19.80 18.10 7.70 10.40 18.10 52 30.10 47.80 27.40 20.40 47.80 53 12.90 19.60 21.10 0.49 21.58 54 30.60 48.20 27.30 20.90 48.20 55 13.00 15.20 19.70 21.19 0.50 21.69 56 14.00 12.00 15.40 22.30 22.63 1.80 24.43 57 15.50 22.70 23.16 1.72 24.88 58 32.20 25.10 9.50 15.60 25.10 59 14.10 33.30 32.53 1.10 33.63 60 14.00 14.00 22.20 35.00 11.50 23.50 35.00 61 13.50 33.40 32.64 1.09 33.73 62 14.90 25.60 27.65 0.55 28.20 63 25.00 19.00 14.70 19.80 17.09 2.90 19.99 64 19.60 36.30 28.75 8.47 37.22 65 20.00 36.20 28.49 8.62 37.11 66 16.00 12.00 22.80 35.70 11.30 24.40 35.70 67 13.40 27.40 27.34 0.33 27.67 68 13.30 32.80 32.04 1.08 33.12 69 26.20 48.40 38.93 14.30 53.23 70 26.40 52.10 37.67 19.10 56.77 71 11.00 17.60 41.60 33.00 12.00 45.00 72 34.70 61.00 38.93 26.90 65.83 73 13.70 24.30 33.02 1.15 34.17 74 14.00 26.40 26.34 0.33 26.66 75 22.40 48.10 35.56 16.20 51.76 76 13.50 22.90 31.11 1.09 32.20 77 15.10 12.00 19.30 44.00 30.90 13.10 44.00 78 21.00 15.00 33.80 45.20 8.33 37.10 45.43 79 21.70 49.30 38.93 15.20 54.13 80 27.00 51.40 37.10 18.90 56.00 81 13.30 24.40 33.12 1.18 34.30 12.00 82 25.00 14.00 32.60 34.50 36.00 34.50 83 12.30 16.60 45.50 30.80 14.70 45.50 40.00 84 14.60 35.60 28.11 8.39 36.50 85 25.00 19.00 15.00 19.80 17.07 2.92 19.99 86 13.00 26.40 26.32 0.35 26.66 87 17.50 34.30 27.83 7.36 35.19 88 16.30 36.90 29.65 8.20 37.85 103.00 89 23.60 48.90 38.13 15.50 53.63 90 27.30 52.50 37.90 19.30 57.20 91 28.40 62.20 45.93 20.40 66.33 92 22.10 46.80 32.31 18.50 50.81 93 22.60 48.90 35.23 17.30 52.53 94 12.50 14.80 36.40 29.35 7.99 37.34 95 12.50 16.10 46.60 31.30 15.30 46.60 40.00 96 10.90 11.70 41.30 33.33 11.40 44.73 97 15.60 11.40 22.40 48.30 28.20 20.10 48.30 98 20.40 45.70 34.78 14.50 49.28 99 13.50 34.70 29.70 5.30 35.00 100 12.10 18.10 41.10 32.22 12.20 44.42 Hybrid Anammox Reactor Effluent 131 Sample Number TOC(mg/L) SOC(mg/L) NH4-N NOx NO3-N NO2-N Corrected NOx Alak(mg/L CaCO3) 101 16.10 12.40 21.70 47.70 27.80 19.90 47.70 102 11.70 38.30 31.97 6.33 38.30 103 16.40 34.70 28.10 7.50 35.60 104 13.90 35.80 30.65 5.46 36.11 105 21.50 43.90 32.55 14.70 47.25 106 21.00 16.00 14.60 20.80 18.66 2.35 21.01 107 23.20 48.20 34.78 17.00 51.78 108 17.80 11.50 22.40 47.70 28.70 19.00 47.70 109 15.10 25.70 27.63 0.66 28.30 110 10.70 37.00 30.78 6.22 37.00 111 21.80 13.80 18.50 50.80 31.00 19.80 50.80 112 20.00 15.00 10.80 16.80 15.03 1.94 16.97 113 16.00 15.30 17.50 12.04 5.80 17.84 114 11.40 38.00 35.22 3.91 39.13 115 16.80 37.40 32.58 5.86 38.44 116 22.20 46.80 32.88 18.00 50.88 117 15.00 12.00 21.00 34.10 11.10 23.00 34.10 118 13.20 36.10 31.02 5.39 36.41 119 16.70 13.60 21.40 44.60 32.33 15.60 47.93 120 12.60 17.70 43.30 29.10 14.20 43.30 40.00 121 13.00 12.00 26.40 39.00 11.42 27.90 39.32 122 10.70 15.80 14.00 1.95 15.95 123 23.50 51.00 38.47 17.30 55.77 124 21.00 16.00 14.90 20.10 17.95 2.35 20.30 125 16.70 36.80 29.60 8.15 37.75 126 12.10 18.00 34.50 25.44 9.57 35.01 127 15.50 12.00 17.70 44.00 31.00 13.00 44.00 128 19.40 48.90 32.42 20.50 52.92 129 15.10 38.50 33.65 5.93 39.58 130 20.00 15.00 11.70 14.80 13.17 1.77 14.94 131 14.60 15.00 47.30 34.30 13.00 47.30 132 16.40 33.20 24.87 9.13 34.00 133 16.30 12.30 14.70 43.70 28.40 15.30 43.70 134 16.50 14.30 14.30 45.80 33.50 12.30 45.80 135 14.70 12.10 18.30 44.10 30.70 13.40 44.10 136 18.40 49.40 30.30 19.10 49.40 137 17.10 34.80 28.06 7.64 35.70 138 16.50 12.80 12.30 30.10 23.79 6.31 30.10 139 19.20 49.10 32.76 20.40 53.16 140 15.70 12.80 16.20 45.90 30.10 15.80 45.90 38.50 141 16.30 12.50 16.10 32.50 21.20 11.30 32.50 142 11.10 38.10 35.23 4.00 39.23 143 19.80 45.20 30.14 18.80 48.94 144 16.80 49.20 32.30 16.90 49.20 145 18.70 44.60 28.70 15.90 44.60 146 14.10 11.50 17.40 45.00 31.70 13.30 45.00 54.00 147 15.40 35.00 26.32 9.52 35.84 148 14.70 15.80 18.30 44.30 30.70 13.60 44.30 54.00 149 14.20 11.10 17.70 44.40 31.10 13.30 44.40 54.00 150 17.40 45.10 28.90 16.20 45.10 Hybrid Anammox Reactor Effluent 132 Sample Number TOC(mg/L) SOC(mg/L) NH4-N NOx NO3-N NO2-N Corrected NOx Alak(mg/L CaCO3) 151 17.40 48.70 29.80 18.90 48.70 152 21.80 14.60 13.50 30.00 23.94 6.06 30.00 153 14.00 42.80 31.40 11.40 42.80 154 19.80 38.40 27.38 11.90 39.28 155 16.80 38.10 26.34 12.60 38.94 156 14.20 32.20 20.90 11.30 32.20 157 18.60 45.30 28.90 16.40 45.30 158 15.70 12.30 16.10 31.20 20.80 10.40 31.20 159 12.50 16.70 46.50 31.20 15.30 46.50 160 19.40 39.00 11.42 27.90 39.32 161 16.90 47.30 30.50 16.80 47.30 162 7.88 31.20 30.64 0.56 31.20 163 7.05 31.90 31.22 0.68 31.90 164 13.40 29.30 23.30 6.00 29.30 165 6.99 30.80 28.35 2.45 30.80 166 15.90 39.60 28.00 12.50 40.50 167 7.53 67.70 65.10 2.60 67.70 168 7.35 30.50 29.87 0.63 30.50 169 7.41 33.90 33.23 0.67 33.90 170 16.70 13.60 17.00 49.30 32.40 16.90 49.30 171 7.13 30.60 27.91 2.69 30.60 172 6.62 26.80 26.50 0.30 26.80 Hybrid Anammox Reactor Effluent 133 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 1 67.05 65.52 90.18 1.63 0.79 0.44 9.96 4.70 3.57 2 59.97 55.64 87.73 1.22 0.48 0.28 6.67 2.43 2.27 3 54.29 47.23 63.83 1.79 1.12 0.69 8.84 4.82 3.98 4 61.49 56.77 90.73 1.41 0.51 0.32 7.86 2.61 2.62 5 41.43 42.84 2.27 1.72 1.09 8.57 6.71 0.00 6 39.21 35.96 42.94 2.29 1.66 1.12 8.16 5.42 4.36 7 62.21 53.51 83.21 1.72 0.72 0.52 9.72 3.50 3.94 8 62.65 56.50 88.71 1.45 0.47 0.35 8.24 2.43 2.85 9 66.86 66.82 85.34 1.39 0.45 0.34 8.42 2.73 2.64 10 58.74 41.80 95.09 1.56 0.65 0.50 8.32 2.46 4.34 11 46.60 24.25 89.73 1.44 0.60 0.47 6.12 1.33 3.86 12 50.24 48.12 69.80 1.62 0.76 0.61 7.40 3.34 3.88 13 46.26 36.60 87.13 1.18 0.49 0.40 4.98 1.63 3.15 14 47.13 40.44 77.91 1.52 0.75 0.61 6.49 2.76 4.35 15 54.77 57.60 98.43 1.50 0.37 0.31 7.44 1.96 2.76 16 44.33 40.16 65.33 1.58 0.76 0.64 6.36 2.78 3.81 17 55.78 53.78 95.55 1.55 0.38 0.33 7.85 1.85 2.85 18 39.39 31.30 62.95 1.61 0.77 0.68 5.77 2.19 3.88 19 1.08 0.46 0.41 20 55.14 56.37 98.54 1.51 0.37 0.33 7.57 1.88 2.95 21 57.22 55.48 96.19 1.55 0.37 0.34 8.05 1.87 2.93 22 55.44 53.11 96.04 1.49 0.36 0.33 7.49 1.74 2.86 23 53.99 51.84 96.18 1.53 0.41 0.37 7.50 1.91 3.23 24 53.14 44.58 83.04 1.54 0.86 0.79 7.43 3.50 5.99 25 49.73 61.04 96.08 1.46 0.36 0.33 6.60 2.00 2.92 26 50.33 60.16 96.06 1.42 0.35 0.32 6.49 1.89 2.80 27 45.89 40.93 50.08 1.87 1.16 1.09 7.80 4.31 4.95 28 60.44 60.79 95.93 1.58 0.37 0.35 8.67 2.06 3.05 29 58.87 60.94 94.36 1.56 0.40 0.38 8.37 2.23 3.25 30 48.99 61.01 96.08 1.49 0.35 0.33 6.64 1.96 2.90 31 58.69 59.36 94.96 1.57 0.38 0.36 8.37 2.04 3.08 32 59.20 61.40 95.18 1.55 0.37 0.35 8.34 2.07 3.06 33 59.64 61.81 95.31 1.51 0.39 0.37 8.19 2.20 3.24 34 58.81 61.71 94.13 1.57 0.39 0.38 8.41 2.21 3.24 35 55.79 60.52 98.35 1.44 0.33 0.32 7.29 1.83 2.87 36 57.77 60.56 95.60 1.55 0.37 0.36 8.14 2.05 3.12 37 66.67 57.55 97.03 1.24 0.35 0.34 7.49 1.85 3.02 38 58.13 60.31 94.28 1.52 0.39 0.38 8.04 2.11 3.22 39 48.88 1.70 1.05 1.02 7.55 0.00 0.00 40 62.02 64.76 96.24 1.61 0.39 0.39 9.10 2.31 3.38 41 43.53 40.83 1.76 1.09 1.08 6.97 4.04 0.00 42 60.08 60.85 95.59 1.52 0.39 0.38 8.28 2.14 3.33 43 1.74 1.07 1.07 0.00 0.00 0.00 44 58.37 61.92 99.17 1.24 0.30 0.30 6.58 1.67 2.66 45 51.20 49.12 95.13 1.45 0.37 0.37 6.74 1.66 3.22 46 30.87 42.47 56.02 1.74 0.48 0.49 4.88 1.86 2.47 47 57.41 56.42 95.25 1.53 0.36 0.36 7.98 1.83 3.12 48 1.78 1.06 1.08 0.00 0.00 0.00 49 57.84 59.41 98.13 1.23 0.29 0.30 6.48 1.59 2.67 50 1.37 0.85 0.87 0.00 0.00 0.00 Anammox Hybrid System Performance 134 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 1 67.05 65.52 90.18 1.63 0.79 0.44 9.96 4.70 3.57 2 59.97 55.64 87.73 1.22 0.48 0.28 6.67 2.43 2.27 3 54.29 47.23 63.83 1.79 1.12 0.69 8.84 4.82 3.98 4 61.49 56.77 90.73 1.41 0.51 0.32 7.86 2.61 2.62 5 41.43 42.84 2.27 1.72 1.09 8.57 6.71 0.00 6 39.21 35.96 42.94 2.29 1.66 1.12 8.16 5.42 4.36 7 62.21 53.51 83.21 1.72 0.72 0.52 9.72 3.50 3.94 8 62.65 56.50 88.71 1.45 0.47 0.35 8.24 2.43 2.85 9 66.86 66.82 85.34 1.39 0.45 0.34 8.42 2.73 2.64 10 58.74 41.80 95.09 1.56 0.65 0.50 8.32 2.46 4.34 11 46.60 24.25 89.73 1.44 0.60 0.47 6.12 1.33 3.86 12 50.24 48.12 69.80 1.62 0.76 0.61 7.40 3.34 3.88 13 46.26 36.60 87.13 1.18 0.49 0.40 4.98 1.63 3.15 14 47.13 40.44 77.91 1.52 0.75 0.61 6.49 2.76 4.35 15 54.77 57.60 98.43 1.50 0.37 0.31 7.44 1.96 2.76 16 44.33 40.16 65.33 1.58 0.76 0.64 6.36 2.78 3.81 17 55.78 53.78 95.55 1.55 0.38 0.33 7.85 1.85 2.85 18 39.39 31.30 62.95 1.61 0.77 0.68 5.77 2.19 3.88 19 1.08 0.46 0.41 20 55.14 56.37 98.54 1.51 0.37 0.33 7.57 1.88 2.95 21 57.22 55.48 96.19 1.55 0.37 0.34 8.05 1.87 2.93 22 55.44 53.11 96.04 1.49 0.36 0.33 7.49 1.74 2.86 23 53.99 51.84 96.18 1.53 0.41 0.37 7.50 1.91 3.23 24 53.14 44.58 83.04 1.54 0.86 0.79 7.43 3.50 5.99 25 49.73 61.04 96.08 1.46 0.36 0.33 6.60 2.00 2.92 26 50.33 60.16 96.06 1.42 0.35 0.32 6.49 1.89 2.80 27 45.89 40.93 50.08 1.87 1.16 1.09 7.80 4.31 4.95 28 60.44 60.79 95.93 1.58 0.37 0.35 8.67 2.06 3.05 29 58.87 60.94 94.36 1.56 0.40 0.38 8.37 2.23 3.25 30 48.99 61.01 96.08 1.49 0.35 0.33 6.64 1.96 2.90 31 58.69 59.36 94.96 1.57 0.38 0.36 8.37 2.04 3.08 32 59.20 61.40 95.18 1.55 0.37 0.35 8.34 2.07 3.06 33 59.64 61.81 95.31 1.51 0.39 0.37 8.19 2.20 3.24 34 58.81 61.71 94.13 1.57 0.39 0.38 8.41 2.21 3.24 35 55.79 60.52 98.35 1.44 0.33 0.32 7.29 1.83 2.87 36 57.77 60.56 95.60 1.55 0.37 0.36 8.14 2.05 3.12 37 66.67 57.55 97.03 1.24 0.35 0.34 7.49 1.85 3.02 38 58.13 60.31 94.28 1.52 0.39 0.38 8.04 2.11 3.22 39 48.88 1.70 1.05 1.02 7.55 0.00 0.00 40 62.02 64.76 96.24 1.61 0.39 0.39 9.10 2.31 3.38 41 43.53 40.83 1.76 1.09 1.08 6.97 4.04 0.00 42 60.08 60.85 95.59 1.52 0.39 0.38 8.28 2.14 3.33 43 1.74 1.07 1.07 0.00 0.00 0.00 44 58.37 61.92 99.17 1.24 0.30 0.30 6.58 1.67 2.66 45 51.20 49.12 95.13 1.45 0.37 0.37 6.74 1.66 3.22 46 30.87 42.47 56.02 1.74 0.48 0.49 4.88 1.86 2.47 47 57.41 56.42 95.25 1.53 0.36 0.36 7.98 1.83 3.12 48 1.78 1.06 1.08 0.00 0.00 0.00 49 57.84 59.41 98.13 1.23 0.29 0.30 6.48 1.59 2.67 50 1.37 0.85 0.87 Anammox Hybrid System Performance 135 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 51 68.91 63.20 73.42 1.93 1.15 1.19 12.10 6.63 7.92 52 28.20 35.27 57.59 1.72 0.47 0.48 4.41 1.50 2.54 53 57.68 60.91 98.58 1.22 0.29 0.30 6.38 1.58 2.65 54 1.71 0.45 0.48 0.00 0.00 0.00 55 54.79 53.52 98.58 1.22 0.28 0.30 6.09 1.37 2.73 56 61.53 63.07 96.01 1.55 0.36 0.39 8.68 2.07 3.40 57 62.10 63.53 96.29 1.60 0.37 0.40 9.01 2.12 3.51 58 39.75 26.98 50.78 1.51 0.79 0.87 5.44 1.95 4.02 59 52.31 65.53 97.62 1.57 0.38 0.43 7.49 2.28 3.84 60 46.89 54.23 57.12 1.71 1.36 1.54 7.27 6.71 7.99 61 53.19 67.23 97.67 1.59 0.39 0.44 7.68 2.36 3.89 62 52.24 54.29 98.51 1.34 0.28 0.32 6.38 1.39 2.87 63 73.13 74.83 95.67 2.03 0.50 0.58 13.52 3.43 5.03 64 46.81 52.31 82.46 1.66 0.36 0.42 7.08 1.69 3.13 65 47.82 53.38 83.16 1.71 0.37 0.44 7.42 1.80 3.34 66 44.44 51.39 56.43 1.67 1.32 1.57 6.74 6.15 8.07 67 59.36 66.58 99.31 1.59 0.38 0.45 8.58 2.27 4.11 68 50.70 61.34 97.42 1.48 0.32 0.39 6.83 1.80 3.47 69 1.57 0.37 0.46 70 1.57 0.37 0.46 71 41.50 54.05 74.58 1.60 0.36 0.44 6.05 1.76 3.00 72 2.02 0.48 0.60 73 59.92 63.56 97.56 1.50 0.35 0.44 8.18 2.03 3.91 74 59.19 63.73 99.33 1.57 0.36 0.45 8.44 2.09 4.11 75 41.00 52.84 73.04 1.89 0.44 0.56 7.06 2.14 3.74 76 61.44 63.11 97.65 1.50 0.34 0.43 8.35 1.97 3.86 77 25.79 37.94 67.49 1.35 0.31 0.41 3.17 1.08 2.49 78 30.76 1.81 0.70 0.91 5.05 0.00 0.00 79 30.26 40.71 68.00 1.61 0.37 0.48 4.44 1.37 2.96 80 26.23 60.21 1.61 0.37 0.48 0.00 0.88 2.62 81 59.72 63.56 97.51 1.48 0.34 0.44 8.05 1.97 3.93 82 39.93 1.77 0.68 0.88 6.42 0.00 0.00 83 24.91 47.47 64.32 1.31 0.32 0.42 2.97 1.37 2.43 84 50.93 61.88 83.25 1.62 0.36 0.47 7.50 2.02 3.55 85 71.12 70.70 95.64 1.91 0.44 0.58 12.34 2.84 5.03 86 58.66 63.89 99.27 1.51 0.34 0.45 8.05 1.96 4.03 87 50.71 57.21 86.42 1.66 0.35 0.47 7.68 1.84 3.68 88 50.09 61.83 85.54 1.69 0.37 0.49 7.69 2.07 3.81 89 33.33 67.23 1.58 0.36 0.48 1.08 2.91 90 1.58 0.36 0.48 91 34.81 59.25 1.46 0.34 0.46 0.00 1.08 2.47 92 39.97 50.44 71.73 1.89 0.43 0.57 6.85 1.96 3.74 93 51.61 61.36 84.55 1.68 0.36 0.48 7.86 2.00 3.72 94 50.61 65.31 1.39 0.33 0.44 0.00 1.51 2.64 95 44.68 65.89 75.43 1.52 0.32 0.43 6.16 1.92 2.98 96 32.02 38.96 59.56 1.65 0.37 0.50 4.80 1.31 2.71 97 45.19 56.69 77.27 1.91 0.44 0.60 7.85 2.27 4.19 98 54.74 65.56 90.02 1.69 0.37 0.50 8.40 2.19 4.07 99 38.91 47.54 73.93 1.53 0.32 0.44 5.43 1.40 2.94 100 33.21 40.87 60.04 1.65 0.37 0.50 4.97 1.37 2.74 Anammox Hybrid System Performance 136 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 51 68.91 63.20 73.42 1.93 1.15 1.19 12.10 6.63 7.92 52 28.20 35.27 57.59 1.72 0.47 0.48 4.41 1.50 2.54 53 57.68 60.91 98.58 1.22 0.29 0.30 6.38 1.58 2.65 54 1.71 0.45 0.48 0.00 0.00 0.00 55 54.79 53.52 98.58 1.22 0.28 0.30 6.09 1.37 2.73 56 61.53 63.07 96.01 1.55 0.36 0.39 8.68 2.07 3.40 57 62.10 63.53 96.29 1.60 0.37 0.40 9.01 2.12 3.51 58 39.75 26.98 50.78 1.51 0.79 0.87 5.44 1.95 4.02 59 52.31 65.53 97.62 1.57 0.38 0.43 7.49 2.28 3.84 60 46.89 54.23 57.12 1.71 1.36 1.54 7.27 6.71 7.99 61 53.19 67.23 97.67 1.59 0.39 0.44 7.68 2.36 3.89 62 52.24 54.29 98.51 1.34 0.28 0.32 6.38 1.39 2.87 63 73.13 74.83 95.67 2.03 0.50 0.58 13.52 3.43 5.03 64 46.81 52.31 82.46 1.66 0.36 0.42 7.08 1.69 3.13 65 47.82 53.38 83.16 1.71 0.37 0.44 7.42 1.80 3.34 66 44.44 51.39 56.43 1.67 1.32 1.57 6.74 6.15 8.07 67 59.36 66.58 99.31 1.59 0.38 0.45 8.58 2.27 4.11 68 50.70 61.34 97.42 1.48 0.32 0.39 6.83 1.80 3.47 69 1.57 0.37 0.46 70 1.57 0.37 0.46 71 41.50 54.05 74.58 1.60 0.36 0.44 6.05 1.76 3.00 72 2.02 0.48 0.60 73 59.92 63.56 97.56 1.50 0.35 0.44 8.18 2.03 3.91 74 59.19 63.73 99.33 1.57 0.36 0.45 8.44 2.09 4.11 75 41.00 52.84 73.04 1.89 0.44 0.56 7.06 2.14 3.74 76 61.44 63.11 97.65 1.50 0.34 0.43 8.35 1.97 3.86 77 25.79 37.94 67.49 1.35 0.31 0.41 3.17 1.08 2.49 78 30.76 1.81 0.70 0.91 5.05 0.00 0.00 79 30.26 40.71 68.00 1.61 0.37 0.48 4.44 1.37 2.96 80 26.23 60.21 1.61 0.37 0.48 0.00 0.88 2.62 81 59.72 63.56 97.51 1.48 0.34 0.44 8.05 1.97 3.93 82 39.93 1.77 0.68 0.88 6.42 0.00 0.00 83 24.91 47.47 64.32 1.31 0.32 0.42 2.97 1.37 2.43 84 50.93 61.88 83.25 1.62 0.36 0.47 7.50 2.02 3.55 85 71.12 70.70 95.64 1.91 0.44 0.58 12.34 2.84 5.03 86 58.66 63.89 99.27 1.51 0.34 0.45 8.05 1.96 4.03 87 50.71 57.21 86.42 1.66 0.35 0.47 7.68 1.84 3.68 88 50.09 61.83 85.54 1.69 0.37 0.49 7.69 2.07 3.81 89 33.33 67.23 1.58 0.36 0.48 1.08 2.91 90 1.58 0.36 0.48 91 34.81 59.25 1.46 0.34 0.46 0.00 1.08 2.47 92 39.97 50.44 71.73 1.89 0.43 0.57 6.85 1.96 3.74 93 51.61 61.36 84.55 1.68 0.36 0.48 7.86 2.00 3.72 94 50.61 65.31 1.39 0.33 0.44 0.00 1.51 2.64 95 44.68 65.89 75.43 1.52 0.32 0.43 6.16 1.92 2.98 96 32.02 38.96 59.56 1.65 0.37 0.50 4.80 1.31 2.71 97 45.19 56.69 77.27 1.91 0.44 0.60 7.85 2.27 4.19 98 54.74 65.56 90.02 1.69 0.37 0.50 8.40 2.19 4.07 99 38.91 47.54 73.93 1.53 0.32 0.44 5.43 1.40 2.94 100 33.21 40.87 60.04 1.65 0.37 0.50 4.97 1.37 2.74 Anammox Hybrid System Performance 137 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 101 54.42 70.60 88.34 1.74 0.34 0.47 8.60 2.21 3.77 102 51.19 59.31 86.39 1.66 0.35 0.48 7.72 1.88 3.74 103 52.58 63.61 89.64 1.66 0.36 0.49 7.93 2.07 4.02 104 46.83 55.58 78.06 1.95 0.45 0.63 8.29 2.29 4.45 105 70.05 69.65 96.47 1.87 0.42 0.58 11.92 2.63 5.05 106 39.34 47.63 72.58 1.86 0.41 0.58 6.67 1.80 3.83 107 32.21 37.43 62.30 1.64 0.36 0.51 4.80 1.23 2.88 108 48.03 42.59 98.21 1.24 0.23 0.32 5.43 0.88 2.86 109 55.63 72.06 88.52 1.70 0.33 0.47 8.61 2.17 3.77 110 1.41 0.32 0.45 0.00 0.00 0.00 111 73.44 73.91 96.72 1.65 0.36 0.51 10.99 2.40 4.50 112 68.36 63.74 90.39 1.64 0.36 113 54.09 68.42 92.48 1.70 0.31 0.45 8.38 1.94 3.78 114 46.23 58.00 89.90 1.60 0.35 0.50 6.71 1.82 4.10 115 31.62 35.65 64.07 1.60 0.35 0.51 4.59 1.13 2.94 116 43.66 45.88 59.22 1.55 1.09 1.58 6.15 4.54 8.53 117 51.95 63.33 89.71 1.63 0.34 0.49 7.68 1.94 4.00 118 44.86 51.91 76.11 1.90 0.42 0.61 7.73 1.97 4.23 119 29.07 40.80 67.65 1.36 0.30 0.44 3.60 1.12 2.72 120 32.79 31.07 50.53 1.54 1.08 1.58 4.59 3.04 7.28 121 74.64 74.15 96.81 1.66 0.36 0.53 11.23 2.41 4.65 122 29.43 64.84 1.55 0.34 0.50 0.00 0.90 2.92 123 69.62 66.96 96.48 1.82 0.39 0.58 11.55 2.37 5.06 124 48.46 57.40 86.02 1.64 0.34 0.50 7.24 1.77 3.94 125 48.12 51.48 82.66 1.60 0.35 0.52 7.01 1.63 3.88 126 27.50 39.38 70.25 1.35 0.29 0.44 3.37 1.05 2.81 127 24.61 36.18 54.95 1.44 0.31 0.46 3.21 1.01 2.29 128 48.16 61.48 89.93 1.64 0.34 0.51 7.17 1.89 4.16 129 73.92 70.75 97.08 1.61 0.35 0.52 10.81 2.22 4.62 130 28.88 52.38 72.80 1.39 0.29 0.45 3.64 1.40 2.96 131 52.12 55.91 83.93 1.64 0.35 0.53 7.78 1.77 4.06 132 32.49 51.64 67.10 1.37 0.31 0.47 4.05 1.44 2.86 133 32.01 55.31 74.95 1.40 0.30 0.46 4.08 1.51 3.13 134 27.44 38.38 70.68 1.36 0.30 0.46 3.40 1.04 2.96 135 27.25 46.20 63.89 1.48 0.32 0.50 3.66 1.34 2.88 136 48.72 52.10 86.26 1.60 0.31 0.48 7.10 1.46 3.77 137 46.19 60.45 86.99 1.25 0.29 0.45 5.24 1.60 3.59 138 34.47 55.65 1.42 0.30 0.46 0.00 0.93 2.35 139 42.14 64.73 1.33 0.28 0.45 0.00 1.08 2.66 140 37.61 44.29 75.59 1.23 0.27 0.43 4.22 1.09 2.98 141 52.78 66.06 92.37 1.65 0.28 0.45 7.92 1.70 3.80 142 30.77 59.22 1.42 0.29 0.46 0.00 0.81 2.50 143 30.75 52.81 70.81 1.51 0.33 0.54 4.22 1.60 3.49 144 30.52 39.87 68.76 1.44 0.31 0.51 4.00 1.14 3.21 145 1.34 0.28 0.45 0.00 0.00 0.00 146 50.88 56.25 83.61 1.63 0.33 0.54 7.52 1.68 4.13 147 1.34 0.28 0.47 0.00 0.00 0.00 148 1.34 0.28 0.47 0.00 0.00 0.00 149 31.09 44.05 68.73 1.44 0.31 0.52 4.06 1.26 3.26 150 28.85 48.21 66.31 1.47 0.31 0.53 3.86 1.38 3.17 Anammox Hybrid System Performance 138 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 151 43.65 55.00 88.05 1.22 0.28 0.47 4.85 1.40 3.80 152 36.18 53.33 77.51 1.41 0.28 0.47 4.64 1.36 3.34 153 43.88 45.75 80.71 1.64 0.34 0.58 6.55 1.42 4.24 154 47.26 54.10 79.74 1.65 0.34 0.58 7.08 1.68 4.22 155 39.35 50.18 76.70 1.21 0.27 0.45 4.33 1.22 3.17 156 28.76 36.52 67.40 1.42 0.30 0.51 3.72 0.98 3.11 157 39.28 40.81 77.73 1.23 0.25 0.44 4.41 0.94 3.09 158 1.34 0.28 0.48 0.00 0.00 0.00 159 43.14 46.26 55.29 1.63 1.17 2.02 6.38 4.92 10.16 160 30.89 50.15 71.33 1.47 0.32 0.55 4.13 1.45 3.56 161 61.35 74.08 98.95 1.60 0.26 0.46 8.93 1.77 4.11 162 61.17 76.42 98.70 1.59 0.26 0.45 8.83 1.79 4.07 163 44.83 53.95 88.28 1.23 0.27 0.48 5.00 1.34 3.85 164 59.58 75.39 95.29 1.48 0.25 0.45 8.02 1.68 3.89 165 46.17 54.18 80.56 1.63 0.32 0.60 6.85 1.60 4.41 166 51.12 74.82 95.45 2.44 0.26 0.49 11.33 1.76 4.28 167 61.57 73.56 98.82 1.56 0.24 0.46 8.73 1.61 4.12 168 70.15 74.80 98.82 2.19 0.25 0.49 13.98 1.73 4.43 169 1.40 0.27 0.54 170 61.38 74.07 95.08 1.55 0.24 0.47 8.64 1.60 4.09 171 74.01 76.85 99.48 2.04 0.25 0.50 13.71 1.73 4.48 Anammox Hybrid System Performance 139 Sample Number Flow Rate (mL/min) HRT (hr) pH ORP Temp 1 5.00 2 4.85 12.03 7.01 35.10 3 5.00 11.67 4 4.50 12.96 7.00 32.40 5 8.00 7.29 6 7.00 8.33 7.18 -118.00 31.80 7 5.00 11.67 6.59 28.90 8 4.00 14.58 6.79 27.50 9 4.00 14.58 6.64 37.70 10 7.00 6.59 -100.20 29.20 11 7.00 8.33 6.92 -56.80 29.70 12 5.00 6.96 29.50 13 10.00 14 7.50 7.78 15 10.00 16 7.50 7.78 17 10.00 5.83 6.69 -117.00 28.90 18 5.00 6.76 28.10 19 7.50 7.78 6.97 -138.20 31.60 20 7.50 7.78 21 7.50 7.78 6.94 -144.80 32.70 22 3.00 19.44 7.11 -81.50 32.70 23 12.50 4.67 6.76 -132.00 29.80 24 3.00 19.44 7.00 -110.00 32.80 25 3.00 19.44 26 6.00 9.72 27 7.50 7.78 28 7.50 7.78 6.95 -97.90 30.80 29 3.00 19.44 30 7.50 7.78 6.95 -149.60 31.40 31 7.50 7.78 32 7.50 7.78 33 7.50 7.78 34 7.50 7.78 6.86 -136.60 33.90 35 3.00 19.44 6.77 35.30 36 7.50 7.78 37 6.00 9.72 7.16 -90.00 32.10 38 7.50 7.78 39 7.00 8.33 7.09 -96.70 32.40 40 7.50 7.78 41 5.00 11.67 42 7.50 7.78 43 3.00 19.44 44 7.50 7.78 45 5.00 11.67 46 7.50 7.78 47 6.00 9.72 48 6.00 9.72 49 7.50 7.78 50 7.50 7.78 7.11 -106.90 31.30 Fixed Bed Anammox Reactor 140 Sample Number Flow Rate (mL/min) HRT (hr) pH ORP Temp 51 7.50 7.78 6.87 -140.50 30.60 52 7.50 7.78 53 4.50 12.96 54 7.50 7.78 55 7.50 7.78 7.17 -71.30 30.10 56 7.50 7.78 6.86 -136.60 33.90 57 7.50 7.78 7.12 -120.50 31.40 58 4.50 12.96 7.56 -109.50 34.00 59 4.50 12.96 60 7.50 7.78 7.13 -45.20 32.80 61 4.50 12.96 62 7.50 7.78 7.16 -139.40 30.20 63 4.50 12.96 7.85 -133.50 34.00 64 4.50 12.96 7.51 -128.60 34.00 65 4.50 12.96 7.84 -131.30 36.00 66 3.00 19.44 67 4.50 12.96 68 3.00 19.44 69 3.00 19.44 70 7.50 7.78 7.03 -80.50 31.30 71 4.50 12.96 72 4.50 12.96 7.51 -128.60 34.00 73 4.50 12.96 7.84 -131.30 36.00 74 3.00 19.44 6.93 -101.30 31.40 75 3.50 16.67 76 7.50 7.78 77 7.50 7.78 7.12 -120.50 31.40 78 7.50 7.78 7.03 -80.50 31.30 79 7.50 7.78 80 7.50 7.78 7.04 -138.80 32.10 81 4.50 12.96 7.51 -128.60 34.00 82 4.50 12.96 7.84 -131.30 36.00 83 4.50 12.96 7.39 -122.00 34.00 84 4.50 12.96 7.38 -110.30 29.00 85 3.50 16.67 86 3.00 19.44 7.02 -94.70 35.30 87 4.50 12.96 7.24 -134.60 31.50 88 3.00 19.44 89 7.50 7.78 90 3.00 19.44 91 4.50 12.96 7.24 -134.60 31.50 92 3.00 19.44 93 7.50 7.78 94 4.50 12.96 95 4.50 12.96 7.24 -134.60 31.50 96 7.50 7.78 7.32 -60.80 34.20 97 7.50 7.78 7.26 -102.50 33.50 98 4.50 12.96 7.38 -110.30 29.00 99 7.50 7.78 7.16 -85.00 29.30 100 3.00 19.44 6.93 -112.90 37.20 Fixed Bed Anammox Reactor 141 Sample Number Flow Rate (mL/min) HRT (hr) pH ORP Temp 101 3.50 16.67 102 7.50 7.78 7.19 -60.00 29.40 103 7.50 7.78 7.32 -60.80 34.20 104 4.50 12.96 7.38 -110.30 29.00 105 7.50 7.78 106 7.50 7.78 107 7.50 7.78 7.02 -149.10 33.20 108 4.50 12.96 109 4.50 12.96 7.60 -117.30 29.00 110 7.50 7.78 111 7.50 7.78 112 3.00 19.44 113 7.50 7.78 114 3.50 16.67 115 3.00 19.44 7.04 35.50 116 4.50 12.96 117 3.00 19.44 118 4.50 12.96 7.60 -117.30 29.00 119 3.50 16.67 7.80 -78.50 30.60 120 3.00 19.44 121 4.50 12.96 7.60 -117.30 29.00 122 3.00 19.44 123 4.50 12.96 7.49 -142.00 29.00 124 4.50 12.96 125 7.50 7.78 126 4.50 12.96 127 4.50 12.96 128 4.50 12.96 7.49 -142.00 29.00 129 3.00 19.44 130 3.00 19.44 131 3.00 19.44 7.22 -67.20 33.40 132 4.50 12.96 7.49 -142.00 29.00 133 3.00 19.44 134 3.50 16.67 135 7.50 7.78 7.29 -77.00 33.10 136 7.50 7.78 137 7.50 7.78 7.02 -149.10 33.20 138 3.00 19.44 139 7.50 7.78 140 7.50 7.78 141 7.50 7.78 142 7.50 7.78 6.98 -110.90 35.90 143 7.50 7.78 144 7.50 7.78 145 3.00 19.44 146 7.50 7.78 6.73 -143.00 32.70 147 7.50 7.78 6.85 -154.60 32.20 148 7.50 7.78 7.35 -110.90 30.90 Fixed Bed Anammox Reactor 142 Sample Number TOC(mg/L) SOC(mg/L) NH3-N NOx NO3-N NO2-N Corrected NOx 1 18.20 11.30 9.11 2.20 11.31 2 19.90 12.40 9.61 3.03 12.64 3 35.10 35.70 16.70 6.70 10.00 16.70 4 14.10 12.40 9.28 3.35 12.63 5 14.00 14.00 44.60 45.20 15.04 30.70 45.74 6 15.00 15.00 25.30 25.90 15.15 11.30 26.45 7 24.40 19.00 9.65 9.36 19.01 8 20.10 13.30 11.82 1.78 13.60 9 14.40 17.50 11.74 6.05 17.79 10 26.30 14.80 8.81 6.00 14.81 11 18.10 30.90 13.80 10.49 3.32 13.81 12 20.40 13.50 10.49 3.02 13.51 13 21.30 32.90 27.40 9.10 18.30 27.40 14 30.00 35.40 21.28 16.10 37.38 15 22.80 37.10 31.20 6.60 24.60 31.20 16 31.20 36.30 21.83 16.50 38.33 17 24.90 36.20 31.10 9.80 21.30 31.10 18 21.30 11.40 10.65 0.76 11.41 19 30.10 36.00 21.50 16.50 38.00 20 28.90 36.00 21.50 16.50 38.00 21 29.30 35.80 22.16 15.70 37.86 22 20.90 14.50 18.05 0.47 18.53 23 23.40 30.10 28.20 7.80 20.40 28.20 24 20.40 33.80 25.11 8.69 33.80 25 20.60 35.30 26.34 8.96 35.30 26 18.00 14.00 29.40 32.30 6.54 26.00 32.54 27 29.50 36.30 14.33 23.30 37.63 28 27.80 33.40 17.53 17.50 35.03 29 19.70 35.10 26.76 8.34 35.10 30 14.00 12.00 31.40 36.90 19.40 19.30 38.70 31 27.50 37.10 19.74 19.20 38.94 32 30.40 30.60 12.13 19.60 31.73 33 29.20 34.50 18.52 17.70 36.22 34 26.30 40.90 22.71 20.30 43.01 35 2.35 11.20 9.91 1.54 11.45 36 29.10 33.50 17.86 17.30 35.16 37 14.00 14.00 23.80 20.50 10.17 10.70 20.87 38 29.40 36.90 14.88 23.40 38.28 39 15.00 15.00 25.40 26.90 10.37 16.90 27.27 40 30.60 31.10 12.90 19.40 32.30 41 24.20 39.00 26.80 6.70 20.10 26.80 42 21.60 26.70 14.33 13.70 28.03 43 20.20 14.30 17.90 0.39 18.29 44 13.00 12.00 29.30 37.90 19.96 19.80 39.76 45 20.20 27.70 20.80 7.00 13.80 20.80 46 13.00 21.70 26.40 14.44 13.30 27.74 47 16.00 23.50 23.80 8.10 15.70 23.80 48 15.00 15.00 17.10 21.10 9.50 11.60 21.10 49 20.70 26.10 14.00 13.40 27.40 50 13.00 20.40 26.20 14.44 13.10 27.54 Up-Flow Fixd-Bed Anammox Reactor Effluent 143 Sample Number TOC(mg/L) SOC(mg/L) NH3-N NOx NO3-N NO2-N Corrected NOx 1 20.40 45.30 32.20 16.00 48.20 2 34.60 52.70 19.42 33.90 53.32 3 14.00 12.00 23.00 37.10 12.20 24.90 37.10 4 26.20 40.20 22.60 19.70 42.30 5 21.00 18.00 29.20 36.90 18.20 18.90 37.10 6 21.10 46.30 31.98 17.20 49.18 7 20.50 44.50 30.55 16.70 47.25 8 16.00 12.00 16.00 23.30 11.30 12.00 23.30 9 30.40 47.90 24.09 26.80 50.89 10 30.30 47.50 30.58 17.90 48.48 11 30.00 50.10 25.91 27.40 53.31 12 23.00 44.80 27.28 20.90 48.18 13 23.20 47.80 37.21 15.20 52.41 14 13.90 12.30 30.60 25.09 8.09 33.18 15 30.90 55.80 28.77 30.60 59.37 16 16.50 25.60 21.00 9.28 30.28 69 17.40 25.50 21.47 8.82 30.29 70 22.00 14.00 17.10 23.45 10.44 13.30 23.74 71 17.50 13.00 11.70 34.60 21.70 12.90 34.60 72 23.20 45.40 27.85 21.00 48.85 73 23.90 44.50 35.05 13.80 48.85 74 16.30 25.90 21.02 9.57 30.59 75 5.50 29.80 24.76 5.04 29.80 76 29.00 55.60 23.55 32.80 56.35 77 21.00 18.00 28.60 37.70 18.81 19.10 37.91 78 17.00 13.00 16.80 22.90 13.44 9.84 23.28 79 28.40 46.30 29.75 17.50 47.25 80 33.10 55.40 16.84 39.10 55.94 81 20.40 49.70 30.14 23.30 53.44 82 23.50 46.20 36.07 14.60 50.67 83 22.20 57.10 30.66 29.20 59.86 84 25.80 49.00 25.68 26.50 52.18 85 5.28 29.60 24.50 5.10 29.60 86 13.50 13.20 11.60 33.40 26.64 9.50 36.14 87 34.30 12.60 19.70 46.30 21.60 24.70 46.30 88 14.80 27.70 52.90 26.09 29.50 55.59 89 32.60 57.70 21.38 37.00 58.38 90 13.70 13.40 31.30 24.76 9.09 33.85 91 20.00 12.10 21.30 46.00 21.80 24.20 46.00 92 15.90 26.90 52.40 25.53 29.50 55.03 93 23.00 16.00 30.00 37.70 18.81 19.10 37.91 94 23.40 55.70 29.34 29.00 58.34 95 40.30 11.80 23.50 46.30 20.90 25.40 46.30 96 20.00 14.00 16.90 27.20 14.26 13.10 27.36 97 14.00 15.30 22.90 13.44 9.84 23.28 98 24.30 46.00 24.89 24.20 49.09 99 16.00 13.00 13.00 27.50 16.20 11.30 27.50 100 17.80 14.20 27.60 51.50 24.41 29.60 54.01 Up-Flow Fixd-Bed Anammox Reactor Effluent 144 Sample Number TOC(mg/L) SOC(mg/L) NH3-N NOx NO3-N NO2-N Corrected NOx 101 5.03 30.30 25.22 5.08 30.30 102 13.00 12.00 13.00 23.50 14.41 9.09 23.50 103 18? 16.40 27.10 14.26 13.00 27.26 104 23.50 50.00 26.03 27.20 53.23 105 23.00 16.00 29.70 38.60 13.14 25.60 38.74 106 32.20 56.10 16.94 39.70 56.64 107 13.80 23.60 50.60 19.08 31.90 50.98 108 15.30 14.80 13.00 34.50 21.90 12.60 34.50 109 17.30 45.50 22.95 25.40 48.35 110 29.90 55.90 24.17 32.50 56.67 111 19.00 13.00 14.20 22.60 13.63 9.12 22.75 112 11.70 1.32 19.70 19.51 0.19 19.70 113 25.70 48.90 19.32 30.20 49.52 114 26.30 11.70 8.70 35.10 23.00 12.10 35.10 115 17.50 14.80 1.74 19.30 19.01 0.29 19.30 116 16.20 13.50 12.10 34.60 21.90 12.70 34.60 117 17.50 14.70 18.20 27.10 26.29 0.81 27.10 118 18.50 46.00 23.40 25.50 48.90 119 26.00 14.70 7.93 35.00 23.00 12.00 35.00 120 26.30 15.30 15.30 27.00 22.59 4.41 27.00 121 18.00 45.20 23.17 24.90 48.07 122 22.50 53.30 28.50 24.80 53.30 123 15.40 38.70 15.00 23.70 38.70 124 16.50 11.90 11.20 32.90 21.20 11.70 32.90 125 24.10 46.60 18.18 29.00 47.18 126 17.10 11.90 11.40 32.80 21.80 11.00 32.80 127 15.80 11.70 12.20 32.90 22.10 10.80 32.90 128 15.00 38.80 14.90 23.90 38.80 129 16.40 11.70 17.30 27.20 26.42 0.79 27.20 130 1.28 18.90 18.62 0.28 18.90 131 15.70 26.80 22.61 4.19 26.80 132 15.90 39.30 16.70 22.60 39.30 133 26.00 11.70 15.80 26.80 22.60 4.20 26.80 134 15.30 7.47 32.20 20.60 11.60 32.20 135 12.00 6.76 6.09 6.16 6.09 136 22.20 57.90 29.70 28.20 57.90 137 22.30 58.20 30.00 28.20 58.20 138 16.30 27.00 26.01 0.99 27.00 139 22.10 58.10 26.40 31.70 58.10 140 21.40 54.30 26.60 27.70 54.30 141 28.80 60.50 26.80 33.70 60.50 142 20.90 122.00 93.40 28.60 122.00 143 20.70 58.20 29.70 28.50 58.20 144 8.53 47.60 44.19 3.41 47.60 145 17.80 14.20 23.00 50.90 28.10 22.80 50.90 146 27.30 59.10 26.40 32.70 59.10 147 22.10 59.00 26.80 32.20 59.00 148 7.51 39.70 36.16 3.54 39.70 Up-Flow Fixd-Bed Anammox Reactor Effluent 145 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 1 71.41 70.11 93.45 0.74 0.44 0.24 15.16 8.78 6.46 2 58.16 52.28 87.73 0.54 0.29 0.17 8.96 4.35 4.32 3 53.67 45.08 74.81 0.81 0.47 0.29 12.49 6.03 6.11 4 70.16 71.91 89.37 0.58 0.33 0.20 11.53 6.68 5.21 5 1.65 0.93 0.59 0.00 0.00 0.00 6 64.59 67.27 78.31 1.46 0.78 0.53 26.90 14.98 11.75 7 60.00 56.04 76.72 0.78 0.40 0.29 13.39 6.40 6.34 8 63.42 57.14 94.91 0.53 0.27 0.20 9.53 4.41 5.47 9 63.54 67.71 82.05 0.50 0.26 0.19 9.15 4.97 4.55 10 58.23 47.40 84.50 0.99 0.50 0.39 16.50 6.83 9.42 11 56.30 38.81 91.78 1.03 0.51 0.41 16.59 5.64 10.68 12 54.68 45.89 90.16 0.54 0.27 0.22 8.41 3.56 5.69 13 36.99 33.80 54.93 1.38 0.72 0.58 14.56 6.91 9.17 14 1.02 0.47 0.39 15 1.44 0.72 0.61 16 1.06 0.47 0.41 17 1.47 0.73 0.65 18 52.05 40.17 97.57 0.49 0.26 0.23 7.30 2.94 6.30 19 1.03 0.46 0.41 20 33.57 32.63 57.47 1.06 0.46 0.42 10.12 4.32 6.88 21 30.60 29.90 58.58 1.01 0.45 0.41 8.86 3.86 6.85 22 63.32 51.84 98.80 0.32 0.09 0.17 5.78 1.34 4.82 23 39.96 37.29 53.74 1.75 0.86 0.79 19.95 9.21 12.19 24 41.15 47.01 75.66 0.32 0.09 0.15 3.76 1.18 3.33 25 37.61 44.17 73.88 0.32 0.09 0.15 3.40 1.12 3.13 26 47.76 45.56 48.72 1.02 0.47 0.44 13.92 6.07 6.10 27 1.08 0.47 0.44 28 37.99 40.34 60.05 1.07 0.50 0.47 11.57 5.80 8.12 29 41.76 47.75 76.51 0.33 0.09 0.15 3.92 1.16 3.35 30 31.01 28.31 53.27 1.07 0.47 0.45 9.47 3.83 6.79 31 33.95 36.05 53.06 1.06 0.46 0.44 10.24 4.78 6.70 32 36.06 32.89 54.73 1.03 0.49 0.47 10.61 4.60 7.31 33 35.85 36.11 59.59 1.07 0.49 0.47 10.99 5.09 8.05 34 0.98 0.42 0.40 35 82.63 93.30 95.47 0.34 0.15 0.15 7.95 4.04 4.01 36 34.79 34.75 60.23 1.04 0.48 0.47 10.31 4.78 8.08 37 58.68 51.23 77.57 0.93 0.42 0.41 15.53 6.17 9.13 38 34.94 35.24 47.65 1.10 0.49 0.48 10.99 4.94 6.57 39 52.97 49.90 66.33 1.12 0.51 0.51 16.96 7.29 9.59 40 35.53 31.54 56.31 1.03 0.48 0.48 10.49 4.35 7.71 41 40.13 24.12 60.67 0.79 0.37 0.37 9.07 2.55 6.38 42 38.31 37.21 59.94 0.85 0.37 0.37 9.26 3.95 6.33 43 62.25 49.12 99.01 0.31 0.09 0.17 5.52 1.22 4.86 44 1.04 0.45 0.45 45 56.89 45.58 73.36 0.81 0.37 0.37 13.17 4.77 7.82 46 0.84 0.37 0.37 47 45.44 40.81 61.43 0.75 0.34 0.35 9.73 4.00 6.17 48 68.66 68.22 79.02 1.05 0.46 0.48 20.66 9.06 10.79 49 39.06 37.27 60.82 0.83 0.36 0.37 9.26 3.80 6.42 50 39.64 37.61 62.78 0.83 0.35 0.38 9.44 3.80 6.82 Fixed Bed Anammox System performance 146 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 51 1.06 0.45 0.49 52 30.26 22.59 49.35 1.09 0.46 0.50 9.41 2.96 7.07 53 39.78 50.72 64.68 0.57 0.13 0.29 6.49 1.92 5.42 54 1.01 0.37 0.50 55 44.20 52.58 54.56 1.16 0.52 0.59 14.69 7.87 9.23 56 0.92 0.35 0.40 57 48.52 50.00 71.75 1.39 0.63 0.72 19.22 9.01 14.81 58 35.87 45.62 61.69 0.57 0.14 0.29 5.80 1.78 5.13 59 39.08 48.88 64.09 0.56 0.13 0.30 6.30 1.86 5.52 60 62.68 65.88 78.57 1.14 0.51 0.60 20.37 9.53 13.58 61 34.26 33.91 51.80 0.67 0.20 0.36 6.56 1.91 5.33 62 0.98 0.33 0.52 63 34.45 36.03 51.85 0.68 0.19 0.37 6.72 2.00 5.46 64 31.72 37.67 53.76 0.55 0.15 0.29 5.02 1.60 4.50 65 28.50 37.13 66.37 0.55 0.15 0.29 4.52 1.59 5.55 66 57.61 67.89 82.86 0.32 0.05 0.20 5.35 1.03 4.83 67 32.05 35.76 48.83 0.72 0.20 0.39 6.55 2.05 5.41 68 55.59 56.12 80.30 0.32 0.07 0.20 5.06 1.14 4.67 69 54.56 52.46 80.99 0.32 0.08 0.20 5.06 1.13 4.64 70 64.32 64.89 78.63 1.23 0.53 0.67 22.56 9.75 15.10 71 45.72 62.38 67.99 0.43 0.08 0.26 5.58 1.35 5.07 72 32.61 36.61 55.79 0.57 0.15 0.31 5.34 1.57 4.91 73 32.81 34.70 70.95 0.58 0.15 0.31 5.41 1.54 6.24 74 54.91 55.34 79.81 0.32 0.07 0.20 4.98 1.11 4.67 75 57.32 82.59 87.77 0.29 0.03 0.21 4.67 0.65 5.21 76 1.00 0.31 0.54 77 44.98 44.14 71.49 1.30 0.55 0.72 16.72 6.97 14.78 78 64.60 64.41 84.20 1.21 0.51 0.67 22.36 9.38 16.17 79 0.95 0.31 0.52 80 1.05 0.36 0.61 81 29.83 42.37 50.74 0.55 0.13 0.31 4.69 1.60 4.44 82 30.23 33.62 69.13 0.57 0.15 0.31 4.93 1.46 6.05 83 28.50 48.97 49.83 0.63 0.14 0.38 5.13 2.01 5.37 84 0.55 0.17 0.29 85 60.14 83.80 88.44 0.30 0.03 0.22 5.21 0.64 5.62 86 53.03 66.18 79.53 0.32 0.05 0.20 4.78 0.95 4.55 87 36.54 46.32 50.30 0.56 0.13 0.32 5.89 1.69 4.63 88 33.17 41.19 53.76 0.44 0.12 0.28 4.14 1.41 4.23 89 1.08 0.35 0.57 90 53.87 61.16 80.58 0.33 0.06 0.20 5.04 1.01 4.65 91 35.23 41.96 51.41 0.57 0.14 0.32 5.77 1.65 4.74 92 35.53 44.42 55.97 0.44 0.12 0.29 4.45 1.47 4.63 93 42.72 37.63 71.32 1.28 0.52 0.72 15.58 5.59 14.66 94 32.22 44.15 50.17 0.64 0.15 0.38 5.86 1.91 5.41 95 32.50 34.36 49.60 0.59 0.15 0.33 5.48 1.49 4.63 96 57.56 59.18 77.87 1.12 0.45 0.64 18.45 7.56 14.23 97 63.15 63.74 83.70 1.12 0.46 0.65 20.20 8.30 15.59 98 30.33 29.57 51.70 0.59 0.16 0.32 5.09 1.33 4.80 99 58.59 66.49 79.96 1.06 0.22 0.37 17.68 4.25 8.35 100 33.92 37.98 54.67 0.44 0.12 0.28 4.30 1.29 4.41 Fixed Bed Anammox System performance 147 Sample Number Total N removal % NH4-N removal % NO2-N removal % Total N Loading (g/d) NH4-N Loading (g/d) NO2-N Loading (g/d) Volumetric removal g/L.d (Total IN) Volumetric removal g/L.d (NH4-N) Volumetric removal g/L.d (NO2-N) 101 58.92 83.18 88.43 0.31 0.03 0.22 5.19 0.60 5.59 102 62.49 66.06 83.88 1.05 0.15 0.22 18.76 2.84 5.30 103 58.37 60.39 78.72 1.13 0.45 0.66 18.82 7.71 14.84 104 24.77 29.43 44.72 0.57 0.15 0.32 4.03 1.28 4.07 105 40.71 34.15 61.68 1.24 0.49 0.72 14.47 4.75 12.71 106 1.05 0.35 0.63 107 26.68 36.39 42.21 0.95 0.25 0.60 7.22 2.65 7.19 108 44.18 55.48 71.17 0.45 0.08 0.28 5.64 1.34 5.76 109 30.68 43.09 44.18 0.50 0.11 0.29 4.40 1.38 3.72 110 1.02 0.32 0.64 111 63.78 64.50 84.95 1.10 0.43 0.65 20.00 7.96 15.89 112 76.00 95.81 99.59 0.25 0.01 0.21 5.39 0.16 5.88 113 27.99 30.91 46.83 0.99 0.28 0.61 7.96 2.45 8.21 114 49.36 71.38 73.98 0.33 0.04 0.23 4.61 0.89 4.95 115 76.20 94.56 99.41 0.25 0.01 0.21 5.47 0.20 6.02 116 45.70 59.26 72.21 0.44 0.08 0.30 5.79 1.33 6.11 117 42.51 41.48 98.34 0.28 0.08 0.21 3.46 0.93 5.89 118 28.09 36.86 44.57 0.51 0.12 0.30 4.10 1.26 3.80 119 49.01 71.68 73.21 0.32 0.04 0.23 4.53 0.82 4.72 120 45.70 47.06 90.48 0.28 0.07 0.20 3.63 0.89 5.17 121 29.39 37.06 45.99 0.51 0.12 0.30 4.29 1.24 3.93 122 0.36 0.10 0.25 123 40.61 50.48 53.44 0.49 0.10 0.33 5.67 1.44 5.04 124 47.75 58.97 74.00 0.44 0.07 0.29 6.04 1.22 6.17 125 31.09 31.53 50.09 0.99 0.26 0.63 8.78 2.35 8.98 126 47.63 59.57 76.45 0.44 0.07 0.30 5.96 1.26 6.61 127 46.56 56.58 76.87 0.44 0.08 0.30 5.91 1.28 6.65 128 40.68 51.77 53.86 0.48 0.10 0.34 5.62 1.44 5.17 129 42.36 42.33 98.45 0.28 0.07 0.22 3.37 0.90 6.16 130 77.33 95.73 99.45 0.26 0.01 0.22 5.75 0.15 6.22 131 44.44 44.91 91.36 0.28 0.07 0.21 3.49 0.87 5.47 132 38.46 45.73 55.07 0.49 0.10 0.33 5.43 1.35 5.13 133 45.31 41.91 91.01 0.29 0.07 0.20 3.72 0.82 5.25 134 53.16 72.84 75.53 0.33 0.04 0.24 4.95 0.78 5.16 135 87.49 81.27 90.13 1.11 0.14 0.24 27.73 3.22 6.15 136 1.09 0.33 0.57 137 1.08 0.32 0.57 138 44.06 43.99 98.06 0.28 0.07 0.22 3.51 0.88 6.20 139 22.18 39.04 1.01 0.31 0.56 1.94 6.26 140 25.20 27.46 50.18 1.09 0.32 0.60 7.87 2.50 8.61 141 1.07 0.31 0.59 142 1.66 0.32 0.62 143 1.06 0.30 0.57 144 59.44 70.99 94.03 1.49 0.32 0.62 25.39 6.44 16.57 145 21.50 60.49 0.36 0.10 0.25 0.61 4.31 146 28.72 39.67 1.04 0.29 0.59 2.42 6.63 147 19.64 41.13 1.06 0.30 0.59 1.67 6.94 148 63.29 73.74 93.82 1.39 0.31 0.62 25.11 6.51 16.59 Fixed Bed Anammox System performance "@en . "Thesis/Dissertation"@en . "2011-11"@en . "10.14288/1.0063190"@en . "eng"@en . "Civil Engineering"@en . "Vancouver : University of British Columbia Library"@en . "University of British Columbia"@en . "Attribution-NonCommercial-NoDerivatives 4.0 International"@en . "http://creativecommons.org/licenses/by-nc-nd/4.0/"@en . "Graduate"@en . "Nitrogen removal from wastewater through partial nitrification/ Anammox process"@en . "Text"@en . "http://hdl.handle.net/2429/36921"@en .