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Parallel treatment of a minimum effluent TMP-newsprint whitewater by aerobic membrane biological treatment.. Ragona, Christina S. F. 1998

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PARALLEL TREATMENT OF A MINIMUM EFFLUENT TMPNEWSPRTNT WHITEWATER BY AEROBIC MEMBRANE BIOLOGICAL TREATMENT AND ULTRAFILTRATION AT 55°C  by CHRISTINA S. F. RAGONA B.Sc.E. (Hons.), Queen's University, Kingston, Ontario, 1994 B.A., Queen's University, Kingston, Ontario, 1995  A THESIS SUBMITTED IN PARTIAL FULFILLMENT OF THE REQUIREMENTS FOR THE DEGREE OF  MASTER OF APPLIED SCIENCE in THE FACULTY OF GRADUATE STUDIES (Department of Civil Engineering)  We accept this thesis as conforming to the required standard  THE UNIVERSITY OF BRITISH COLUMBIA April, 1998 © Christina Sarah Francesca Ragona, 1998  In  presenting this  degree at the  thesis  in  partial  fulfilment  University of British Columbia,  of  the  requirements for an advanced  I agree that the Library shall make it  freely available for reference and study. I further agree that  permission for extensive  copying of this thesis for scholarly purposes may be granted by the department  or  by  his  or  her  representatives.  It  is  understood  that  head of my copying  or  publication of this thesis for financial gain shall not be allowed without my written permission.  Department of  Q y((  The University of British Columbia Vancouver, Canada  DE-6 (2/88)  ABSTRACT A lab scale membrane biological reactor (MBR) consisting of an aerobic biological reactor coupled to a lab scale ceramic ultrafiltration membrane (pore size 500 Angstroms) was operated in parallel with an ultrafiltration treatment system consisting of a non-inoculated mixing tank and the identical ultrafiltration membrane to treat a simulated minimum effluent TMP-newsprint Whitewater at 55°C.  The MBR system was operated at hydraulic residence times (HRTs) of 1 day, 0.5 days and 0.33 days with a constant solids retention time (SRT) of 20 days, corresponding to water recovery fractions of 0.95, 0.975, and 0.983, while the UF system was operated at water recovery fractions of 0.9, 0.95, 0.983. Thefilterswere operated at a flow through velocity of 4 m/s and a transmembrane pressure of 138 kPa (20 psi).  The MBR performed optimally at a water recovery fraction of 0.983, achieving removal of total and dissolved solids of 29% and 22%, and total and dissolved chemical oxygen demand of 48%) and 34%. Removal of resin and fatty acids were 66% and 99% respectively, cationic demand removal was 48% and removal of UV-Lignin, 8%. The maximum flux through the filter was 162 L7(m »hr) and the time for a 20% loss of flux was 110 hours. 2  The UF system performed best at a water recovery fraction of 0.95, achieving lower removal of total solids (23%), dissolved solids (18%), total COD (31%), dissolved COD (4%) than the MBR.  Removal of resin and fatty acids were 95% and 98% respectively, and removal of  cationic demand was 74%. UV-Lignin was not removed at all by the UF system. Maximum flux through the filter was 162 L/(m »hr) and the time for a 20% loss of flux was 170 hours. 2  ii  The reduced fouling potential and improved removal of certain contaminants coupled with the lower cost of operation and fewer operational upsets would suggest the ultrafiltration treatment system operated at a water recovery fraction of 0.95 (or volume reduction factor of 20) has higher potential for treating minimum effluent TMP-newsprint Whitewater at 55°C than aerobic membrane biological treatment.  iii  T A B L E OF CONTENTS ABSTRACT  ii  TABLE OF CONTENTS  iv  LIST OF TABLES  vii  LIST OF FIGURES  viii  LIST OF ABBREVIATIONS AND ACRONYMS ACKNOWLEDGMENTS  xi xiii  1. INTRODUCTION  1  1.1 Motivation for Research  1  1.2 Thesis Organization  2  2. BACKGROUND AND LITERATURE REVIEW  4  2.1 Systems Closure and Minimum Impact Technology in the Pulp and Paper Industry  4  2.2 Closure of Integrated TMP-Newsprint Mills 2.2.1 Integrated TMP-Newsprint Whitewater System 2.2.2 Minimum Effluent TMP-Newsprint Whitewater  10 10 11  2.3 Implications of TMP-Newsprint Closure 2.3.1 Whitewater Characteristics 2.3.2 Corrosion 2.3.3 Product Quality  14 14 23 25  2.4 Closure Alternatives 2.4.1 Fresh Water Use Minimization 2.4.2 Pulp Washing 2.4.3 Mechanical Vapor Recompression (MVR) Evaporation 2.4.4 Physical Chemical Treatment 2.4.5 Aerobic Biological Treatment 2.4.6 Recycle of Secondary Effluent 2.4.7 Anaerobic Biological Treatment 2.4.8 Ultrafiltration 2.4.9 Membrane Bioreactor (MBR)  26 26 29 30 30 32 34 35 38 44  2.5 Technical and-Economic Assessments of Closure Options  51  2.6 Summary and Conclusions  54  iv  3. OBJECTIVES FOR THE RESEARCH  57  4. EXPERIMENTAL METHODS AND APPARATUS  61  4.1 Experimental Apparatus  61  4.1.1 Membrane Biological Reactor System 4.1.2 Ultrafiltration System 4.1.3 Membrane Cleaning System  61 66 67  4.2 Materials 4.2.1 Wastewater Feed 4.2.2 Nutrient Solution 4.2.3 Biomass  68 68 69 69  4.3 Experimental Methods 4.3.1 Biomass Acclimation 4.3.2 Membrane Cleaning 4.3.3 Sampling and Sample Preparation 4.3.4 Quality Assurance/ Quality Control (QA/QC) 4.3.5 Analytical Methods and Equipment 4.3.6 pH 4.3.7 Temperature 4.3.8 Dissolved Oxygen 4.3.9 Permeate Flow Rate 4.3.10 Statistical Analyses  70 70 70 71 72 72 80  4.4 Experimental Design and Operating Parameters 4.4.1 Water Recovery Fraction 4.4.2 Temperature 4.4.3 Transmembrane Pressure and Velocity 4.4.4 Nutrients  81 81 85 86 86  5. RESULTS AND DISCUSSION  87  5.1 Whitewater Characteristics  87  5.2 System Characterization 5.2.1 Initial Membrane Flux  88 88  5.3 Comparison of MBR and UF System Performance 5.3.1 Operating Parameters 5.3.2 Contaminant Removal 5.3.3 Permeate Flux 5.3.4 Characteristics of Retentate v  8  0  80 80 80  89 89 91 110 115  5.3.5 Solids Mass Balance  118  5.4 Biological Activity in the M B R 5.4.1 M L V S S 5.4.2 Food to Microorganism Ratio  121 121 123  5.5 Effect of V R F on Operation of the UF System  125  5.6 Comparison to Other Research  126  6. CONCLUSIONS  129  6.1 Comparison : M B R and U F Treatment of Minimum Effluent Whitewater  129  6.2 Conclusions: M B R Biokinetics  131  6.3 Conclusions: Operation of a U F at Varying VRF  131  6.4 Most Viable Treatment Option  132  7. REFERENCES  134  vi  LIST OF TABLES Table 2-1: Composition of TMP-Newsprint Whitewater  12  Table 2-2: Composition of Manufactured TMP-Newsprint Whitewater  13  Table 2-3: TMP Whitewater from Howe Sound Pulp and Paper  14  Table 2-4: Comparison of UF studies on Pulp and Paper Effluents  42  Table 2-5: continuing (Table 2-4)  43  Table 2-6: Comparison of MBR studies on Pulp and Paper Effluents  48  Table 4-1: Specifications and Operating limits of the Membralox 1T1-70 Ultrafiltration Membrane (Membralox, 1996)  65  Table 4-2: Analysis of Solids  73  Table 4-3: Temperature Program for Gas Chromatographic Analysis of Samples for Resin and Fatty Acids 76 Table 4-4: Resin and Fatty Acids Quantified in this Study  76  Table 4-5: Experimental design and operational parameters  84  Table 5-1: Composition of Synthetic Whitewater  88  Table 5-2: Characteristics of the MBR Retentate (pt. I)  116  Table 5-3: Characteristics of the MBR Retentate (pt. II)  116  Table 5-4: Characteristics of the UF Retentate (pt. I)  117  Table 5-5: Characteristics of the UF Retentate (pt. II)  117  Table 5-6: F/M Ratios  125  Table 5-7: Comparison of Optimal Operating Conditions  128  vii  LIST OF FIGURES  Figure 2-1: Configuration of a Linear Cationic Polymer (taken from Pietschker (1996))  22  Figure 2-2: Scanning Electron Micrograph of Alumina Ultrafiltration Membrane (Hseih, 1988)  41  Figure 4-1: Aerobic Membrane Biological Reactor  62  Figure 4-2: IT-70 Alpha Alumina Membralox Membrane (Membralox, 1996)  64  Figure 4-3: Cleaning System  67  Figure 4-4: Experimental Program to investigate the application of an aerobic membrane biological reactor to treat low water use integrated TMP-newsprint Whitewater  83  Figure 4-5: Experimental Program to investigate the application of an ultrafiltration system to treat low water use integrated TMP-newsprint Whitewater 84 Figure 5-1: Transmembrane Pressure in the Membrane Bioreactor System  89  Figure 5-2: Transmembrane Pressure in the Ultrafiltration System  90  Figure 5-3: Operating Temperature in the Membrane Bioreactor System  90  Figure 5-4: Operating Temperature in the Ultrafiltration System  91  Figure 5-5 :Solids Concentration in the Membrane Bioreactor System as a Function of Time92 Figure 5-6: Solids Concentration in the Ultrafiltration System as a function of Time  92  Figure 5-7: Total Solids Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 93 Figure 5-8: Total Solids Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  94  Figure 5-9: Dissolved Solids Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 94 Figure 5-10: Dissolved Solids Removal in the Ultrafiltration System as a Function of Water Recovery Fraction 95 Figure 5-11: Chemical Oxygen Demand (COD) Concentration in the Membrane Bioreactor System as a Function of Time 95  Vlll  Figure 5-12: Chemical Oxygen Demand (COD) Concentrations in the Ultrafiltration System as a Function of Time 96 Figure 5-13: Total Chemical Oxygen Demand (TCOD) Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 97 Figure 5-14: Total Chemical Oxygen Demand (TCOD) Removal in the Ultrafiltration System as a Function of Water recovery Fraction 98 Figure 5-15: Dissolved Chemical Oxygen Demand (DCOD) Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction  99  Figure 5-16: Dissolved Chemical Oxygen Demand (DCOD) Removal in the Ultrafiltration System as a Function of Water Recovery Fraction 99 Figure 5-17: Resin Acid Concentration  100  Figure 5-18: Fatty Acid Concentration  100  Figure 5-19: Resin Acid Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 101 Figure 5-20: Resin Acid Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  102  Figure 5-21: Fatty Acid Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 103 Figure 5-22: Fatty Acid Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  103  Figure 5-23: Cationic Demand Concentration in the Membrane bioreactor System as a Function of Time  105  Figure 5-24: Cationic Demand Concentrations in the Ultrafiltration System as a Function of Time 106 Figure 5-25: Cationic Demand Removal for the Membrane Bioreactor System as a Function of Water Recovery Fraction 106 Figure 5-26: Cationic Demand in the Ultrafiltration System as a Function of Water Recovery Fraction 107 Figure 5-27: UV-Lignin Concentration in the Membrane Bioreactor System as a Function of Time 108 Figure 5-28: UV-Lignin Concentration in the Ultrafiltration System as a Function of Time 108  IX  Figure 5-29: UV-lignin Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 109 Figure 5-30: UV-lignin Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  109  Figure 5-31: Permeate Flux in the Membrane Bioreactor and the Ultrafiltration System over the Experimental Period 110 Figure 5-32: Maximum Flux  112  Figure 5-33: Time for a 20% Reduction in Permeate Flux in the Membrane Bioreactor and Ultrafiltration Systems as a Function of Water Recovery Fraction 114 Figure 5-34: Cumulative Solids Mass Flows: MBR, as a Function of Time  119  Figure 5-35: Cumulative Solids Mass Flows: UF, as a Function of Time  120  Figure 5-36: MLVSS and MLVSS* Concentrations in the Membrane Bioreactor as a Function of HRT  122  Figure 5-37: MLVSS * Concentrations in the MBR as a Function of Time  122  Figure 5-38: Determination of BCOD (mg/L) in the Membrane Bioreactor  124  LIST OF ABBREVIATIONS AND ACRONYMS adt  Air-dried tonne  ASB  Aerated stabilization basin  AST  Activated Sludge Treatment  AT AD  Autothermal aerobic digester  BCTMP  Bleached chemi-thermomechanical pulp  BCOD  Biodegradable Chemical Oxygen Demand  BOD  Biochemical oxygen demand  BOD  5  Biological oxygen demand (5 day)  CD  Cationic demand  CF  Concentration factor  COD  Chemical oxygen demand  CTMP  Chemi-thermomechanical pulp  d  Day(s)  DCOD  Dissolved chemical oxygen demand  DCS  Dissolved and colloidal substances  DDPM  1,5-dimethyl 1-1,5 diazaundecamethylene polymethylobromide  DHA  Dehydroabietic acid  DO  Dissolved oxygen  F/M  Food to microorganism  FA  Fatty acids  HRT  Hydraulic retention time  MBR  Membrane biological reactor  MF  Microfiltration  ML  Mixed liquor  MLSS  Mixed liquor suspended solids  MLTDS  Mixed liquor total dissolved solids  MLVSS  Mixed liquor volatile suspended solids  MST  Membrane sewage treatment  MVR  Mechanical vapour recompression  MW  Molecular weight  MWCO  Molecular weight cutoff  N  Nitrogen  NF  Nanofiltration  OUR  Oxygen uptake rate  P  Phosphorus  P  Pressure  PAPRICAN  Pulp and Paper Research Institute of Canada  psi  Pounds per square inch xi  PVSAK  Polyvinyl sulphuric acid potassium salt (K)  RA  Resin acids  RFA  Resin and fatty acids  rpm  Revolutions per minute  So  Influent COD or BOD concentration  SBR  Sequencing batch reactor  SOUR  Specific oxygen uptake rate  SRT  Solids retention time  T  Temperature  TBO  Toluidine blue O  TCOD  Total chemical oxygen demand  TDCS  Total dissolved and colloidal solids  TMP  Thermomechanical pulp  TS  Total solids  TSS  Total suspended solids  UASB  Upflow anaerobic sludge blanket  UBC  University of British Columbia  UF  Ultrafiltration  UV  Ultraviolet  VDS  Volatile dissolved solids  VFA  Volatile Fatty Acids  VRF  Volume reduction factor  VS  Volatile solids  VSS  Volatile suspended solids  Y  Water recovery fraction  xii  ACKNOWLEDGMENTS The research towards and writing of this thesis would not have been possible without the support, guidance and good humor of many individuals whose contribution I would like to recognize.  To begin, I would like to thank my supervisor, Dr. Eric R. Hall for his ideas, support and review of this thesis project.  Secondly, I would like to thank all the people who assisted me with beginning this project and the many more individuals who lived with the trials and tribulations of life in the lab. Dave Francis, Dave Reside and my fellow civil engineer, Olivier Tardif for their many ideas to begin the research and provide insight along the way. Rita Penco, the librarian at the Pulp and Paper Center, for her assistance with the literature research. Peter Taylor for his help in building and modifying laboratory equipment.  Alan Werker, Stephanie Ebelt and Paula  Parkinson, all of whom spent endless hours helping me with equipment operations and analysis of samples, Pierre Berube who was a wonderful mentor and friend, and Sue Sim, Bruce M°Lean, Samantha Fothergill, Mary Campbell and Carlos Blanco - all of whom escorted me to the mill and helped maneuver many heavy buckets of effluent.  Finally, I would like to thank Robert Campbell for many hours of mopping the floor, good ideas, support, encouragement and camaraderie.  This research was funded by the Council of Forest Industries of British Columbia (COFI), through the NSERC/COFI Industrial Chair in Forest Products waste Management, and by the University of British Columbia (UBC).  xiii  1. INTRODUCTION  1.1 Motivation for Research Economic and environmental considerations in the pulp and paper industry have led to interest in and research into the minimization of fresh water use and progressive systems closure. Reduction offreshwater input to a mill system would incorporate such strategies such as pulp washing and countercurrent water recycling to maximize the degree of water reuse within a mill. With the reduction offreshwater into pulp and paper processing, however, will come an increase in the concentration of dissolved and colloidal contaminants in both the pulp and water streams, as well as an increase in operating temperatures. The increase in contaminant concentrations may negatively affect mill operation and paper quality.  One strategy to  minimize some of the problems associated with a high degree of closure and water reuse in a pulp and paper mill is the insertion of a treatment step (or "kidney") into the water recirculation system, for purging the water stream of such contaminants. The reduction of contaminants in the water stream will result in decreased contamination of the pulp stream and higher newsprint quality.  Thermo-mechanical pulping (TMP)-newsprint operations have historically used large volumes of water (as much as 200 m /adt) in the pulping and paper forming processes to purge the 3  system of excess heat and contaminants. Newer mills use less water, in the range of 10-150 m /adt. With effluent flows in excess of 10 nvVadt, "end of pipe" secondary (biological) 3  treatment and disposal to the environment is the only economically viable option for liquid waste management. As TMP-newsprint operations use water reduction strategies to bring  1  fresh water excess flows into the range of 2-5 m /adt, other treatment options become 3  economically viable (Wearing, 1992, 1993).  This thesis project was initiated as part of a long term examination of possible treatment options for the Whitewater derived from a low water use (2-5 m /adt) integrated 3  thermomechanical (TMP) newsprint mill.  Treatment options investigated to date include:  ultrafiltration of Whitewater at 10-50 °C using plate and frame filters with molecular weight cutoffs (MWCOs) of 10 and 100 kDaltons (Elefsiniotis, 1994); biological treatment of Whitewater using a sequencing batch reactor (SBR) in the range of 20-50 °C, and a retention time of 2 days (Johnson, 1995); ultrafiltration of SBR effluent with a plate and frame filter with MWCOs of 10 and 100 kDaltons in the range of 20-40 °C (Elefsiniotis et al, 1995); and aerobic membrane biological treatment of Whitewater at temperatures of 40-55 °C, and HRTs of 0.7-2.8 days (Tardif, 1996). This thesis focuses on a direct comparison of ultrafiltration (UF) and aerobic membrane bioreactor (MBR) treatment for the removal of dissolved and colloidal contaminants from a simulated minimum effluent TMP-newsprint Whitewater. A , comparison of these treatment systems (including those examined in this thesis) is presented in section 5.6.  1.2 Thesis Organization This thesis is divided into six chapters. The first three chapters introduce the background information and the context for this research: an introduction; a background literature review and a discussion of the motivation for this particular research.  Chapter 4 describes the  methods and materials used in this research, and Chapter 5 presents the results and a  2  discussion of them. Chapter 6 summarizes some conclusions from this research and the entire research project.  3  2. BACKGROUND AND LITERATURE REVSEW  2.1 Systems Closure and Minimum Impact Technology in the Pulp and Paper Industry "The ultimate goal of a closed cycle mill is to have minimal impact on the environment" (Johnson etal, 1996).  Systems Closure or closed cycle refers to a form of pollution prevention control practiced by the pulp and paper industry in which liquid effluents are minimized by recycling them back into the process (Towers and Wearing, 1994).  The driving pressures behind closed cycle developments in the pulp and paper industry have been increasing public environmental expectations reflected both in regulation and the market place.  Relevant concerns surrounding the pulp and paper industry in particular include (Gleadow et al, 1994): •  forest ecology - including concerns regarding sustainable forestry and protection of old growth forests and bio-diversity;  •  emissions- toxicity and odors from air and water emissions from processing operations;  •  waste reduction- paper recycling, and decreased consumption of water and energy use.  It has been suggested that minimization of the environmental impact of the pulp and paper industry will require an integrated approach - a combination of measures including: pollution control at the source (choice of species for pulp production, optimization of storage to 4  prevent pollution to the surrounding environment and transformation of wood based pollutants while in storage); appropriate choices regarding fillers and additives, in-plant changes to reduce fresh water requirements and allow for process water recycling (integration of biological and physical treatments on-line) and application of additional chemicals (for example, biocides) (Geller and Gottsching, 1982).  Regulation of the pulp and paper industryfroman environmental perspective has undergone significant changes since the 1970's, when emissions controls were first implemented. The original wastewater discharge regulations were based almost entirely on the assimilative capacity of specific receiving water bodies (Edde, 1994), whereas recent amendments to wastewater discharge regulations and future legislation are aimed at prevention of degradation of sensitive environments and promotion of innovative solutions to pollution prevention, including closed cycle technologies (Dexter, 1996).  Production of paper from a closed cycle or zero-effluent mill offers a recyclable product (paper) produced from a renewable resource which directly addresses the issues of water use and toxicity. When combined with an air quality control program, solid waste minimization and appropriate forest management, it represents a significant step to address public concerns surrounding the environmental impacts of the pulp and paper industry (Gleadow et al, 1994). Closed cycle technology is seen by many proponents as environmentally "benign" (Patrick et al, 1994).  The challenge of closed cycle technology raises a number of issues, including technical and economic feasibility, and questions regarding the effects on the process operation and 5  maintenance, air quality and product quality (Johnson et al, 1996). Closure of pulp and paper operations will clearly result in increased temperatures and contaminant concentrations, changes in pH and electrochemical properties and microbial populations in the process waters which may result in a variety of detrimental process and product effects (Kotila and Estes, 1994). Retrofitting of "open" pulp and paper mills to closed cycle operation would require a vast reduction in fresh water use, due to the fact that the costs associated with system closure are a direct function of the volume of process water to be recovered.  Fresh water  requirements for mechanical newsprint mills need to be reduced to the 2-5 m /adt range before 3  the very high capital and operating costs associated with closure compare favorably to external biotreatment and disposal  Nonetheless, there is evidence to suggest that improved resource productivity (heat, fiber and chemical recovery) and decreased treatment costs may offset some of the major capital costs associated with closure (Dexter, 1996; Towers and Wearing, 1994).  There have been several attempts at closure and zero effluent technology in the pulp and paper industry. These have met with varying, degrees of success, with 20 mills operating world wide (in 1996) as totally effluent free operations (Wiseman and Ogden, 1996).  The first commercial attempt at closed cycle technology in the pulp and paper industry was the Rapson-Reeve process. The Rapson-Reeve approach to closure of bleached kraft mills wasfirstproposed by two University of Toronto researchers, Dr. W.H. Rapson and Dr. D.H. Reeve in 1967. The process proposed to eliminate all contaminated effluent and fresh water make-up by several modifications to the process: replacement of up to 70% of the chlorine in 6  the first stage bleaching process with chlorine dioxide; use of counter current washing; minimization of fresh water use in the bleach plant; recovery of salt from white liquor crystallization; provision of spill control; and use of a stripper to treat evaporator condensates. In 1973, Great Lakes Forest Products (now Avenor) proposed to use this process in a new bleached kraft mill in Thunder Bay, Ontario. In 1977, the construction was completed and bleach plant effluent recovery and salt removal from the kraft liquor recovery cycle commenced.  This process was never able to achieve full recycle of bleach plant effluents, and after repeated efforts to modify the process, it was abandoned in 1985. Failure of the process was attributed to a variety of causes (Hershmiller et al, 1992): •  significant corrosion throughout the process - the operational lifetime of evaporators and boiler recovery tubes was judged to be about one quarter of that observed in similar equipment from an "open" operation;  •  low steam economy in the white liquor evaporators, resulting in high energy costs;  •  pitch build up and deposition preventing production of acceptable quality market pulp;  •  scaling and solids precipitation in thefirsttwo evaporators of the salt recovery plant, and plugging of pipelines carrying alkaline bleach plant effluent as a result of CaC0  3  deposition; •  problems with recovery furnace operation and emissions control as a result of the high salt content in the black liquor;  •  significant operating problems in the causticizing of green liquor;  7  •  increased consumption (approximately 15%) of bleaching chemicals due to the reduced efficiency in pulp washing.  Several other attempts at zero effluent technologies were pursued following the failure of the Rapson-Reeve approach.  In 1991, the BCTMP (bleached chemi-thermomechanical pulp) mill owned and operated by Louisiana Pacific in Chetwynd, British Columbia attempted to operate a zero-effluent mill by implementation of a freeze crystallization process.  Freeze crystallization is a process most often associated with the concentration of fruit juices. As a mechanism for dehydration, it is preferable to evaporation, as the latent heat of crystallization is lower than the latent heat of vaporization, and as such, represents a significant savings in energy. In this application, process water from the pulping operation was first clarified by dissolved air flotation and then passed through a series of low temperature heat exchangers to crystallize off the pure water, leaving a contaminated concentrate. This concentrate was then recycled to the freeze process or incinerated.  This process failed to work as a result of the covering of the heat exchangers with huge sheets of ice and calcium carbonate deposits which completely inhibited heat transfer. This process was abandoned in 1993 and replaced with a mechanical vapor recompression (MVR) evaporation system which had been used successfully at the Millar Western BCTMP mill in Meadow Lake, Saskatchewan.  8  The zero-effluent operation at Meadow Lake was devised as a solution to a lack of locally availablefreshwater. The Millar Western mill is situated in a location with a ready supply of wood, electricity, natural gas and labor, but with a limited water supply, particularly in winter when the water supply is anoxic and the flow is extremely limited (Gleadow et al, 1994).  BCTMP pulping is particularly amenable to closed cycle technology due to the low water use pulping (10 - 20 m /adt), the compatible effluent from pulping and bleaching operations, high 3  yield and relatively new plants (Reid and Lozier, 1996).  At Meadow Lake, process water from the pulp mill is screened and treated in flotation clarifiers to remove suspended solids and then evaporated in large vapor recompression evaporatorsfrom2% to 35% w/w solids. The TOPSfromthe evaporators is then stripped of volatile organics, while the MTDS is biologically stabilized and returned to the process water stream. The liquorfromthis process is incinerated in a recovery furnace. Suspended solids removed in the screening and flotation processes are passed through a sludge press and incinerated, or sent to landfill.  The Millar Western mill at Meadow Lake has instituted a number of in-mill changes to further minimizefreshwater consumption, such as the use of 2% (solids content) water in chemical feed applications and to wash process equipment with a high degree of counter current washing (Reid and Lozier, 1996).  Still, there is a net loss of water from this operation, requiring a fresh water make-up of approximately 2 m /adt. Pulp quality does not appear to be compromised as a result of this 3  9  reduced fresh water consumption, though the energy requirement per tonne of pulp is significantly higher thanfroma traditional BCTMP pulping operation.  Current research in the area of pulp and paper mill closure is focused on separation technologies to purge trace contaminants which otherwise would accumulate to unacceptable levels in the process water (Wearing, 1993). There are a variety of options, physical, chemical and biological, to treat Whitewater reviewed in later sections. A brief discussion of published technical and economic assessments is also presented.  "The challenge is to develop alternative process configurations in existing and new installations and to evaluate and verify their economic and technical performance" (Gleadowera/., 1994)  2.2 Closure of Integrated TMP-Newsprint Mills  2.2.1 Integrated TMP-Newsprint Whitewater System TMP, or thermomechanical pulping, is a type of mechanical pulping in which wood chips are steamed at atmospheric pressure, prior to refining in a disc refiner. Pulp may be processed in either one or two refiners, mixed with water in a latency chest to straighten the pulp fibers and then screened and cleaned.  In the case of an integrated TMP-newsprint mill, the cleaned pulp is thickened and then sent to a paper machine where it is processed and dried into sheets of finished paper. For  10  newsprint manufacture, TMP is mixed with a small percentage of kraft, or chemical pulp, prior to papermaking, to improve the quality of the paper  Large quantities of fresh water and steam are added to the wood fibers during the pulping and papermaking process, 50-200 m of water/adt of pulp in older mills and 10-20 m of water/adt 3  3  pulp in newer mills. This water, when reclaimed in the mill, is then referred to as Whitewater. Whitewater, also referred to as backwater, is the general term for any stock filler or process water containing fiber fines (Smook, 1990). "Rich" Whitewater contains a high concentration of fiber fines (>0.02%), while "lean" Whitewater contains a lower concentration of fiber fines (Smook, 1992).  2.2.2 Minimum Effluent TMP-Newsprint Whitewater As a completely closed TMP-newsprint mill does not presently exist, the composition of the Whitewater from such an operation is unknown.  To date, several researchers have  investigated the potential composition of a Whitewater from a mill implementing water reduction/closure strategies.  Jarvinen et al. (1980) determined that the release of pollutants from TMP pulp occurred in two stages: carbohydrates dissolve at the refiner, while lignins and extractives dissolve in conjunction with pulping post-treatment. It has been found that the bulk of the biochemical oxygen demand found in TMP pulping Whitewaters is released at the primary refiner. Closure of the Whitewater system of an integrated TMP-newsprint mill and implementation of a countercurrent flow system, with allfreshwater entering the mill at the paper machine would  11  result in a concentration gradient between the pulp and paper mill Whitewaters, and a decreased dissolution of extractives and lignin in the pulp mill (Jarvinen et al, 1980).  Pietschker (1996) assessed the impact of total water system closure on Whitewater quality, chemical additive performance and microbial populations. Closing the Whitewater system resulted in higher concentrations of suspended and dissolved solids, increased temperature and reduced dissolved oxygen in the Whitewater. The increased temperatures and decreased oxygen levels resulted in a decreased concentration of aerobic bacteria, and a burgeoning of anaerobic microbiological activity (Pietschker, 1996).  Table 2-1 presents some published composition data for minimum effluent TMP newsprint Whitewaters. All data presented in this table (with the exception of Lo et al, 1994) were collected in pilot plant experimentation using the SCAN-M method of "hot disintegration" pulp washing.  Table 2-1: Composition of TMP-Newsprint Whitewater Reference Water use (m /adt) Temperature (°C) TDS (mg/L) RFA (mg/L) Extractives (mg/L) TCOD (mg/1) BOD (mg/L) Lignin (mg/L) 3  Francis, 1996b 2 8510 71.94 458  5  1880  Jarvinen etal, Francis, 1985 1996b 4.6 5 50-60 4960 50.4 349 300 3720 1400 823 2110  Jarvinen et al, Lo etal, 1985 1994 6.8 7 50-60 15.4-13.6 258 3140 1300 1075  1050  Table 2-1 indicates that the concentrations of all contaminants greatly increase with decreasing water consumption. 12  Table 2-2 presents data from three researchers who were investigating different treatment methods for a minimum effluent TMP-newsprint Whitewater. The Whitewaters were produced using three different methods: "hot disintegration" (Jahren and Rintala, 1996); a mixture of 10% evaporator concentrate, 80% 4th stage TMP cleaner rejects and 10% chip wash water (Lagace et al, 1996); and a mixture of 0.7% evaporator bottoms, 20% plug screw feeder pressate and tap water (Tardif, 1996). The Whitewater used by Tardif had been used in two previous studies - Johnson (1995) and Elefsiniotis (1994).  Table 2-2: Composition of Manufactured TMP-Newsprint Whitewater . Reference Water use (mVadt) Temperature (°C) TDS (mg/L) RFA (mg/L) Extractives (mg/L) TCOD (mg/1) BOD (mg/L) Lignin (mg/L) 5  Jahren and Rintala, 1996  Lagace etal, 1996 15  Tardif, 1996 2-5  2400  3200 27.2  62  170 3390 1865  2200 1100 630  Clearly, there has been a wide variation in the accepted composition of simulated low water use TMP-newsprint Whitewaters studied to date.  Table 2-3 presents data from two sewer profiles on the Whitewater from the TMP-newsprint mill used in this thesis.  13  Table 2-3: TMP Whitewater from Howe Sound Pulp and Paper Reference Water use (m /adt) Temperature (°C) TSS (mg/L) BOD (mg/L) 3  5  Sim, 1993 20 57 606 648  Mawbray, 1995 20 61.4 (68.6-35.1) 972 (2016 - 140)  2.3 Implications of TMP-Newsprint Closure Although no fully closed TMP-newsprint mills exist at present, there is a body of literature examining the potential effects of closure on the composition of Whitewater, the operating conditions within the mill and pulp and newsprint quality.  2.3.1 Whitewater Characteristics  2.3.1.1 Increased Temperature Present TMP Whitewater temperatures range from 57-62 °C (Sim, 1993; Mawbray, 1995; Jahren and Rintala, 1996).  With closure, and the reuse of process water, will come an  increase in the average temperature of this Whitewater (Pietschker, 1996; Wearing, 1992; Jarvinenefa/., 1985).  Increased operating temperatures may result in energy cost savings and production increases for energy limited systems (Kotila and Estes, 1994), but may also result in increased wear and maintenance costs for production equipment (Johnson et al, 1996).  14  The negative impact of increased operating temperatures with closure would be most apparent in the biological waste treatment plant of a closed system. Flippin and Ekenfelder (1994) summarized these effects as: suppressed BOD removal, increased effluent  solids  concentrations and poorer sludge settleability, with the magnitude of these problems increasing at temperatures above 40 °C.  Johnson (1995) observed very poor sludge  settleability and poor removal of all contaminants of interest in a sequencing batch reactor treating simulated TMP-newsprint Whitewater when operated at temperatures greater than 40°C. Liu et al. (1993b) examined the effect of temperature on the treatment of a CTMP effluent in an aerobic bioreactor over the range of 13-50 °C. They observed a moderate increase in removal of RFA, BOD , COD, TOC and total carbohydrates (measured as 5  apparent glucose) as the temperature was raised from 13 °C to 20 °C, a slight drop in removal effectiveness of all contaminants as the temperature was raised from 20 °C to 40 °C, and a dramatic decrease in contaminant removal when the temperature was increased from 40 °C to 50 °C. The reduction in treatment performance above 40 °C was attributed to a lower mixed liquor suspended solids concentration and a decrease in dissolved oxygen concentrations (Liu etal, 1993b).  Treatment of pulp and paper wastewater by anaerobic biological systems does not appear to be as highly affected by increases in temperature. Rintala et. al (1991) used an anaerobic treatment system at 55 °C and 65 °C to treat sulfate-rich pulp and paper wastewater and observed little appreciable difference in COD removal. Jahren and Rintala (1996) reported slightly lower removal of COD from a TMP Whitewater at 70°C (55%) than at 55 °C (68%).  15  2.3.1.2 Increased Contaminant Concentrations Clearly with process water recycle and fresh water input minimized, there will be an increase of all substances in a TMP-newsprint Whitewater. The potential implications of increased concentrations of five particular contaminants are discussed here.  Pilot plant and simulation studies have demonstrated that the accumulation of contaminants in the Whitewater circuits increases exponentially with system closure - these contaminants can result in a wide range of problems, often synergistic in nature (Noel et al, 1992).  Dissolved, Colloidal, and Suspended Solids An increase in dissolved and suspended solids concentrations can affect both the pulping and paper making processes, as well as the quality of the product.  Wearing (1992) indicated that increased concentrations of dissolved and colloidal substances (DCS) were a major concern in closure of mechanical newsprint operations, although lab scale and pilot plant experiments indicated that high concentrations of DCS can be tolerated.  Dissolved solids contain inorganic and organic species - primarily wood components dissolved in the refining process but also chemical additives. These include (but are not limited to) hemicellulose fragments, resin and fatty acids, extractives, cations (Na, K, Ca, Mg, Fe, Al), chloride ions and oxidized sulfur compounds (Asselman et al, 1994). The presence and concentration of various dissolved components in the Whitewater can be highly affected by process conditions and wood species (Lloyd et al, 1996).  Asselman et al. (1994) also  reviewed a number of articles that investigated the impacts of dissolved solids on the 16  papermaking process.  Effects included a reduction in the surface tension of the pulp,  decreased retention aid efficiency and corrosion.  Suspended solids or "fines" potentially pose significant problems for mill closure. The major problems associated with increasedfinesconcentration are: consumption of additives and the production of surface foam. Additives, particularly high molecular weight cationic bridging polymers, associate with suspended solids, which results in a reduction of their effective volume and a shielding of their effective charge. As a result, much larger quantities of cationic additives are required in paper making (this is discussed further under the heading "Cationic Demand"). High concentrations of suspended solids also result in the production of surface foam. This foam causes problems with housekeeping and safety, in addition to causing deposition on the product. Surface foam carries entrained air which can cause pump cavitation and drainage problems, (Barnett and Grier, 1996).  Organics Increased organic concentrations and long incubation periods in the Whitewater system will result in increased microbiological activity. As discussed under the heading "Solids", the increased operating temperatures and the resulting decrease in dissolved oxygen will cause a shift in bacterial populations towards microorganisms which are primarily anaerobic (Gudlauski, 1996).  Increased anaerobic bacteria levels will result in slime deposition, odor, under-deposit corrosion, toxic gases and fiber degradation. Two anaerobic species commonly found in papermaking systems - Desulfovibrio spp. and Clostridium spp, which would flourish under 17  closed conditions, produce volatile fatty acids and hydrogen sulfide which have strong distinct odors which can permeate both the mill atmosphere and the finished product (Gudlauski, 1996).  Resin and Fatty Acids (RFA) Resin and fatty acids are members of a large group of compounds referred to as extractives, comprising 8% of the dissolved and colloidal substances in the Whitewater from TMP processing (Voss, 1987). Resin and fatty acids are released at the first refiner of a two refiner pulping system and are present in the process water in dissolved, colloidal and particulate form (Peng and Roberts, 1996). With increased closure and process water reuse, resin and fatty acid concentrations in the process water will increase.  Resin acids (RA) are tricyclic, diterpenoid, carboxylic acids that are naturally found in the wood extractives fraction of softwoods.  Resin acids are classified as either abietanes or  pimaranes, differentiated by the substitutions at the C13 position.  Resin acids are non-  volatile, hydrophobic, and tend to be more soluble under alkaline conditions (at pH >7 the dissolution of resin acids increases dramatically (Voss, 1987; Bicho et al, 1995). Ekman et al. (1990) showed that a greater fraction of resin and fatty acids were found in the Whitewater at pH 8 than at pH 5 - 5.5.  Resin acids are the primary cause of toxicity in wastewaters from mechanical pulping. Leach and Thakore (1976) determined that 60 - 90% of the acute toxicity resulting from TMP wastewater could be attributed to resin acids. Resin acids are most toxic in their particulate and colloidal fractions (Hoel, 1995), with toxicity increasing markedly with decreasing pH 18  (Leach and Thakore, 1976). Dehydroabietic acid (DHA) is the most abundant resin acid in TMP pulp and paper wastewaters, and although it is the least degradable, it is also the least toxic. Abietic acid is the second most abundant resin acid in TMP wastewaters - it is both more degradable and more toxic than DHA (Patoine et al, 1997).  Zender et al. (1994) examined the biotransformation pathways in resin acid degradation in an aerobic/ anaerobic treatment plant for wastewater from a kraft pulp and paper mill and found that resin acids could be broken down by hydrogenation, hydroxylation and decarboxylation. Resin acids are readily degradable in aerobic treatment plants (Liu et al, 1993b), and are removed by bio-oxidation, adsorption onto sludge and air oxidation (Liu et al, 1996). Resin acids have been shown to be problematic in anaerobic treatment plants - often causing inhibition of methanogens (Patoine et al, 1997; Bicho et al, 1995).  The resin acid content of wastewater streams in pulp and paper mills has been found to vary seasonally (Bicho et al, 1985) perhaps as a function of changes in the wood furnish or possibly due to in-mill changes. Total resin acid content of the chip wash stream from a mill in the interior of British Columbia was found to be significantly higher (60%) in the winter months (December - February) than in the summer and fall (Bicho et al, 1995).  Fatty acids (FA) are straight chain carboxylic acids having an even number of carbon atoms ranging from 12 - 24. In mechanical pulp suspensions, fatty acids exist primarily as "bound" esters rather thanfreefatty acids. Fatty acid removal in biological treatment systems is nearly 100% (Voss, 1987).  19  "Pitch" is a term used to describe colloidal deposits offreefatty acids (5-15%), esterified fatty acids (30-55%), glycerols (30-50%) and resin acids (2-40%) and their esters (Mouyal, 1996). Pitch is known to be highly problematic in papermaking, causing deposits on paper, wires and felts of the paper machine (Nguyen and Dreisbach, 1996) and slowing production by diminishing water drainage and decreasing paper strength, resulting in costly web breaks and shut-downs (Jacobs, 1995).  The presence of resin and fatty acids at high concentrations, can cause pitch to form as a thin layer on the surface of fines and fibers and as dropletsfreelysuspended among the fibers in the process water (Jacobs, 1995).  Cationic Demand Closing of the Whitewater system will give rise to an increase in cationic demand (also referred to as "anionic trash" or detrimental substances) as these compounds are only partially adsorbed or not adsorbed at all onto solids in the paper stock, and as such, accumulate in the water circuit (Linhart et al, 1987; Mikkonen and Eklund, 1996). This group of compounds is particularly prevalent in TMP pulping wastewaters and consists primarily of acid soluble lignin, Klason lignin, carbohydrates, uronic acids, fatty acids, resin acids, acetic acid, acetyl compounds, organic extractives and minerals (Alince, 1987). The "anionic" nature of this material is associated with the dissociation of carboxyl and sulfonic acid groups, and specifically adsorbed hydroxyl groups. These compounds form a relatively stable suspension, as the particles are prevented from settling by repulsive electrostatic forces (Nylund, 1993). The accumulation of cationic demand within the water system is limited by the solubility of each compound - at extremely high concentrations, some cationic demand will agglomerate 20  onto the active surfaces of solids materials - leading to paper deposits and runnability problems (Linhart et al., 1987). '  Control of cationic demand is of particular concern to papermakers concerned with the retention of fillers, fines and additives (Alince and Pikulik, 1991). Retention is an important control parameter to minimize fiber loss, to reduce deposits on paper forming equipment responsible for corrosion and, in a closed system, to maximize the quantities of BOD, COD and nutrients which leave with the paper stock - preventing microbial growth in the Whitewater system (Foster and Rende, 1997). Retention aids, typically high molecular weight cationic polymers, are added to mechanical pulp suspensions to increase the retention of fines andfillersby adherence to the surface of thefiberparticles and "bridging" between individual fibers (Mikkonen and Eklund, 1996).  Cationic demanding substances interact with these cationic polymers and reduce the effectiveness of these retention aids by three mechanisms: decreasing the effective volume of the polymer, shielding the effective cationic charge, and complexing with the polymer to form polyelectrolyte complexes (PEC) which are ineffective as retention aids (Barnett and Grier, 1996; Nylund, 1993; Jacobs, 1995). Figure 2-1 shows the change in effective volume of the polymer with increased salt concentration, an indication of the decreased effectiveness of cationic polymers with high contaminant concentrations.  21  Extended Rod — Low Salt *'  Approximation  «•?  o  o  o  o  o  o  o  o  I ... l . l . t . l . l . T . t .  \  ,  Each Condition  _  Baiting Up —  Random Coil — Moderate Salt  High Salt  Figure 2-1: Configuration of a Linear Cationic Polymer (taken from Pietschker (1996))  The degree to which cationic demand limits the effectiveness of retention aids is a function of a number of factors including pH and salt concentration (Foster and Rende, 1997; Mikkonen and Eklund, 1996; Nylund, 1993), the effective charge of the polymer (Linhart et al, 1987), type of polymer, concentration of suspended colloidal and particulate matter (Sundberg, 1995) and ionic strength of the Whitewater (Alince and Pikulik, 1991; Penniman, 1995).  Linhart et al. (1987) identified some actions which can be taken to minimize the effect of cationic demand on retention aid systems: correct selection of raw materials; improvement of the water circuit; purification of fresh water and Whitewater; removal of detrimental substances with the paper stock by use offixingagents and choosing a suitable combination of cationic retention aids.  22  UV-Lignin UV-lignin, so-called for the fact that it comprises the majority (>70%) of all material in pulping effluents which absorbs light in the ultraviolet region, is the second most abundant component of wood.  Lignin is the glue, or cement which binds the cellulose and  hemicellulosefiberstogether to give wood its structural rigidity. Lignin is a high molecular weight, complex, three dimensional aromatic polymer composed of three phenyl propane monomers. Lignin is only soluble in water when it has been broken down into smaller fragments. (Voss, 1987).  Due to its inherently insoluble nature, lignin is associated with the "colloidal" fraction of Whitewater, consisting of high and low molecular weight lignosaccharides adsorbed onto colloidal resin particles (Jacobs, 1995).  Lignin, when in high concentrations, such as in closed Whitewater systems is a major component of pitch (refer to "Resin and Fatty Acids") and a primary culprit in the neutralization of cationic polymers used as retention aids.  2.3.2 Corrosion Increased temperatures and high concentrations of dissolved solids, and gases, enhanced biological activity and failure to provide adequate cleaning and flow result in substantially increased rates of corrosion in closed mill systems (Bowers, 1983).  Hubbe and Bowers (1978) examined 30 northern European mills which were closed or partially closed, and found that lower pH (below 5) and high alum concentrations resulted in  23  corrosion of mild steel and brass, for all grades of paper production. A number of authors (Robinson, 1982; Thompson and Garner, 1996) have documented increased corrosion of 304 stainless steel, although corrosion of 316 SS was very uncommon. Corrosion of 304 SS appears to be of three types (Robinson, 1982)) heat affected zone (HAZ) pitting on welded coupons; ii) pitting of guillotined edges and iii) pitting on plain surfaces - initiated by a scratch of other surface defect. Corrosion by galvanic action may be enhanced when mixed metals are installed with new process equipment (Bowers, 1983).  Increased concentrations of "critical" ions - thiosulfate (S2O3 "), sulphate (S0 ") and chloride 2  2  4  (CI") have been shown to cause increased pitting, increased propagation rates in crevice corrosion and increased cracking in austenitic steel (Thompson and Garner, 1996). Sodium hydrosulphite, a common bleaching agent in mechanical pulping, dissociates by the following reaction to produce sodium thiosulfate:  H 0 + 2Na S 0 -> N a S 0 + 2NaHS0 2  2  2  4  2  2  3  3  A number of other Whitewater characteristics have been shown to influence the rate and degree of corrosion of process machinery including: pH (the production of sodium thiosulfate drops off rapidly above pH 5); concentration of organic acids and microbiological activity (Bowers, 1983).  Corrosion in closed systems can be minimized by reducing the concentration of CI" in the Whitewater; restricting the use of sodium hydrosulfite, increasing the pH of pulp stock prior to bleaching, and replacement of 304 SS piping with 316 SS. 24  2.3.3 Product Quality Decreased fresh water usage in the manufacture of TMP-newsprint would result in increased concentrations of certain key contaminants (e.g. lignin, extractives and carbohydrates) which could negatively impact the quality of thefinishedproduct.  A number of investigations, presented here in chronological order, have examined the effects of Whitewater closure on TMP pulp and newsprint. Heller et al (1979) operated a pilot scale paper machine under complete Whitewater recycle conditions and found problems with brightness reversion, color, sizing and first pass retention. Increased conductivity, extractives and sulfate concentrations have been shown to have a detrimental effect on electrochemical mechanisms required for drainage, retention, and sizing and decreased physical strength of the newsprint (Wenzl, 1981).  Wenzl also observed that increased anaerobic microbiological  activity in the Whitewater system resulted in production of H S, and acetic, propionic, butyric, 2  and lactic acids resulting in strong putrefactive odors in the finished product. Jarvinen et al. (1985) found that increased lignin, carbohydrate and extractive concentrations resulted in lowered brightness and slightly decreased tensile strength but that opacity and light scattering properties of the newsprint increased with Whitewater closure. No change in the printing properties of newsprint produced under closed conditions was observed (Jarvinen et al, 1985).  Wearing et al (1985a) performed an extensive series of experiments examining the effect of closure on newsprint properties.  Increased  25  concentrations  of lignin, extractives,  polysaccharides and other surface active components  were found to change the  hydrophobic/hydrophilic balance of the fiber and effluent, resulting in decreased interfiber hydrogen bonding and strength and a reduced effectiveness of brightening agents. Wet web tensile strength and dry strength properties were impaired as a result of lower surface tension forces, reduced fiber/fiber interaction, decreased bonded area and decreased bond strength. Handsheet drainage time was found to be unaffected by the increased concentrations of dissolved and colloidal substances, while the optical properties of the handsheets appeared to be slightly affected by the increase. Of all contaminants, fatty acids were identified as the most detrimental due to their high surface activity (Wearing et al, 1985a).  It has been determined that increased concentrations of colloidal particles (0.1 - 1 urn), composed primarily of extractives, decreased the tensile strength of newsprint (Francis, 1996a).  2.4 Closure Alternatives  2.4.1 Fresh Water Use Minimization The primary step in the closure of integrated pulp and paper mills will be a reduction of fresh water usage from current values of 10-150 m /adt, to 2-5 m /adt, such that novel treatment 3  3  alternatives become economically viable (Wearing, 1992; Robinson, 1982). In addition to increased closure opportunities, reduction of fresh water usage results in other savings including reduced effluent treatment costs, lower energy costs, higher recovery of fiber, reduced water treatment costs, and compliance with effluent regulations.  26  The fresh water requirement of a particular mechanical newsprint mill is determined by the quantity of contaminants released from the wood into the water stream during pretreatment, refining and bleaching, the type of paper being produced and the age of the mill. The concentration of contaminants in the water stream is a function of the type and extent of pretreatment, the presence or absence of interstage or pulp washing, the bleaching conditions, and the maximum allowable BOD in the effluent (conventional treatment systems should not have greater than 600 - 700 mg/L BOD) (Reside, 1994).  Whitewater management strategies are based on two main principles (Noel et al, 1992): where possible, Whitewater should be used to replace fresh water; and water streams must be segregated based on water quality (i.e. rich or cloudy Whitewater should be kept separate from lean or clear Whitewater). A high degree of Whitewater closure can be achieved by replacingfreshwater additions by recirculated Whitewater of a suitable quality. The choice of which Whitewater streams can be reused is primarily a function of the quality of the Whitewater. Water use reduction in mechanical pulp and paper mills is often limited by the stringent water qualities perceived as being necessary for certain pieces of critical mill equipment, such as paper machine showers (Reside, 1994).  Simulation models can be used to estimate the degree of water reduction possible for a particular mill and the possible locations for water reuse in mechanical pulp and paper mills. Jantunen (1993) applied the RAMI dynamic simulation of mass and energy balances to an integrated pulp and paper mill and determined that replacement of fresh water with paper machine Whitewater in pulp washing and the wood room could reduce fresh water consumption from over 20 m /adt to 6.9 m /adt. 3  3  27  Noel et al. (1992) used the PAPMOD steady state simulation package developed by Paprican to investigate water use reduction in a Canadian TMP-newsprint mill. For this particular mill, they identified four practical changes the mill could implement to limit fresh water requirements: i) recirculation of water from the paper machine section (following filtration to remove long fibers); ii) improvement of the cleaner circuit to increase fiber recovery from the rejects; iii) reuse of screw press Whitewater and other highly contaminated streams as dilution for a high consistency streams; and iv) increased use of Whitewater on paper machine showers along with the installation of self cleaning shower heads to prevent clogging.  Potential opportunities for the reduction of fresh water requirements have been investigated by a number of authors. Noel et al. (1992) suggested that the fresh water minimization would require mill wide control and management of Whitewater inventories - allowing for fluctuations in individual chest levels and tank sizing capable of handling exceptional needs like paper breaks.  Ropponen (1979) concurred that fresh water requirements could be  minimized by controlling the number of chaotic events like accidental overflows which disrupt the water and fiber balance in a mill and by decreasing the volume of water leaving with rejects.  Reside (1994) identified a number of streams with the potential for fresh water  replacement within the mill, namely: saveall Whitewater, cloudy/rich Whitewater, paper machine rejects, press section Whitewater, vacuum pump seal water, cooling water returns, evaporator distillates and dryer vapor. In addition, reduction of the pulp mill purge rate, an increase of the consistency of the final pulp press, recovery of heat, paper machine reject thickening, and use of clear Whitewater for hoses, cleanup and showers could result in major savings in terms of fresh water requirements and as a result, effluent production. 28  2.4.2 Pulp Washing As was briefly mentioned in the previous section, pulp washing is one means of reducing the fresh water requirements of an integrated TMP-newsprint mill.  Over 90% of the BOD, COD, extractives and trace inorganics (Na, K and Si0 ) found in 2  TMP pulping effluents are derived from the dissolution of cellulosic substances during the mechanical defibration process (Breck and Wong, 1983). In a mill where the pulp is not washed, these contaminants are carried into the Whitewater system and then distributed throughout the mill. Breck and Wong (1983) showed in laboratory experiments, that the overall effluent production of a TMP-newsprint mill could be reduced to 10-15 m /adt when 3  pulp washing and pressing was incorporated, with some portion of the press filtrate being recycled into the Whitewater system.  Henzel (1984) demonstrated the removal of 75% of the BOD load in the final effluent by washing the pulp prior to paper making in Consolidated's Fort Madison corrugated pulp and paper mill. By washing the pulp and removing a high proportion of the contaminantsfromthe process with a relatively small volume of water, the volume of mill effluent can be reduced allowing for partial closure.  Wearing et. al. (1985b) examined two pulp washing arrangements (counter current and interstage washing) which would remove some contaminants from the pulp without increasing the final effluent volume and compared the mass and energy balances with a fully operational  29  integrated mill, using the GEMS dynamic simulator. It was found that the washing of pulp with recycled filtrate decreased the dissolution of wood components - that is, contaminants were more likely to remain bound to the fiber when washed with filtrate rather than fresh water. In a countercurrent washing arrangement, where fresh water is added at the paper machine, this may result in redissolution of contaminants in the paper machine section.  In addition, it was determined that an integrated TMP-newsprint mill instituting interstage washing could reduce effluent volume from 10 m /adt to 1.7 m /adt, as compared to 3.7 3  3  m /adt for a mill using a countercurrent Whitewater arrangement, with pulp washing following 3  the secondary refiner. However, interstage washing requires substantially higher capital costs and mill modification. Most mills have already instituted some degree of countercurrent flows, and pulp washing could be amalgamated with latency removal (Wearing et al, 1985b).  2.4.3 Mechanical Vapor Recompression (MVR) Evaporation The most successful technology used for mill closure to date is mechanical vapor recompression (MVR) evaporation. This technology is currently employed in the two zero effluent mills in Canada, and is described in detail in section 2.1.  2.4.4 Physical Chemical Treatment Lagace et al. (1993, 1996) examined the possibility of treating a low flow integrated TMPnewsprint Whitewater using a lime addition and clarification in an attempt to improve the quality of the Whitewater for recycle into the mill. This was proposed as a low cost alternative  30  for Whitewater treatment, eliminating the need for expensive,  maintenance-intensive  equipment and high operating costs.  A Whitewater was prepared to mimic a mill using 15 m fresh water/adt by combining 80% 3  TMP cleaner rejects with 10% contaminated condensates from heat recovery and 10% chip wash water. Lagace et al. (1993) found that they could remove 91% of extractives, 24% of the TOC, 43%> of the color and 36% or the turbidity with an optimal dosage of 800 mg/L KH P0 , 200 mg/L MgO and 1000 mg/L CaO. The addition of lime, however, resulted in 2  4  increased dissolved concentrations of calcium and phosphate (628% and 1300% respectively). This may limit the reuse potential for this Whitewater as the scaling potential would be significant.  In a second paper published by Lagace at al. (1996), they cited the optimal dose of chemicals to be 500 mg/L KH P0 , 300 mg/L MgO and 1000 mg/L CaO for removal of over 90% of 2  4  the extractives and 60% of the color from Whitewater. Again, the hardness of the treated effluent was very high, and the dissolved solids increased by 50%.  They proposed a  Whitewater treatment scheme for recycle to include a physical-chemical treatment step followed by biological treatment step to remove smaller organic contaminants and then an ion exchange step to remove sodiumfromthe effluent. This would suggest that physical-chemical treatment alone would be insufficient for treatment of Whitewater for recycle to the mill, but it may provide an inexpensive option for removal of some contaminants.  31  2.4.5 Aerobic Biological Treatment Conventional aerobic biological treatment or secondary treatment for pulp and paper mill effluents usually consists of an aerated lagoon, activated sludge treatment system (AST), or a sequencing batch reactor (SBR). The treatment process includes a primary treatment step, where the wastewater is settled in a primary clarification tank, an aerobic biological treatment step and a secondary clarifier where the biomass is settled from the treated effluent. Secondary biological treatment is the current "end-of-pipe" technology used to reduce organic material, suspended solids and toxic constituent concentrations to within effluent limitation guidelines.  The installation of secondary treatment systems for TMP-newsprint effluents was a result of the implementation of strict discharge limitations and guidelines promulgated to protect aquatic ecosystems.  TMP-newsprint effluents have low pH (4.6 - 6.1), low alkalinity, low  acidity and high concentrations of organic materials, dissolved and colloidal solids and toxic extractives such as resin acids, that are not removed by primary treatment alone (Thurley, 1983; Huster et al, 1991). TMP Whitewaters are toxic to fish, and anaerobic treatment alone is insufficient to completely detoxify these effluents (Lo et al, 1994).  Thurley (1983), Servizi and Gordon (1986), Liver et al. (1993) and Lo et al. (1994) have published results from activated sludge (AST) pilot scale and mill scale plants treating TMP and CTMP effluents. Earlier studies (Thurley, 1983; Servizi and Gordon, 1986) suggested that long retention times (5-7 days) were required to remove sufficient levels of BOD and to 5  detoxify effluents, but more recent studies (Liver et al, 1993a; Lo et al, 1994) have shown that shorter retention times (8-24 hours) will remove up to 96% of the BOD and 100% of the 5  32  influent resin acids can be removed from the influent stream.  Degradation of organic  components follows first order kinetics (Lo et al, 1994) and requires careful control of biological parameters such as F/M ratio, sludge age and loading rate to optimize removal and prevent sludge bulking (Liver et al, 1993).  Conventional aerobic systems are relatively simple to operate and are capable of treating TMP effluent sufficiently for discharge into the environment under current legislation. However, aerobic biological treatment requires high capital (large storage tanks, and control equipment) and operational (nutrient addition, cooling, pH neutralization, aeration, sludge disposal) costs and is susceptible to system upsets. Drastic changes in effluent composition, as a result of a spill or break can disrupt aerobic biological systems and may result in incomplete treatment or "toxicity breakthrough" (Roy-Arcand et al, 1996). At temperatures greater than 40 °C, problems with biomass decay and sludge settling can also occur (Johnson, 1995; Liu et al, 1993a).  Roy-Arcand et al. (1996) investigated the use of ozonation in conjunction with an aerobic biological system to treat high strength TMP wastewaters. They examined the pretreatment of the high strength components of the wastewater stream (e.g. wood room and chip wash wastewaters) with ozone prior to biological treatment and found an improved removal of contaminants.  Johnson and Hall (1995) examined the treatment of a simulated, low effluent, integrated TMP-newsprint Whitewater with a sequencing batch reactor at temperatures of 20, 30, 40, 45 and 50 °C. They reported removal of COD from 76-65%, removal of dissolved and colloidal 33  solids (32-25%) and high removal of fatty (92-95%) and resin acids (99 - 100%) below 40 °C. Above 40 °C, fatty acid removal was 95-96% but removal of all other contaminants significantly decreased.  The lowered contaminant removal efficiencies were observed  concurrent to lower reactor biomass concentrations and reduced substrate utilization rates and growth yields.  2.4.6 Recycle of Secondary Effluent Wearing (1992) suggested that one option for mill closure is the reuse of secondary treated effluent (possibly following a tertiary polishing step) in mill operations. A number of North American pulp and paper operations reuse treated sewage or treated mill wastewater mixed with treated linerboard effluent as the mill water source (Dorica et al, 1996).  Dorica et al. (1996) examined a TMP-newsprint wastewater treated by a full scale primary treatment system (including coagulation and flocculation) followed by a pilot scale air activated sludge system, for reuse within a mill.  The treatment system was capable of  removing 95% of the influent BOD , 91% of the COD, 94% of the total suspended solids 5  (TSS), 87%> of the color and 99% of the resin and fatty acids. Even with high treatment efficiencies, the concentrations of COD, TSS and color in the treated effluent were still 80120%) higher than the surface water used in the mill. Concentrations of certain metals and ionic species - aluminum, calcium, silicate, chloride and sulfate - were also slightly higher in the treated effluent. Mixing of the treated effluent with surface water in various proportions also yielded interesting results. Residual ionic species in higher concentrations in the treated effluent responded in a straight line dilution, but a synergistic removal (9-30%) was observed  34  with COD, potassium, aluminum, iron and manganese. With this information, they attempted some steady state modeling of replacement of the millfreshwater supply with a mixture of a 1:1 fresh watentreated effluent and found that the expected steady state concentrations of most contaminants would be in the range presently encountered in pulp and paper operations.  2.4.7 Anaerobic Biological Treatment Anaerobic biological treatment is similar to aerobic biological treatment, in that it may consist of primary clarification followed by a biological (in this case anaerobic) step and, often, secondary clarification. Anaerobic biological treatment has a number of advantages over aerobic biological treatment (Jurgensen et al, 1985) including reduced capital and operational costs, an ability to treat high strength wastes and methane production to offset power costs. Anaerobic systems can tolerate higher organic loading rates than aerobic systems as they are not limited by oxygen transfer (Ince et al, 1993).  Anaerobic treatment has seen some application as an internal "kidney" to purge contaminants from closed cycle waste paper mills (Huster et al, 1991; Barascud et al, 1992, 1993; Habets et al, 1996). Huster et al. (1991) discussed the idea of an installation of an anaerobic treatment step into the Whitewater circuit of a plant processing waste paper to prevent the build up of impurities in the water circuit and deposits on the product. Barascud et al. (1992) built a lab scale upflow anaerobic sludge blanket (UASB) to treat Whitewaterfroma recycled paper mill and were able to remove 75% of the COD from the high strength wastewater (10,000 mg/L) stream. A pilot scale application of this same technology was only able to remove (64 - 42%) of the influent COD, but resulted in reduced cationic demand and  35  improved sheet forming characteristics and strength properties of the paper when used in paper forming experiments.  Habets et al. (1996) documented the installation of a pilot scale treatment system with an aerobic "polishing" step to removed dissolved and colloidal solids, volatile fatty acids, secondary stickies and anionic trash at the Zulpich Papier recycled paper mill in Cologne, Germany. The anaerobic stage was able to degrade carbohydrates, VFA's and sulphates to produce methane and hydrogen sulphide for low energy consumption and a low biomass growth. However, the degradation was incomplete and produced odorous byproducts which could contaminate the final product. The aerobic polishing step was able to convert the remaining organics to carbonate and remove calcium hardness in the form of a calcium carbonate precipitate, and remove the odor causing compounds.  Schnell et. al. (1990) examined the effluent management system at the Spruce Falls Power and Paper Co. in Kapuskasing, Ontario and found that a pilot scale high rate anaerobic treatment system installed at the mill was incapable of completely detoxifying the effluent and removing sufficient quantities of BOD5 to meet effluent discharge requirements. In this case also, an aerobic treatment step was added to remove the residual BOD and resin acids. 5  Rintala and Lepisto (1992) examined the feasibility of treating a TMP Whitewater for reuse within the mill by batch anaerobic treatment at 35, 55 and 65 °C and UASB treatment at 55 and 70 °C. The TMP effluent was treatable at all temperatures - 65-75% of the influent COD was removed in the UASB at 55 °C and 60% of the COD was removed in the 70 °C reactor.  36  They found that carbohydrates accounted for 40-50% of the COD removal and that methane was produced from 57-85% of the metabolized COD.  Low molecular weight and monomeric lignins and fatty acids are easily degraded in anaerobic treatment systems, while resin acids and high molecular weight lignin usually comprise the recalcitrant fraction of COD. Anaerobically treated effluent is darker in color, likely due to the increase in chromophoric phenolic groups produced in the breakdown of polymeric lignin (Rintala and Lepisto, 1992; Sierra-Alvarez era/., 1990).  The quality of the anaerobically treated effluent may be negatively impacted by the high decay rate of thermophilic bacteria - Rintala and Lepisto (1991) found that some portion of the COD in the treated effluent was a result of bacterial lysis.  Jahren and Rintala (1996) studied the closure of a TMP Whitewater circuit by the insertion of a UASB at 55 and 70 °C. They built a treatment system in which the Whitewater was passed through a UASB and was then cycled through a "hot disintegration" process (to mimic pulp washing) and then returned to the UASB. They found that the UASB was able to remove all COD, carbohydrate and UV-Lignin that was dissolved in the hot disintegration step and that the system was stable following two recirculations. The study did not examine the influence of the UASB effluent on product quality, although the pulp washed with the effluent from the UASB was reported to be discolored and less cohesive.  37  2.4.8 Ultrafiltration Membrane separation processes remove contaminants from a feed stream based on steric exclusion and/or interaction of the solute and solvent with the membrane surface. Nonporous membranes remove unwanted contaminants by molecular interactions with the membrane surface, while porous membranes transfer the bulk fluid through the membrane leaving the contaminants behind (Pfromm, 1996). Classification of porous membranes is based on the molecular weight cutoff (MWCO) and pore size of the rejecting surface - microfiltration (MF) has a pore size of 1000-10000 A, ultrafiltration (UF) has a pore size of 10 A, and reverse osmosis (RO) has a pore size of 1 A. Nanofiltration (NF) lies between ultrafiltration and reverse osmosis (Bryant and Sierka, 1993).  Membranefiltrationis generally operated under "cross flow" conditions in which membranes are configured in a tubular arrangement and the liquid to be clarified is pumped axially through the membrane tube under pressure.  The pressure forces the permeate (primarily  solute and somefractionof dissolved materials) to pass through the membrane while larger solutes and solids are retained in the feed stream. Some rejected material accumulates at the membrane surface as a "gel layer", imparting an additional resistance to permeation in a process referred to as concentration polarization. The thickness of this layer is controlled by the axial flow of fluid through the membrane tube which creates a shear stressfieldparallel to the membrane surface retarding the accumulation of a thick filter cake. Under steady state conditions, the convective transport controlling the accumulation of a gel layer, and the shear force dispersion, balance each other (Upton et al, 1997). The rate at which permeate is produced per unit area of membrane is referred to as the flux (J), and can be modeled by the following equation: 38  J7] X S(Rm+Rp+ Rc) where: AP  = transmembrane pressure  T)  = dynamic viscosity  Rm  = resistance associated with the membrane  Rp  = resistance associated with pore plugging  Rc  = resistance associated with cake fouling of the membrane surface  The two major disadvantages of membrane treatment are the high energy requirement to produce permeate and the loss of flux resulting from membrane compaction and fouling of the membrane surface (Sierka etal, 1994).  Ultrafiltration is able to remove most suspended and colloidal materials, including microbial matter from the feed stream at relatively high fluxes (Deitrich, 1995). Ultrafiltration compares favorably, in terms of capital and operational costs, to other closed cycle technologies (mechanical vapor recompression and freeze crystallization) at fluxes greater than 140 L/(m  2  hr) (Paleologou etal, 1994).  Treatment of wastewaters by membrane filtration technology results in a treatedfiltrateor permeate and some volume of concentrate which still requires disposal following treatment. This concentrate can be burned in an incinerator or used in the manufacture of such products as adhesives (Dorica, 1986).  39  The original membranes used in filtration technology were constructed from organic polymers, but more recently, inorganic (ceramic) membranes have been introduced into use. Ceramic membranes are generally superior to organic membranes in thermal, mechanical and structural stability, chemical and microbiological resistance and ease of cleaning and regeneration.  Ceramic membranes are constructed from inert mineral materials (such as  zirconia or alumina) and generally consist of a porous, mechanically strong supports a few millimeters thick, upon which is superimposed a thin layer of a selective membrane (a few microns thick) with one or more intermediate layers sandwiched between the membrane and support (Hseih, 1988). Figure 2-2 shows a scanning electron micrograph of an alumina membrane and support.  Ceramic membranes generally have a sharply defined pore size, a high tolerance to extreme pH, to oxidizing and reducing environments, and radiation. They can easily be cleaned by removing single units from a module. They can also withstand temperatures of up to 350 °C and pressures of up to 15 bar (Pejot and Pelayo, 1993).  40  Figure 2-2: Scanning Electron Micrograph of Alumina Ultrafiltration Membrane (Hseih, 1988)  In ultrafiltration applications, fouling is primarily attributed to the deposition of colloidal material on the membrane surface. Rejected colloidal materials deposited on the membrane surface can be transported back into the bulkfluidby Brownian motion, by shear induced lift or by electrostatic repulsion.  Diffusivity resulting from Brownian motion increases with  decreasing particle size (<0.01 urn), while diffusivity as a result of shear induced lift increases with particle size (>10 um) such that colloidal particles in the range of 0.01 - 10 um are most likely to cause the fouling of ultrafiltration membranes (Ramamurthy et al, 1995).  The nature and extent of fouling is influenced by the chemical nature of the membrane, the solution to befilteredand membrane/solute interactions. Proteins, salt, and lipids can adsorb onto the membrane surface and/or precipitate into the pores resulting in increased resistances, and decreased flux. Physical factors, such as temperature, flow rate, pH and pressure also affect the rate and extent of fouling (Cheryan, 1986).  41  Table 2-4: Comparison of UF studies on Pulp and Paper Effluents Study  Operating Conditions  Performance  Doricaetal. (1985)  Membrane: Tubular Cross Flow  Flux: 198 L/(m «hr)  MWCO: 20 kDaltons  Removal Efficiencies:  Pressure: 1 MPa  2  % RFA = 100%  Temperature: 75 °C VRF 20 Elefsiniotis et al. (1995)  Membrane: tangential flow  Flux: 48 L/(m »hr)  MWCO: 10 kDaltons  Removal Efficiencies:  2  Pressure: 240 kPa  % Total Solids = 21  Temperature: 40 °C  % Dissolved COD = 35  VRF 10  % RA = 25 % FA = 94  Elefsiniotis et al. (1995)  Membrane: tangential flow  Flux: 72 L/(m »hr)  MWCO: 100 kDaltons  Removal Efficiencies:  2  Pressure: 240 kPa  % Total Solids = 13  Temperature: 40 °C  % Dissolved COD = 20  VRF 10  %RA=45 %FA= 100  Ekengren et al. (1993)  Membrane: Tubular cross-flow Flux: 100 L/(m »hr) 2  Removal Efficiencies:  (negative charge) Pressure: 750 kPa  % COD = 58  Velocity - 3 m/s  % AOX = 63 % RA = 55 % FA = 75  Ekengren et al. (1991)  Membrane: Tubular cross-flow Flux: 135 L/(m *hr) 2  (negative charge)  Removal Efficiencies:  Pressure: 750 kPa  % COD = 60-80  Velocity - 4.5 m/s  % AOX = 60-9  42  Table 2-5: continuing (Table 2-4) Study Operating Conditions  Performance  Jonsson and Wimmerstedt Membrane: Tubular cross-flow  Flux: 150L/(mMir)  (1985)  Removal Efficiencies:  MWCO: 60 kDaltons  % COD = 50  Velocity - 4 m/s VRF: 10 Pejotand Pelayo (1993)  Manttari et al. (1997)  Membrane: Tubular cross-flow  Flux: 100L/(m -hr)  Pressure: 400 kPa  Removal Efficiencies:  2  Velocity - 4 m/s  % COD = 75  VRF: 15  % Total Solids = 32 sheet cross Flux: 15 L/(m »hr)  Membrane: flat  2  Removal Efficiencies:  flow MWCO: 8 kDaltons  % COD = 56  Pressure: 1.5 MPa  % UV 8o = 67 2  Temperature: 40 °C Velocity = 3 m/s Nuortila-Jokinen  et al.  (1994)  Membrane:  ceramic tubular Flux: 54 L/(m »hr) 2  cross flow  Removal Efficiencies:  MWCO: 10 kDaltons  % Cationic demand=72  Pressure: 101 kPa  % UV oo = 62 4  Temperature: 25 °C VRF = 1.8 Nuortila-Jokinen (1995)  et al.  Membrane: tubular cross flow  Flux: 51-62 L/(m «hr)  MWCO: 8 kDaltons  Removal Efficiencies:  2  Pressure: 200 kPa  % COD = 20-8  Temperature: 41 °C  % Dissolved Solids"= 12-2  Velocity = 2 m/s  % Cationic demand =72-77 % UV  2 8 0  = 24-7  % UV400 = 62  43  Ultrafiltration has been used in the pulp and paper industry for effluent treatment, concentration of dilute streams and fractionation (Jonsson and Wimmerstedt, 1985). Zaidi and Buisson (1991) published a comprehensive historical review of the use of membrane technology in the pulp and paper sector, noting the renewed interest in membrane treatment in the 1990's as a result of the increasing pressure on industry to reduce the discharge of toxic organics (with the long term expectation of eliminating discharges) and the improved manufacturing technology for membranes and membrane systems allowing for the production of membranes which are customized to suit specific requirements.  Table 2-4 presents a  comparison of UF treatment studies for pulp and paper effluents.  Ultrafiltration is a physical treatment technology to separate contaminants from a wastewater stream based on steric exclusion and membrane interactions which has seen extensive application and research in the pulp and paper sector as a result of its simplicity of operation and lower cost than some biological operations at higher temperatures.  2.4.9 Membrane Bioreactor (MBR) The membrane biological reactor (MBR) is a wastewater treatment technology which is a modification of the activated sludge process, whereby the solid-liquid separation step is performed by an ultrafilter rather than a secondary clarifier.  Activated sludge treatment  systems often experience incomplete sedimentation or problems with sludge bulking, such that long HRTs, low biomass concentrations and tertiary polishing may be required to keep the quality of thefinaleffluent high (Ilias and Schimmel, 1995).  44  The biological step of the MBR treatment system converts soluble organic contaminants into insoluble biomass, which can then be filtered out using the ultrafilter (Drummond et al, 1992). The effectiveness of the solid-liquid separation is primarily a result of interactions between the membrane and the solute and solvent, in addition to steric (size exclusion) and electrochemical (Van der Waals) effects (Dufresne et al, 1996).  Membrane bioreactor technology was conceptualized at the University of California at Los Angeles in 1959 when Sourijan and Loeb developed an asymmetric thin skin cellulose acetate membrane (Mishra et al, 1994).  By the mid-1960's Dorr-Oliver began to explore the  technology of membrane ultrafiltration and in 1969 they oversaw the development of the membrane sewage treatment system (MST) (Budd and Okey, 1969). The MST consisted of a suspended growth aerobic biological reactor, from which effluent was drawn and passed through a membrane loop. The first large scale application of this technology was a pilot plant in the mid 1960's in Greenwich, CT. By the mid 1970's, Thetford systems developed a similar municipal sewage treatment plant, the "Cycle-Let" system. To date, there are over 80 Cycle-Let systems for aerobic and anoxic treatment of municipal wastewater. By the 1980's there were many versions of conventional MBR systems, both aerobic and anaerobic, available for the treatment of industrial wastewater.  The major supplier of these systems in North  America is Zenon Municipal Systems, with other versions in operation in Japan, Germany, South Africa and France including MEMBIO, Zenogem (part of Zenon) and ADUF treating a variety of municipal and industrial wastewaters (Janson and Mishra, 1993; Ross and Strohwald, 1994).  45  Membrane biological treatment offers a number of advantages over conventional biological treatment - smaller land space requirements, improved effluent quality (including complete pathogen removal (Aya, 1994)), operation at high biomass concentrations since all biomass is retained within the system, complete independence of hydraulic residence time (HRT) and solids retention time (SRT), reduced sludge production and reduced chemical costs (Zaloum et al, 1996; Hare et al, 1990).  The performance of any biological treatment system is dictated by the overall metabolic activity, which can be controlled by two parameters: A. active biomass concentration and B. biomass specific activity. A membrane bioreactor is able to operate under high concentrations of biomass, allowing for compact treatment systems capable of high organic loading rates. Lubbecke et al. (1995) examined the influence of high biomass concentrations (up to 40 g/L) on the biological response and the operating conditions in a membrane bioreactor. Loading was held constant over the course of the experiment, with the feed rate increasing with higher biomass concentrations. At biomass concentrations greater than 22 g/L they observed a wider distribution of floe size and a greater mean size. Above 30 g/L there was a drop in the flux across the membrane as a result of increased kinematic viscosity.  In addition, the rate at  which BOD could be consumed (specific substrate utilization rate) dropped slightly (less than 5  0.5%) at high biomass concentrations.  One of the first commercial applications of membrane bioreactor technology was a pilot scale aerobic suspended growth reactor coupled with an ultrafiltration system for the treatment of oily wastewater from the automotive manufacturing industry. The system exhibited almost complete removal of BOD and suspended solids, and COD removal ranging from 90.3% to 5  46  96.8% under a range of operating conditions (HRT = 1.8-3.4 days, SRT = 50-100 days) (Hare et al, 1990).  The manufacturing facility compared the cost effectiveness of three  wastewater management options: ultrafiltration (which was the current treatment system), MBR treatment  and physical-chemical treatment.  It was determined that although  ultrafiltration was the least expensive option, they would build a full scale MBR system in anticipation of additional imminent restrictions on wastewater discharges.  Two full scale  treatment systems were built at automobile manufacturing facilities in Ohio. The Mansfield, Ohio plant is treating 151 m of wastewater a day containing (on average) 5643 mg/L COD, 3  removing 100% of theBOD and TSS and 97% of the COD (Knoblock etal, 1994). 5  Zaloum et al. (1994) published the results from an MBR system treating wastewater from the metal transformation industry. The MBR system was capable of removing over 95% of the BOD (as compared to only 60% removal by UF) and was able to detoxify the final effluent. 5  The use of MBR technology in the pulp and paper industry is still being examined at the pilot scale stage. Table 2-6 presents a comparison of some studies of MBR treatment of pulp and paper effluents.  One of the major design parameters in membrane biological treatment is the maximum attainable flux through the filter. As discussed in section 2.4.8, flux is defined as the volume of effluent passing through an area of the filter per unit time and is controlled by a variety of resistances.  47  Table 2-6: Comparison of MBR studies on Pulp and Paper Effluents Study  Operating Conditions  Performance  Dufresne et al. (1996)  Membrane: Hollow Fiber  Flux: 30 L/(m'hr)  MWCO: 0.1 urn  Removal Efficiencies:  Nuortila-Jokinen et al. (1996)  Pressure: 13.5 kPa (vacuum)  % COD = 80  Temperature: 35 °C  % Total Solids = 36  VRF 15  % Dissolved Solids = 32  Membrane: cross flow flat sheet Flux: 38L/(m «hr) 2  (neg. charge)  20% loss of flux = 2 hours  Pressure: 800 kPa  Removal Efficiencies:  Velocity = 2.8 m/s Tardif (1996)  % COD = 77.9  Membrane: tubular cross flow  Flux: 15 L/(m «hr)  MWCO: 0.08 urn  Removal Efficiencies:  2  Pressure: 79 kPa  % COD = 81  Temperature: 55 °C  % Dissolved COD = 78  VRF 37  % Total Solids = 43 % Dissolved Solids = 38 % RFA = 100 % Cationic Demand = 53  Bohman et al. (1991)  Membrane: tubular cross-flow  Removal Efficiencies:  MWCO: 8 kDaltons  % COD = 69-74  Pressure: 1000 kPa (vacuum)  % BOD = 69-74 7  % AOX = 56-60  In the case offiltrationof biosolids, flux is controlled by transmembrane pressure, viscosity and the resistances across the membrane surface (Magara and Itoh, 1991). The fouling resistance associated with cake fouling (Rc) is the predominant resistance in thefiltrationof biosolids, and the factors affecting it and its development have been the subject of extensive study.  48  Magara and Itoh (1991) found that the development of the cake layer was a function of the suspended solids concentration, and that the thickness of the cake layer was determined by fluid shear stress and operating pressure.  They observed a decrease in flux with high  concentrations of suspended solids.  Physiochemical models used to estimate flux when filtering a solution of abiotic particles have been found to underestimate the cross-flow microfiltration flux of colloidal particles (Shimizu et al, 1993). Dufresne et al. (1996) suggested that the decrease in flux across membranes used in membrane biological systems is attributable to those substances with a molecular weight of more than 500,000. This is in direct contradiction to the published work of Shimizu et al. (1993) who found that the formation of the cake layer was controlled by the shear induced back transport of particles (controlled by lift velocity) which, in the filtration of a fluid with different size particles, is controlled by the smallest particles.  Temperature has also been shown to influence the flux across an ultrafiltration membrane. Chiemchaisri and Yamamoto (1994) found that flux decreased with decreasing temperature (from 25 -5 °C), as a result of the increase in kinematic viscosity.  The rate and extent of fouling of the ultrafilter in a membrane biological system is another important design consideration. Fouling by biosolids has been investigated by a number of authors.  49  Fane et al (1994) showed that in some cases the accumulation of only one layer of bacteria along the surface of the membrane is sufficient to reduce the flux by one or two orders of magnitude. Biomass particulates are colloidal and adhesive, and biofluids are adsorptive and tend to aggregate such that the fouling potential of biological suspensions is very high. They observed that thefiltrationof bacteria which form an extracellular (EC) matrix causes the void spaces in thefilterto becomefilledwith EC matrix which can impart the bulk of the hydraulic resistance across a filter. The extent of fouling and the difficulty of cleaning appear to be functions of the ionic concentration of the filtrate and the transmembrane pressure. To minimize fouling whenfilteringbiological material, low to modest pressures should be used, and thefiltershould be an isoporous membrane of high porosity.  Shimizu et al (1994) observed that the shear stress applied by cross flow pumping used in the filtration process broke bacterial cells and induced the discharge of granulated matter such as glycogen and cell wall fragments. These particles were found to increase the mean specific filtration resistance, and to reduce the flux as a result of the increased cake fouling. They also reported that the steady state flux in a mixture of different size particles (such as a shear broken cell suspension) was controlled by the lift velocity of the smallest particle.  Choo and Lee (1996) examined the fouling in a membrane coupled anaerobic bioreactor (MCAB) and found that the external fouling was closely related to two factors: migration of cells to the surface of the membrane and inorganic precipitation. They found that 16% of the biomass in the reactor was associated with the membrane surface as a result of the shear stresses associated with mechanical pumping, the flow of permeate across the cell surface forcing cells to move and anchor to the membrane surface and the ideal growth conditions at 50  the membrane surface with a constant permeation of nutrients and substrate through the attached layer. The inorganic precipitate struvite (TvIgNH P04 6H 0) was found to harden ,  4  2  the cake layer at the membrane surface and prevent sloughing of the foulant.  2.5 Technical and-Economic Assessments of Closure Options Several authors have published economic and technical comparisons of closure options in an attempt to identify the most feasible technology to achieve zero effluent.  Jantunen (1993)  used the RAMI dynamic mass and energy balance simulator to compare the capital and operating costs for open and closed greenfield newsprint mills. The proposed technologies for the closed mill included a combination of evaporation, ultrafiltration and reverse osmosis to treat 6.9 m /adt water internally, while the open mill treated this same effluent in an external 3  biological treatment plant. It was determined that there were no major differences in capital or operating costs between the open and closed greenfield mill.  However, using this same  model, the author concluded that the closure of an existing newsprint mill is unlikely to be profitable.  The lowest cost and optimal performance closed cycle configuration would be specific to each particular mill, requiring some combination of in-mill and ex-mill measures to achieve zero discharge. Gerbasi et al. (1993) examined three options for closing a TMP-newsprint mill producing 550 adt newsprint/day. The authors determined the capital and operating costs for the treatment of 20 m /adt, 10 m /adt and 5 m /adt of effluent by three systems: biological3  3  3  membrane treatment (including anaerobic, aerobic, ultrafiltration and reverse osmosis unit operations); freeze crystallization and mechanical vapor recompression evaporation. These  51  costs were then compared with the capital and operating cost of a conventional end-of-pipe biological treatment plant with discharge to the environment. They determined that the costs associated with any of the closed cycle technologies were significantly higher than the cost for treating the effluent in a conventional secondary treatment plant, and the difference between these costs increased as the volume of effluent to be treated was increased. Of the three closed cycle technologies, they determined that evaporation is the least costly and most proven technology available for systems closure at this time. Suitable technologies for system closure must be insensitive to effluent flow rates, should treat the effluent only to the degree required and be able to be implemented in stages.  A techno-economic assessment for the closure of an older integrated-newsprint mill was developed to determine the relative costs of reducing effluent flows to 10 nvVadt, 5 m /adt and 3  2 m /adt and then treating the effluent by evaporation (Francis et al, 1995). These costs were 3  compared to the costs of constructing and operating a biological (secondary) treatment plant and discharging the effluent.  Effluent volumes were minimized by a number of measures:  counter current water recycling, paper machine furnish thickening, ultrafiltration of Whitewater for shower water and broke system sizing. Unlike the results reported by Gerbasi et al. (1993), this study found that effluent reduction and system closure had a higher capital cost but a lower operating cost than biotreatment and discharge, and that amortized over time, system closure was a more economically viable treatment option.  Braker et al (1996) examined four strategies for effluent reduction in a fully integrated TMPnewsprint mill: partial closure without effluent segregation, total closure without effluent segregation, partial closure with effluent segregation and total closure with effluent 52  segregation.  With the use of a simulation model, they determined the operating  concentrations of dissolved solids and the relative pay-back periods for each of the options.  Results from the model indicated that the biological system currently treating the effluent would require some modifications to assimilate the increased concentrations of contaminants present in the wastewater and that under total system closure scenarios, the concentration of dissolved solids could increase to values in excess of 13,000 mg/L, which could result in decreased product quality and increased corrosion of the system. Evaluation of all the options determined that partial closure without segregation of the process and non-process streams was the simplest option to implement, with a quick pay-back period, but that partial closure with segregation of process and non-process streams would ultimately be the best option to minimize biological treatment costs.  Wiseman and Ogden (1996) evaluated the costs for six options of zero effluent pulp and paper processing: physical treatment (clarification); physical treatment followed by biological treatment; physical treatment, biological treatment and membrane filtration; physical treatment and membrane filtration; mechanical vapor recompression evaporation and freeze crystallization. The authors noted that zero effluent would first require a major reduction in the volume of effluent to be treated, by means of such water reduction techniques as the use of mechanical seals, clarified Whitewater for cleaning, savealls for fiber recovery, and the segregation of water streams. The conversion to a closed cycle system would require a major capital investment and the incurring of significant operating cost. It was determined that physical treatment alone, although being the least expensive option, would not produce sufficiently clean water for reuse. Membrane treatment was determined to be less expensive  53  (lower capital and operating costs) than MVR evaporation or freeze crystallization, but was thought to be of limited practical application as a result of its susceptibility to chemical fouling and attack.  Tardif and Hall (1997) examined ultrafiltration (UF), sequencing batch reactor (SBR), filtration of SBR effluent and MBR treatment of a minimum effluent integrated TMPnewsprint Whitewater for reuse within the mill.  They determined that the most effective  removal of the contaminants of interest (resin and fatty acids, total dissolved solids, dissolved COD and dissolved organic carbon) was by the sequencing batch reactor followed by ultrafiltration. However, this treatment was only effective up to temperatures of 40 °C, such that it was not appropriate for high temperature applications. For high temperature treatment of this effluent, the MBR was judged to be the most suitable process for treating the Whitewater. It was found that the MBR was stable under a range of operating conditions, and was able to remove 100% of the influent RFA, 84-72% of the dissolved COD and 18-37% of the dissolved solids. The MBR was shown to be a superior technology to the SBR for this application. The MBR allowed for total retention of solids, complete control of the sludge retention time, produced less sludge requiring disposal and was a more robust and compact treatment system.  2.6 Summary and Conclusions A review of the current literature on systems closure in integrated TMP-newsprint mills yielded the following conclusions.  54  Systems closure or closed cycle technology is a form of pollution prevention in which liquid effluents are minimized by recycling them back into the process. System closure in the pulp and paper industry is of interest due to increased public environmental expectations and increasingly stringent legislation. TMP-newsprint operations use large quantities of water; older mills in the range of 50-200 nvVadt and newer mills in the range of 10-20 m /adt. 3  Closure of pulp and paper mills will first require a drastic reduction in the volume of effluent requiring treatment, into the range of 2-5 m /adt. 3  Closure of Whitewater systems will result in a variety of effects, including: increased temperature (up to 70 °C), decreased oxygen levels and increased concentrations of various, contaminants (solids - both suspended and dissolved, organics, resin and fatty acids, cationic demand and U V lignin), corrosion of piping and equipment and reduced product quality. Complete closure of TMP-newsprint mills will require management of contaminants at a levels at which runnability and product quality are not compromised. There are a number of alternatives available to close the water system in a TMP-newsprint mill - reduction offreshwater use and implementation of pulp washing as well as various treatment alternatives: mechanical vapor recompression evaporation, physical-chemical treatment, biological treatment (aerobic and anaerobic), recycle of secondary treated effluent, ultrafiltration and membrane biological treatment, most of which are still being investigated at a lab scale.  Viable treatment alternatives must be able to withstand  changes in effluent supply and quality, be able to treat effluent only to the level required and be able to be implemented in a staged fashion.  55  Techno-economic assessments have been performed on some of the treatment technologies, with evaporation appearing to be the most viable treatment alternative presently available. Two promising alternatives for system closure which have not been demonstrated at pilot or full scale to date are ultrafiltration and membrane biological treatment. A direct comparison of these two treatment alternatives would provide valuable information about the treatment effectiveness and system capacity before pilot scale testing.  56  3. OBJECTIVES FOR THE RESEARCH The hypothesis stated at the onset of this research was as follows: "There will be an appreciable difference between the treatment capabilities of an aerobic membrane bioreactor and an ultrafiltration system for the treatment of a minimum effluent integrated TMP-newsprint Whitewater when operated under identical conditions".  As discussed in Chapter 1, this research project was part of an investigation into possible treatment options for a minimum effluent integrated TMP-newsprint Whitewater for direct reuse within the mill. Related research completed prior to this thesis was as follows: Johnson (1995) examined the biological treatment of minimum effluent integrated TMP-newsprint Whitewater by a sequencing batch reactor (SBR) at temperatures from 20 to 50 °C and an HRT of 2 days; Elefsiniotis (1994) investigated the treatment of this same Whitewater by ultrafiltration at temperatures ranging from 10 to 50 °C using two plate and frame filters (operated in batch mode) with differing membrane pore sizes (10 and 100 kDaltons); Elefsiniotis et al. (1995) then considered the treatment of minimum effluent Whitewater by SBR and UF in series, byfilteringSBR effluent using the plate and frame 10 and 100 kDalton UF filters. Tardif (1996) considered the treatment of a similar minimum effluent whitewater by aerobic membrane biological reactor (MBR) at temperatures from 40 to 55 °C and HRTs of 0.7-2.8 days, with a ultrafilter of a MWCO of 75 kDaltons. The investigations into treatment options at that point had rendered several key conclusions (Tardif and Hall, 1996). •  Aerobic biological treatment of a minimum effluent integrated TMP-newsprint whitewater in a sequencing batch reactor (SBR) at temperatures between 20 and 40 °C resulted in removal of 40% to 100% of all contaminants of interest.  57  •  At temperatures greater than 40 °C, treatment of the Whitewater in the SBR resulted in poor contaminant removal efficiencies as a result of low biomass concentrations, poor sludge growth and poor sludge settleability.  •  Ultrafiltration of the Whitewater was unaffected by temperature, but yielded poor removal of most key contaminants of interest (with the exception of fatty acids).  •  The sequential combination of SBR+UF resulted in significant removals of all contaminants considered, but was not feasible at temperatures greater than 40 °C (due to the poor settleability of the sludge), and resulted in the production of significant volumes of waste sludge and/or concentrate from both treatment systems.  •  MBR treatment resulted in removal of 35% - 100% of all contaminants of interest (with the exception of color) under the full range of operating conditions considered: temperatures from 40 to 55 °C and HRTs of 0.7-2.8 days and produced minimal waste sludge.  •  Flux through the MBR ultrafilter with a MWCO of 75 kDaltons was very low - (8-13 L/m hr), a full order of magnitude lower than the flux through the UF membranes with 2  MWCOs of 10 and 100 kDaltons used by Elefsiniotis (1994).  There were a number of unanswered questions remaining following these investigations: 1. What would the composition of a minimum effluent integrated TMP-newsprint Whitewater be, and how could that be most closely simulated using existing pulp and paper mill wastewaters? 2. Does an MBR offer sufficient advantages over ultrafiltration to offset the additional costs associated with biological treatment (such as: aeration, temperature regulation, and  58  nutrient addition) and the potential for process instabilities under dynamic operating conditions? 3. What is the minimum hydraulic retention time in the MBR to adequately degrade the organic matter in the Whitewater? 4. What is the effect of volume reduction factor (VRF) on the performance of the ultrafiltration membrane in the MBR and UF treatment systems?  It was thought that operation of an MBR and a UF system in parallel, (using identical membranes, under a range of operating conditions) treating a simulated minimum effluent TMP-newsprint Whitewater could answer these questions.  Ultrafiltration membranes typically operate in the range of VRF = 3 to VRF =15, while aerobic membrane biological systems operate at HRT's of 3 days to several hours. It was desirable that the range of operating conditions examined in this experiment would include the optimum range for each system. A minimum hydraulic residence time of 8 hours was chosen to comply with the experimental constraints of Whitewater supply and to minimize Whitewater storage time prior to use.  The approach chosen for this project attempted to address a number research objectives: 1. To compile a thorough review of any information in the literature pertaining to TMP, newsprint and integrated TMP-newsprint Whitewaters and determine: •  the most likely concentrations of key contaminants in a TMP-newsprint whitewater in a mill with excess flows of 2-5 m /adt, and 3  59  •  the most reasonable approximation of that whitewater using existing pulp and paper wastewater streams.  2. To operate a lab scale ultrafiltration system and an aerobic membrane bioreactor in a manner that allowed for a comparison their treatment capabilities, maximumflux,fouling potential, and retentate characteristics. 3. To determine the effects of varying the hydraulic retention time (to a minimum of 8 hours) on the biokinetics of the M B R . 4. To investigate the behavior of an ultrafiltration system operated in a continuous fashion under varying volume reduction factors. 5. To compare the treatment capabilities and flux through the M B R and UF treatment systems when operated in parallel.  60  4. EXPERIMENTAL METHODS AND APPARATUS In this section, descriptions of all materials and experimental methods used in this investigation are presented.  Section 4.1 describes the apparatus used, Section 4.2 the  materials, and Section 4.3 the methods. Section 4.4 gives a brief description and explanation of the experimental design used in this study  4.1 Experimental Apparatus 4.1.1 Membrane Biological Reactor System A schematic of the system, which consisted of an aerobic biological reactor and ultrafiltration unit, is shown in Figure 4-1. All process piping was PFA (Teflon) except for the membrane module which was constructedfromalpha alumina.  4.1.1.1 Aerobic Reactor The aerobic reactor was constructed from clear polyacrylate tubing with a diameter of 25.4 cm (10") and a length of 29.6 cm. This reactor was surrounded by a second piece of tubing also 29.6 cm in length and 30.4 cm (12") which acted as a water jacket for temperature control. Ports were located in the lid of the reactor for feeding of wastewater and nutrients, and wasting of sludge. A thermocouple, aeration unit, three level controllers and a condenser, to prevent water vapor loss due to evaporation, were mounted on the lid of the reactor. Mixed liquor was pumped from the aerobic reactor to an ultrafiltration unit using a progressing cavity Moyno 500 pump, model number 33304-04fromCole Parmer, Inc. The pump was powered by a 3/4 hp motorfittedwith a variable speed controller. Liquid level in the reactor was 10 L for runs 1 and 2, and 5 L for run 3.  61  Figure 4-1: Aerobic Membrane Biological Reactor  62  4.1.1.2 Ultrafiltration Unit The ultrafiltration membrane chosen for this experiment was a ceramic membrane with a pore size of 500 Angstroms, small enough to filter bacteria from solution.  A pilot scale  Membralox™ ceramicfilterdistributed by the United States Filter Corporation of Warrendale, PA was chosen for this experiment on the basis of its small size, its chemically inert nature, and ease of cleaning. The ultrafiltration unit consisted of a porous ceramic filter element sealed in stainless steel housing fitted with Viton gaskets.  The ceramic membrane was  constructed of alpha alumina (99.9% pure) supported by sub-layers of ceramic material through which the permeate flowed to two outlets on the side of the housing. One of the permeate ports was capped, such that permeate flowed from a single port. showing the unit andfittingsis presented in Figure 4-2.  A diagram  The unit was removed from the  system by disconnecting the 3/8" NPTfittingsat each end of the filter.  The nominal pore size of the ceramic membranes was 0.05 um. Thefilterunit was 250 mm in length with a channel inside diameter of 7 mm. The membrane provided a total surface area of 0.0055 m . 2  The expected flow rate from the permeate port was 5 to 250 mL/min,  corresponding to a flux of 50 to 2500 L/m hr. The characteristics of the membrane, as 2  provided by the manufacturer are presented in Table 4-1.  Pressure gauges were installed at the membrane inlet and outlet to enable measurement of the pressure drop through the tube and the transmembrane pressure.  These glycerine filled  gauges manufactured by WDCA, were able monitor pressures from 0 to 413 kPa (0 to 60 psi) and werefittedwith chemical seals to prevent clogging of the gauges by particulate matter. The inlet pressure was maintained at approximately 138 kPa (20 psig). The flow rate through 63  the system was 10 L/min., resulting in liquid flow through velocities of approximately 4 m/s. Adjustments in pressure and flow rate were made by manipulating the pump speed and a plug valve on the concentrate line.  Figure 4-2: IT-70 Alpha Alumina Membralox Membrane (Membralox, 1996)  64  Table 4-1: Specifications and Operating limits of the Membralox 1T1-70 Ultrafiltration Membrane (Membralox, 1996) Model Material of construction Housing Material Nominal Pore Size Configuration Nominal Membrane Surface Area Maximum Operating Pressure Recommended Operating Pressure Temperature Operating Range pH Operating Range Recommended velocity Suggested Flux (tap water)  Membralox Ceramic Filter IT 1-70 99.9% alpha alumina 316 L stainless steel 0.05 urn single 7 mm internal diameter tube 0.0055 m 1030 kPa (150 psig) 140 - 200 kPa (20-30 psig) 0 - 300 °C 0-14 2 - 4 m/s 5 - 250 mL/min. 2  4.1.1.3 Feeding and Wastage of the Reactor A feed solution consisting of simulated, concentrated whitewater from a TMP mill was fed to the reactor using a variable speed Masterflex peristaltic pump and speed controller. A nutrient solution containing nitrogen from ammonium nitrate, and phosphorus from N a H to the reactor using a second Masterflex pump and controller.  2  P04,  was fed  Volumetric flow rates  delivered by the pumps were controlled by the speed of the pump motor. This was measured daily by means of a large graduated cylinder and timer and was adjusted as necessary.  Pumping of feed and nutrient solutions was activated once an hour by a Chrontrol timer to approximate a continuous feed.  The composition of the feed and nutrient solutions are  described in Sections 4.2.1 and 4.2.2 respectively.  Biomass was manually wastedfromthe reactor once daily to maintain a sludge retention time of 20 days.  65  4.1.1.4 Instrumentation Temperature in the bioreactor was maintained at a constant 55 °C by a water jacket surrounding the bioreactor. Water was circulated from a 62 °C water bath using a centrifugal pump at a rate of approximately 40 L/min., which resulted in a mixed liquor temperature of 55 °C. The internal temperature of the reactor was measured using a YSI thermocouple suspended from the lid into the reactor contents.  Three level controllers were installed in the reactor to control the working liquid volume and to prevent over flow from the system or burn out of the recirculation pump in the event of a mechanical or system failure. One controller activated a three way solenoid valve which recycled permeate to the reactor when flux from the filter exceeded the feed rate to the reactor. This allowed for control of the hydraulic residence time through the feed rate. A second controller interrupted feeding to the reactor when a high level float switch was activated, and a third controller switched off power to the recirculation pump when the low level float was activated.  4.1.2 Ultrafiltration System The system, consisting of a non-inoculated mixing tank and ultrafiltration unit, was identical to the membrane bioreactor system depicted in Figure 4-1, though the dimensions varied slightly. Total system volume was approximately 10 L, for run 2 and 5 L for runs 3, 4 and 5.  66  4.1.2.1 Mixing Tank The mixing tank was constructed from clear polyacrylate tubing with a diameter of 20.3 cm (8") and a length of 52.8 cm. The mixing tank was surrounded by a second piece of tubing also 52.8 cm in length and 25.4 cm (10") in diameter which acted as a water jacket for temperature control. As in the membrane bioreactor, ports were located in the lid of the reactor for feeding and wastage, in addition to supporting the thermocouple and level controllers. Nutrients and aeration were not provided to the mixing tank. Concentrate was pumpedfromthe mixing tank to an ultrafiltration unit using a progressive cavity Moyno 500 pump, model number 33304-04 from Cole Parmer, Inc. The pump was powered by a 3/4 hp motor fitted with a variable speed controller. The ultrafiltration unit, feeding and wasting system, and instrumentation were configured in the same manner as in the bioreactor.  4.1.3 Membrane Cleaning System A schematic of the membrane cleaning system is shown in Figure 4-3.  UF UNIT  Figure 4-3: Cleaning System  67  40 L SINK OR 20 L BUCKET  The circuit consisted of a 40 L sink basin, two 20 L buckets containing stock solutions of acid and caustic and a rotary vane pump. Permeate flow rate was measured by collecting permeate as it was filtered into a graduated cylinder.  4.2 Materials  4.2.1 Wastewater Feed The influent to the bioreactor and ultrafiltration system consisted of a simulated thermomechanical-newsprint whitewater with a composition that was based on whitewater characteristics predicted for a low water use or zero-effluent integrated newsprint mill, as presented in Section 2.2.2. The formulation of the feed was similar to that used by Johnson (1995) and Tardif (1996) and was derived in consultation with Wearing, Francis, and Reside.  The simulated closed mill integrated TMP whitewater was prepared by combining 125 mL of 35% w/w evaporator bottoms with 2.5 L of plug screw feeder pressate and 22.375 L of clear TMP whitewater to a total volume of 25 L. In order to remove suspended fiber, the effluent was passed through a 0.4 mm mesh screen.  Simulated whitewater was made up  approximately every four weeks and stored in carboys at 4 °C.  Some fiber settled in the  storage carboys, but the feed was mixed again prior to feeding.  Plug screw feeder pressate and clear TMP whitewater were collected from the Howe Sound Pulp and Paper thermomechanical pulp mill, where TMP pulp is manufactured from a 55% spruce, 45% hemlock balsam composite (hembal) furnish. Average collection temperatures were 85 °C for the plug screw feeder pressate and 65 °C for the clear whitewater. Evaporator  68  bottoms (35% w/w) from the zero-effluent Millar Western BCTMP mill in Meadow Lake, Saskatchewan, were stored at 4 °C until use.  4.2.2 Nutrient Solution A nutrient solution was added to the aerobic reactor to provide nitrogen and phosphorus sources for cell metabolism and growth. The nutrient solution consisted of 110 g of NH4NO3 and 117 g of H3PO4 dissolved in 2 L of water. Nutrients were added separatelyfromthe feed solution in excess of the COD:N:P ratio of 200:5:1.  4.2.3 Biomass The aerobic sludge used to seed shake flasks was collected from a variety of sources to provide a mixed microbial culture. Biomass sources were selected in an attempt to enrich for a thermophilic population that was able to degrade and metabolize typical constituents of the simulated thermomechanical pulping whitewater. Sludge was collected from the 47 °C autothermal aerobic digester (ATAD) at the Whistler municipal sewage treatment plant, in Whistler , B.C. and was mixed with mixed liquor (37 °C)fromthe treatment facility at Howe Sound Pulp and Paper, in Port Mellon, B.C., settled sludge from a bench scale municipal sewage treatment study at the University of British Columbia (UBC) at 22 °C and sludge (53 °C)froma bench scale kraft ATAD unit operating at the Pulp and Paper Center at UBC.  The biomass was re-seeded periodically with sludge from the bench scale kraft ATAD, and was cultured in a shake flask incubator as described in Section 4.3.1.  69  4.3 Experimental Methods In this section, the techniques used for biomass acclimation, membrane cleaning, sampling and analytical methods will be described.  4.3.1 Biomass Acclimation Seed biomass for the bioreactor was acclimated in a shake flask incubator. Organisms were cultured in six 1 L Erlenmeyer shake flasks at a constant temperature of 55 °C and agitated at a rate of 80 rpm. The shake flasks were removedfromthe incubator and biomass was wasted and wastewater and nutrients were fed at a rate corresponding to a three day hydraulic residence time. Biomass was acclimatized for two months in this fashion, after which it was transferred to the aerobic bioreactor operated in a batch mode for two weeks.  For an  additional 6 weeks prior to beginning the experimental period, the reactor was operated in a continuous fashion to further acclimatize the biomass.  4.3.2 Membrane Cleaning Prior to removal of the membranefromthe system for cleaning, the pressure on the membrane was relieved and biomass or concentrate was removed by opening the plug valves on either end of the filtration unit. The recirculation pump was shut off, thefilterapparatus drained and valves closed, and the membrane module, gauges and valves were disconnected from the system.  The membrane module, valves and gauges were then connected to the cleaning  system and the permeate port was capped. The membrane was first rinsed with water for approximately 10 minutes. A 200-300 mg/L free chlorine solution made upfrom130 mL of  70  5% NaOCl in 20 L water was then circulated through the system for 10 minutes at ambient temperature. The ultrafiltration unit was then drained and a 20 L stock solution of 2% NaOH solution was circulated for 20-30 minutes, first with permeate ports closed, and then at a transmembrane pressure of 5-10 psi for an additional 15-20 minutes. Following that, the spaces on both sides of the membrane were drained and thefilterwas rinsed with tap water for approximately 10 minutes, until the pH was close to neutral. The permeate ports were then closed, and the membrane was rinsed with a 1% HNO3 solution for 15-20 minutes. The permeate ports were then opened at a transmembrane pressure of 10 psi for 10-20 minutes. The filter was then drained and water rinsed to neutral pH before being returned to the system. The clean water flux was then measured to confirm that the cleaning was complete. The cleaning process took approximately six hours to complete.  4.3.3 Sampling and Sample Preparation All liquid samples were collected in washed and distilled water-rinsed Nalgene containers. Samples of whitewater influent, and permeate were collected dailyfromeach system and were analyzed for total, dissolved and suspended solids, total and dissolved chemical oxygen demand (COD), resin and fatty acids (RFA), cationic demand and UV lignin. Samples (2 mL) for RFA analysis were preserved with 1 mL of a 50% methanol, 50% 2N NaOH solution and frozen in fired glass test tubes until extracted and analyzed.  Samples of mixing tank  concentrate and sludge were also collected daily and analyzed for total, suspended and volatile suspended solids.  Grab samples of the reactor and mixing tank contents were taken from the wastage line and analyzed for total and dissolved COD, and resin and fatty acids  71  4.3.4  Quality Assurance/ Quality Control (QA/QC)  All samples were analyzed in-house, following the analytical methods outlined below. Standards, blanks and in some cases, duplicates were analyzed as part of a quality control program.  Further details are given in section 4.3.5.  Percent removal data for each  contaminant, for each water recovery fraction, are presented with 90% confidence intervals to indicate the variability of each data set.  4.3.5 Analytical Methods and Equipment  4.3.5.1 Solids Analysis Samples were analyzed for total solids (TS), total dissolved and colloidal solids (TDCS), and total suspended solids (TSS) as described in Standard Methods for Water and Wastewater Testing (APFIA et al, 1989) immediately following collection.  Mixed liquor samples from the membrane bioreactor (MBR) and concentrate samples from the mixing tank were analyzed for total, suspended and volatile suspended solids content using a slightly modified method, as filtration of an adequate volume of sample using a Whatman 934-AH was not possible. Mixed liquor and concentrate samples were centrifuged at 3000 rpm for 30 minutes and a known volume of supernatant was filtered and dried at 104 °C to determine dissolved solids content. Volatile suspended solidsfrommixed liquor samples were calculated by difference. Table 4-2 outlines the methods used for solids analysis used in this study.  72  Table 4-2: Analysis of Solids Solids type  Experimental Method  Total solids  A known volume of sample was oven-dried to a constant weight at 104 °C.  Volatile Solids  Sample from total solids determination was fired to a constant weight at 550 °C.  (mixed liquor and concentrate samples only) Total dissolved and colloidal solids (influent and permeate samples) Total dissolved and colloidal solids (mixed liquor and concentrate samples)  A known volume of sample was filtered with a Whatman 934-AH glass microfibre filter and oven dried to a constant weight at 104 °C. 40 mL of sample was centrifuged for 30 minutes at 3000 rpm. A known volume of sample was filtered using a Whatman 934 AH glass microfibrefilterand oven dried to a constant weight at 104 °C.  Volatile dissolved and colloidal solids  Sample from total dissolved and colloidal solids (mixed liquor and concentrate samples determination was fired to a constant weight at 550 °C. only) Total suspended solids (influent and A known volume of the sample wasfilteredusing a Whatman 934-AH glass microfibre filter. Filter was permeate) then dried to a constant weight at 104 °C. Total suspended solids (mixed liquor and concentrate samples) Volatile suspended solids (mixed liquor and concentrate samples)  Total suspended solids in the mixed liquor and concentrate samples were evaluated by subtracting the total dissolved solids form the total solids. The volatile suspended solids for the mixed liquor and concentrate samples were obtained by subtracting the volatile dissolved solids from the volatile solids.  4.3.5.2 Chemical Oxygen Demand Influent samples were diluted 1:10, and UF and MBR permeate samples were diluted 1:5, with distilled water prior to analysis for total COD (TCOD). Samples analyzed for dissolved COD were filtered prior to dilution using Whatman 934-AH 1.5 um microfibre filters. Permeate samples were not filtered and DCOD was assumed to be equivalent to the TCOD as the nominal pore size of the ultrafiltration unit (0.05 um) was smaller than the pore size of the  73  glass microfibre filters (such that all the particulates would be removed). Diluted samples (2 mL) were added to COD vials containing a mixture of 1.6 mL of COD digestion reagent and 2.4 mL of acid reagent (APHA et al, 1989). The vials were preserved at 4 °C until analysis. Samples were prepared and analyzed using the closed reflux colorimetric procedure (standard method 5220D) adopted by the American Public Health Association (APHA et al, 1989). Chloride ions were found to be present in all samples, such that the standard method addition of mercuric chloride was required.  Following digestion in a Hach COD reactor the  absorbance of the samples and standards was measured at 600 nm using a Hach DR-2000 spectrophotometer.  4.3.5.3 Resin and Fatty Acid Analysis Permeate and influent was sampled daily for resin and fatty acid (RFA) analysis. RFA concentrations  were determined using a method adapted from Voss and Rapsomatiotis  (1985) by the Pulp and Paper Research Institute of Canada (1988), and which was further modified in-house. Two mL of sample were placed in afiredglass test tube and 1 mL of a solution of 50% methanol and 50% 2N NaOH was added prior to freezing and storage Frozen sample tubes were then thawed immediately prior to extraction and were analyzed for resin and fatty acid content.  Grab samples of the mixed liquorfromthe membrane bioreactor and concentrate from the ultrafiltration unit were collected once per run. Samples were centrifuged at 3000 rpm for 30 minutes.  The supernatant was retained as one sample, and the pellet, containing the  particulates, was resuspended in distilled water to a volume equal to the original sample  74  volume of mixed liquor and kept as a second sample. This allowed for the determination of the resin and fatty acids in solution and bound to the solids. Samples were preserved and analyzed in the same manner as for the influent and permeate samples.  Each sample was neutralized with 2N HC1 to between pH 9-11, after which an internal extraction standard of heptadecanoic acid was added. Samples were then extracted twice with equal volumes of methyl-t-butyl-ether.  The solvent extracts were concentrated by  allowing the methyl-t-butyl-ether to evaporate under nitrogen gas. An internal methylation standard (methyl heneicosanoate and tricosanoic acid) was then added and dried again under vacuum. Methylation of the resin and fatty acids was then carried by addition of 250 uL of a solution of diazomethane gas in methanol/methyl tert-butyl ether.  The samples were then  transferred to 100 uL glass inserts in 3 mL teflon-lined glass vials prior to analysis.  Derivitized RFAs were analyzed using a Hewlett-Packard 5880A gas chromatograph with a 30 m DB-1 fused silica column of internal diameter of 0.32 mm and offilmthickness of 0.25 um (J&W Scientific, Folsom, CA) and detected using aflameionization detector (FID). The carrier gas was helium at a linear velocity of 20 cm/s at 290 °C. Theflameionization detector (FID) makeup gas was composed of helium, hydrogen and purified air (flows of 20, 30 and 400 mL/min., respectively).  The temperature regime used is detailed in Table 4-3.  The method detection limit was approximately 0.1 mg/L.  Table 4-4 summarizes the resin and fatty acids measured in the samples analyzed. Resin and fatty acid concentration values reported are in mg/L as dehydroabietic acid (DHA), as DHA was used as the methylation standard.  This approach has been used by Voss and  75  Rapsomatiotis (1985). Palustric and levopimaric acid concentrations were recorded as a pair as their peaks could not be separated.  Table 4-3: Temperature Program for Gas Chromatographic Analysis of Samples for Resin and Fatty Acids Time (min)  Temperature(°C)  Rate of Change (°C/min)  1.00  150  stable  23.75  increasing  4°C/min  3.00  265  stable  5.00  290  stable  Table 4-4: Resin and Fatty Acids Quantified in this Study Resin Acids  Fatty Acids  Pimaric Sandaracopimaric Isopimaric Palustric + Levopimaric Dehydroabietic Abietic Neoabietic  Palmitic Linoleic Linolenic Oleic Stearic  4.3.5.4 Cationic Demand The cationic demand of influent and permeate samples was determined upon collection using a method developed by the Pulp and Paper Research Institute of Canada (Kwong, 1994). Samples were centrifuged and a cationic polymer, 1,5-dimethyl 1-1,5  diazaundecamethylene  polymethylobromide (DDPM) was added to the supernatant. The excess cationic polymer in the sample was titrated with an anionic polymer, polyvinyl sulfuric acid potassium salt (PVSAK), using toluidine blue O (TBO) as a color indicator.  A summary of the method is as follows.  76  1. A solution of 0.1 % toluidine blue O was prepared by dissolving 0.100 g of TBO in deionized water in a 100 mL volumetric flask. 2. A 0.01 N solution of DDPM was prepared by adding 2.000 g of DDPM (obtained from Sigma of St.-Louis, Missouri) to 1.0 L of deionized water in a volumetric flask. From this stock solution, a 0.001 N solution for titration was prepared by diluting 100 mL of the stock solution with deionized water in a 1.0 L volumetric flask. This titration solution was used to standardize the PVSAK solution as detailed below, based on an equivalent weight of 187.11 and an average equivalent weight to cationic charge ratio of 200 for the DDPM. 3. A stock solution of approximately 0.002 N of PVSAK was prepared by slowly adding approximately 0.1622 g of PVSAK (obtained from ACROS) in 1.0 L of warmed deionized water. This solution was continuously warmed and stirred with a magnetic stir bar to enhance dissolution. An approximate 0.001 N solution was made up by dilution of this solution by 50% with deionized water. Standardization of the solution was carried out as follows: a) A blank titration was carried out to determine the cationic demand of distilled deionized water. A 100 mL aliquot of deionized water was added to a 250 mL beaker and 3 drops of the 0.1 % TBO solution were added. The solution was mixed with a magnetic stirrer for 1 minute and then titrated with the PVSAK solution until a pink end point was reached. This volume  (V t wa  er  blank)  was then  used for the calculations below. b) The PVSAK solution was then standardized: 10.00 mL of 0.001 N DDPM solution and 3 drops of TBO were added to 100 mL of deionized water in a 250 mL beaker. This solution was mixed for one minute and titrated using the  77  approximate  0.001  corresponds to V  PV  N  PVSAK  SAKblank  solution until the pink end point. This volume  in Equation  4.1.  NDDPM x VDDPM  NPVASK  (4.1)  VPVASK - VPVASK blank  where: NpvSAK  Normality of the PVSAK solution  VpvSAK blank  Volume of PVSAK consumed for titrating 10.00 mL of DDPM in a deionized water blank  VDDPM  10.00  mL  NDDPM  0.001  N  V  Volume PVSAK consumed for titrating 100 mL of  w a  t e r blank  deionized water containing three drops of TBO.  Process samples were centrifuged at 3000 rpm for 30 minutes and  20  mL of supernatant from  each sample was diluted to 200 mL using a volumetric flask. One hundred mL of the diluted sample were then placed in a 250 mL beaker and 3 drops of 0.1 % TBO and 10.00 mL of 0.001 N DDPM standard were added. The samples were then mixed for one minute and titrated with the PVSAK titration solution until a pink end point was reached. This volume (VPVSAK)  was recorded. The cationic demand of the sample could then be calculated using  Equation 4.2. Cationic demand is expressed in mg of DDPM/ L of sample. It can also be expressed in terms of eq/L by not multiplying by the factor of 2-10 mg/L in Equation 4.2. 5  78  (4.2)  where:  NpvSAK  Normality of the P V S A K solution (as determined from Equation 4.1)  VpvSAK blank  Volume of P V S A K consumed titrating 10.0 mL of D D P M in a deionized water blank  VpvSAK  Volume of P V S A K consumed in titrating 10.0 mL of D D P M in the diluted sample.  sample  Actual volume of sample (10.00 mL)  4.3.5.5 UV-Lignin Influent and permeate samples were analyzed for U V lignin daily. Four mL of each sample were acidified with 3 drops of concentrated sulfuric acid and after mixing, were allowed to react and settle. Samples were then filtered using a Whatman 934 A H glass microfibre filter and 1 mL of the filtrate was diluted 200 times with distilled water. Diluted sample was then placed in a 1 cm glass cuvette and absorbance at 205 nm was measured against a standard of distilled water using a Hach spectrophotometer.  U V - Lignin concentrations were determined as follows: UV - Lignin (g / L) = Absorbance (@ 205 nm) x Dilution  79  (4.3)  4.3.6 pH The pH of the influent, permeate, mixed liquor and concentrate was measured using a Beckman pH meter with automatic temperature compensation. The pH meter was calibrated using standard buffers of pH 4.0, 7.0 and 10.0.  4.3.7 Temperature The mixed liquor temperature in the ultrafiltration system and in the membrane bioreactor was measured constantly and recorded daily using a YSI model 47 scanning tele-thermometer equipped with a submersible thermocouple.  4.3.8 Dissolved Oxygen The dissolved oxygen concentration of grab samples of the MBR mixed liquor was also periodically monitored using a YSI model 54 ARC DO meter equipped with a model 5739 submersible probe.  4.3.9  Permeate Flow Rate  The flow rate of the permeate from both systems was monitored daily by collecting permeate in a graduated cylinder and determining the volume filtered as a function of time.  4.3.10 Statistical Analyses All percent removal data were analyzed for standard deviation and confidence intervals. The 90% confidence intervals are plotted on each graph to indicate the variability of the data presented.  4.4 Experimental Design and Operating Parameters  4.4.1 Water Recovery Fraction Water recovery fraction (Y) was the key process design parameter varied in this experimental work. Water recovery fraction corresponds to the ratio of the permeate flow rate (QP) to feed flow rate (QF), and can be related to the volume reduction factor (VRF) as depicted in Equation 4.4.  Y = — = QF  Q  F  - Q QF  W  = 1 - — VRF  (4.4)  where: Y  = water recovery fraction; QP/QF  QP  = flow rate of permeate, standardized flux (L/day)  QF  = feed rate (L/day)  Qw  = wastage rate (L/day)  VRF  = volume reduction factor  Volume reduction factor (VRF) is a means of expressing the degree to which the ultrafiltration unit has reduced the volume of the raw influent stream. For a batch system, this corresponds to the ratio of the original volume to be filtered (V ) to the final, retained filtered 0  volume (V). In a system run in a continuous fashion, this can be expressed as the ratio of feed flow rate (QF) to the wastage rate (Qw)-  81  Assuming a constant volume of retentate in the mixing tank, this can also be related to the sludge retention time (SRT) and the hydraulic residence time (HRT) (Equation 4.5).  VRF = Q L - < > = JRT Qw (V/SRT) HRT V / H R T  where:  HRT  = hydraulic residence time; V / Q F (days)  SRT  = solids retention time; V/Qw (days)  V  = volume in reactor (L)  As discussed in the previous section, this study examined the effect of water recovery fraction on permeate flux and the removal efficiencies of certain key contaminants of interest from a low water flow TMP-newsprint Whitewater in a membrane bioreactor and an ultrafiltration system.  Figure 4-4 and Figure 4-5 illustrate the experimental design used in this study. There were a total of five experimental runs - one on the membrane bioreactor alone, two with the membrane bioreactor and the ultrafiltration system running in parallel and two with the ultrafiltration system running alone.  Experimental runs one, two and three ran for approximately three weeks, with sampling almost daily. Run 3 was cut short for the ultrafiltration system (13 days versus 23 for the  82  MBR) as it was inoperable at the high volume reduction factor of 60. Run 4 (a duplication of run 2 for the ultrafiltration system) ran for 10 days with samples being taken (on average) every two days, and run 5 was approximately two weeks in length, with samples being taken every other day. Table 4.5 details the experimental program with respect to run duration, number of samples taken, solids retention time (SRT), hydraulic residence time (HRT), water recovery fraction and volume reduction factor. Runs were chosen to be approximately one solids residence time (SRT) - approximately 20 days (with the exception of run 4) , while the transitions were a minimum of 1.5 SRT (30 days). Transitions between runs were initiated the day following the last day of a run, such that the system was allowed approximately 30 days to acclimatize.  Table 4-4 and 4-5 present the runs in chronological order, with run 1  beginning at day 0.  MBR  80 70 o ro o •« o  60 A 50 40  .  30  1 >  20  E  4  10  50  i 1 00  150  200  Days  Figure 4-4: Experimental Program to investigate the application of an aerobic membrane biological reactor to treat low water use integrated TMP-newsprint whitewater.  83  UF  80  1  T  70 -iiiiiiiiiiiii 60  —  —  50 - llllllllllllllllllllllllll 40 -lllllllllllllllllllllllllllllllllll  30 JIIIIIIIIIIIIIIIIIIII 10 --  i  0 -I  1  0  50  1  1  100  150  ii  200  Days  Figure 4-5: Experimental Program to investigate the application of an ultrafiltration system to treat low water use integrated TMP-newsprint Whitewater.  Table 4-5: Experimental design and operational parameters Run  Operational Water Recovery System(s) Fraction (Y)  1 2  MBR MBR UF MBR UF UF UF  3 4 5  Duration Number of (days) samples  0.95 0.90  Volume Reduction Factor (VRF) 40 20  25 20  0.983  60  0.90 0.9  20 10  23 13 7 10  4.4.1.1 Hydraulic Residence Time  HRT (days)  SRT (days)  17 18  0.5 1  20 20  17 12 7 10  0.333  20  1 1  20 10  (HRT)  The hydraulic residence times in the membrane bioreactor and the ultrafiltration system were varied in conjunction with the solids retention time to control the water recovery fraction of  84  each system as outlined in Table 4-5. Hydraulic residence times were varied between 0.333 days and 0.75 days in the MBR and 0.333 days and 1 day in the UF system.  Hydraulic residence time was controlled using wastewater feed rate (QF). For run one this corresponded to a feed rate of 20 L/day, and for run two a feed rate of 10 L/day. The total system volume for runs one and two was 10 L. For run three, the feed rate was 15 L/day, and for runs four and five, the feed rate was 5 L/day. For runs 3, 4 and 5 the total system volume was reduced to 5 L., to reduce operational demands on the system.  4.4.1.2 Solids Retention Time (SRT) Solids retention time in each reactor was controlled by the wastage rate (Qw) under steady state conditions. Table 4.5 indicates the SRT for each experimental run. For experimental runs one and two, corresponding to water recovery fractions of 0.95 and 0.90, the wastage rate, Qw, was set at 500 mL/day, corresponding to a solids retention time of 20 days. For the runs three and four (water recovery fractions of 0.983 and 0.90) Q was set at 250 mL/day, w  corresponding to a SRT of 20 days for each run (volume of the reactor for those runs was lowered to 5 L). For run 5 Q was set at 500 mL/day, corresponding to a solids retention w  time of 10 days.  4.4.2 Temperature Internal bioreactor and mixing tank temperatures were maintained at 55 °C for the duration of the study.  85  4.4.3 Transmembrane Pressure and Velocity The transmembrane pressure on the ultrafiltration units on each system was maintained at 138 kPa (20 psi) and volumetric flow through the filters was controlled at 10 L/min. corresponding to a crossflow velocity through the filters of 4 m/s. Daily adjustments to the pump motor speed and the plug valve on the return line maintained these settings.  4.4.4 Nutrients Nitrogen and phosphorus additions to the MBR were made in excess of a COD:N:P ratio of 200:5:1 to provide sufficient nutrients for cell metabolism and growth.  86  5. RESULTS AND DISCUSSION In this section, the data and results obtained during the whitewater characterization and the operation of the ultrafiltration and membrane bioreactor treatment systems are presented and discussed.  5.1 Whitewater Characteristics Due to the fact that closed or partially closed integrated TMP-newsprint mills do not exist at present, a simulated whitewater representative of a low water use process was developed for use in this research.  The simulated whitewater was prepared to emulate contaminant  concentrations for an integrated TMP newsprint mill with a totalfreshwater consumption of 2 - 5 m /adt (Wearing et al, 1985b). Several authors have performed experiments to determine 3  the composition of such a whitewater (Jarvinen et al, 1985; Lagace et al, 1996; Francis, 1996b). In general, closure or partial closure of an integrated TMP whitewater system would result in an increase in suspended solids, dissolved and colloidal solids, lignin and temperature, and a decrease in dissolved oxygen (Pietschker, 1996).  The whitewater used in this present research was prepared by augmenting a whitewater from a coastal TMP mill, derivedfroma 45% hembal (hemlock balsam composite) and 55% spruce furnish, with plug screw feeder pressate from the same mill and 35% w/w evaporator bottoms from a closed BCTMP mill as described in section 4.2.3.  The characteristics of this  whitewater following screening through a 4 mm mesh screen, are given in Table 5-1. The composition of the whitewater varied over the course of the experiment as a result of the varying composition of the feed stocks and natural variation in the source materials. Whitewater was collected from a saveall, in which solids were able to settle from the 87  whitewater. Depending on the time of collection, and the degree of settling which had occurred in the saveall, the composition of the whitewater was variable.  Table 5-1: Composition of Synthetic Whitewater Contaminant  Mean  pH Total Solids (mg/L) Dissolved Solids (mg/L) Suspended Solids (mg/L) TCOD (mg/L) Dissolved COD (mg/L) Resin Acids (mg/L) Fatty Acids (mg/L) Cationic Demand (mg/L) UV Lignin (g/L)  5.67 5125 4640 488 5420 4140 23.4 43.4 0.077 1.05  Standard Deviation 446 270 312 915 500  0.014 0.09  5.2 System Characterization  5.2.1 Initial Membrane Flux The initial permeate flux of the 500 Angstrom Membralox Tl-70 filter was measured by filtering tap water through the membrane at a transmembrane pressure of 138 kPa (20 psi) and a recirculation rate of 10 L/min. This corresponded to a velocity across the membrane surface of 4 m/s at an operating temperature of 55°C. The tap water flux prior to "conditioning" (first use) was determined to be 1300 L/(m »hr), decreasing to 550 L/(m «hr) following several 2  2  weeks of operation prior to commencement of the experimental period.  88  5.3 Comparison of MBR and UF System Performance  5.3.1 Operating Parameters Two operational parameters which were independently controlled for this experiment were temperature and transmembrane pressure. Both of these parameters can greatly influence the performance of the biological and filtration systems and were held as constant as possible.  The transmembrane pressure in each of the reactors is presented in Figure 5-1 and Figure 5-2. The two systems were operated under similar and stable conditions at 138 kPa (20 psi). Variations in the transmembrane pressure were controlled by adjusting the outlet valve for the ceramic membrane. The drop in transmembrane pressure in the MBR from days 42 - 53 was due to operational difficulties which required that the pressure be lowered for that period of time. 25  0-1  1 ~  :  1 (N  =  1  1  1  ,  *t  U->  *0  t—  1  h  O  O  O  Day  Figure 5-1: Transmembrane Pressure in the Membrane Bioreactor System  89  Figure 5-2: Transmembrane Pressure in the Ultrafiltration System  Temperature in each of the reactors over the experimental period is plotted in Figure 5-3 and Figure 5-4.  Periods of low operating temperature were a consequence of occasional  operating difficulties resulting in a temperature decline in the water bath or a stopping or slowing of one or both of the positive displacement recirculation pumps. 65  rees  c oc 3,  59 57 55  3 53  1 a. i  51 49 47 45  Day  Figure 5-3: Operating Temperature in the Membrane Bioreactor System  90  65 j 63 -• 61 -  4 7 -45  J *0  1 <N  1  1  OO  OO 0\  1 ^  1 ^t*l  h *0  Day  Figure 5-4: Operating Temperature in the Ultrafiltration System  5.3.2 Contaminant Removal In this section the concentrations of each contaminant in the influent (both total and dissolved, where applicable), and the effluents of the MBR and UF treatment systems over each experimental period are presented along with the statistical mean percent removal, with 90% confidence interval bars for each contaminant of interest at the different water recovery fractions.  5.3.2.1 Solids Figure 5-5 and Figure 5-6 present the solids concentrations over the course of the experimental period. Influent Total and Influent Dissolved refer to solids concentrations in the influent, while MBR and UF refer to the solids concentration in each of the permeates.  91  8000  |  3000 2000 1000 0  Day -•—Influent Total  - Influent Dissolved — • — MBR  Figure 5-5 : Solids Concentration in the Membrane Bioreactor System as a Function of Time  6000  <*> 2000  1000 +  Day -•—Influent total  - Influent Dissolved •  -UF  Figure 5-6: Solids Concentration in the Ultrafiltration System as a function of Time  The concentration of solids in the influent and each of the effluents was highly variable, suggesting that the degree to which the treatment systems were able to remove solids was  92  partly a function of the influent solids concentration, particularly in the case of the MBR system.  Figure 5-7, Figure 5-8, Figure 5-9 and Figure 5-10 show the average performance of each system for the removal of total and dissolved solids respectively.  Removal of total solids in the membrane bioreactor was between 34% and 29% (Figure 5-7) and decreased with increasing water recovery fraction, while removal of total solids in the ultrafiltration treatment system (Figure 5-8) was poor and remained relatively insensitive to the experimental conditions. These results suggest that capability of the ultrafiltration system for removal of total solids was not greatly affected by volume reduction factor, and was more likely a function of membrane pore size. 100 90 80 70 H  emo'  s  60 50  CA e 40 u u  Ch  30 20 10 0  -I  1  0.9  1  0.95  1  0.975  0.983  Water Recovery fraction  Figure 5-7: Total Solids Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction  93  Figure 5-8: Total Solids Removal in the Ultrafiltration System as a Function of Water Recovery Fraction In each system, the removal of suspended solids was 100%, as the pore size of the ceramic membrane (500 Angstroms) was smaller than the filter pore size (1450 Angstroms) used in the determination of suspended solids. Removal of dissolved solids was poor in both treatment systems, although as in the case of total solids removal, there was a decline in removal efficiency in the membrane biological reactor with increasing water recovery fraction (shorter HRT).  Figure 5-9: Dissolved Solids Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 94  Figure 5-10: Dissolved Solids Removal in the Ultrafiltration System as a Function of Water Recovery Fraction 5.3.2.2 Chemical Oxygen Demand  12000  Figure 5-11: Chemical Oxygen Demand (COD) Concentration in the Membrane Bioreactor System as a Function of Time  Figure 5-11 and Figure 5-12 show the variation in chemical oxygen demand in the influent (total and dissolved) and in the permeate of the M B R and UF. As was the case with solids,  95  the concentrations of total and dissolved chemical oxygen demand in the influent were highly variable. In the case of the permeate from each of the treatment systems, however, the concentration of chemical oxygen demand in the effluent samples appeared to be more consistent than in the case of solids.  7000  Figure 5-12: Chemical Oxygen Demand (COD) Concentrations in the Ultrafiltration System as a Function of Time  Removal of total chemical oxygen demand (Figure 5-13) by the membrane biological reactor ranged from 54% to 48%, and the removal efficiencies in the system decreased with increasing water recovery fraction. This corresponds to a decreased removal of total chemical oxygen demand with decreased hydraulic residence time (from one day to eight hours). Improved removals of COD (95 - 99%) by aerobic membrane bioreactor systems treating other industrial (car manufacturing; metal transformation; dairy production) wastewaters have been reported by a number of authors (Hare et al, 1990; Zaloum et al, 1994; Zaloum et al, 1996)  96  as well as complete (99.9%) removal of COD from a municipal wastewater by aerobic membrane biological treatment (Trouve et al, 1994).  Lower removal efficiencies for COD in the present research may be attributed to the large non-degradable COD fraction in this stream (refer to section 5.4.2), the short retention times of the treatment system and the large pore size of the membrane relative to organic macromolecules.  Figure 5-13: Total Chemical Oxygen Demand (TCOD) Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction  In the ultrafiltration system, the removal of chemical oxygen demand ranged from 36% to 23%. In the case of the UF system, however, removal efficiency appeared to increase with increasing water recovery fraction (Figure 5-14). One possible explanation for this result is an increased thickness of the gel layer with increased concentration of the retentate (i.e. under increased water recoveryfractions).The thickness of the gel layer on the membrane surface would result in an increased selectivity of the membrane and an improved removal of insoluble  97  contaminants.  Another possible explanation for the increased removal of total chemical  oxygen demand at higher water recovery fractions, would be the precipitation of some components of total chemical oxygen demand in the retentate at higher water recovery fractions.  Figure 5-14: Total Chemical Oxygen Demand (TCOD) Removal in the Ultrafiltration System as a Function of Water recovery Fraction  Nuortila-Jokinen et al. (1995) reported that they observed improved percent removals of COD with increasing concentration of COD in the retentate (as in the case of increasing water recoveryfractions)when treating a papermill Whitewater by ultrafiltration.  Removal of dissolved chemical oxygen demand (Figure 5-15) ranged from 45-25% in the MBR, and -6 - 18% in the UF system (Figure 5-16). It is possible that in the case of the UF system, some insoluble COD was being converted into dissolved COD through of anaerobic biodegradation at a water recoveryfractionof 0.9, the final experimental run, leading to an apparent increase in dissolved COD over the experimental period.  98  100  80  o o u Q  60  1 o E &  I  40  I  5  20  0.9  0.95  0.975 Water Recovery  0.983  fraction  Figure 5-15: Dissolved Chemical Oxygen Demand (DCOD) Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction  Figure 5-16: Dissolved Chemical Oxygen Demand (DCOD) Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  5.3.2.3 Resin and Fatty Acids Figure 5-17 shows the concentration of resin acids in the influent and M B R and U F permeates, while Figure 5-18 shows fatty acid concentrations.. The concentrations of resin 99  and fatty acids in the influent were very high for run 1, at which time only the membrane bioreactor was operational. Following run 1, the concentrations of both resin and fatty acids decreased (presumably as a result of the changing composition of furnish in the TMPnewsprint mill), and remained relatively stable for the remainder of the experiment.  70  100  120  — 140  160  180  Day - Influent  — « — MBR  -UF  Figure 5-17: Resin Acid Concentration  140 120  Q 1320  40  60  80  100  120  Day -•—Influent — • — M B R  Figure 5-18: Fatty Acid Concentration 100  -UF  140  160  180  Figure 5-19 and Figure 5-20 illustrate the removal of resin acids by each of the treatment systems. The ultrafiltration system demonstrated superior removal of these compounds in all experimental runs, with removal efficiencies ranging from 99- 93%.  The most complete  removal of resin acids occurred at the lowest water recovery fraction, 0.9. Zaidi and Buisson (1991) found that resin acids existed as calcium salts in the retentate of UF systems, and as such may be rejected both by steric exclusion (as a result of being adsorbed onto suspended solids) and solute/membrane interaction.  The removal of resin acids by the MBR rangedfrom52 - 76%, with the removal of resin acids being most pronounced at the highest water recovery fraction. The difference between the two systems may be explained on the basis of the different pH's in each of the operating systems. The pH in the ultrafiltration system was in the range of 5.2 - 5.5 while the pH of the MBR system was in the range of 6.8 - 7.5.  Figure 5-19: Resin Acid Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction 101  The solubility of most resin acids is at a maximum at pH's greater than 7, such that in the pH range of the MBR, a substantial portion of the resin acids would have been soluble and therefore able to pass through the membrane (unlike the colloidal resin acids retained in the UF system). Removal of resin and fatty acids from solution is facilitated by the agglomeration of colloidal resin and fatty acids onto larger macromolecules, (or onto each other) to form pitch deposits. These pitch deposits arefilterablefrom solution, though the individual resin and fatty acid molecules are able to pass through a 500 Angstrom filter (Zaidi and Buisson, 1991).  100  •  ~  g—  80 -•  60 -  40  20 ••  0  -I  1  0.9  1  0.95  1  0.975  0.983  Water Recovery fraction  Figure 5-20: Resin Acid Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  Fatty acids molecules are considered to be among the most detrimental, as they are more readily able to form larger, filterable pitch deposits (Welkener et al, 1993).  This would  account for the near complete removal of fatty acids in both treatment systems (Figure 5-21 and Figure 5-22).  102  Figure 5-21: Fatty Acid Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction  Figure 5-22: Fatty Acid Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  Removal of resin and fatty acids from the influent stream may also have been a result of the formation of a colloidal "gel layer" of RFAs along the surface of the membrane. This surface layer would promotefiltrationof RFAs from solution by two mechanisms: one, the gel layer  103  would serve as a more selective membrane surface through which agglomerated resin and fatty acids were unable to pass, and two, the gel layer may have induced an electrostatic repulsion which prevented the permeation of agglomerated and individual molecules of resin and fatty acids, and their salts into the effluent stream.  In the UF system at low water recovery fractions, the flux was relatively high and the rate of fouling was low (sections 5.3.3.1 and 5.3.3.2) such that cleaning was required only infrequently.  The long period of time between cleanings would have allowed for a full  development of a gel layer. At higher water recovery fractions, the rate of permeation was considerably lower, and the rate of fouling increased, such that cleaning frequencies were also higher. This frequent cleaning would have prevented the formation of a membrane surface layer of resin and fatty acids, and allowed for the permeation of a greater fraction of RFAs.  Removal of resin acids in the membrane biological reactor was considerably poorer than in the UF system, and was most likely attributable to the difference in system pH, as discussed earlier. Unlike the UF system, resin acid removal appeared to improve in the MBR with increasing water recovery fraction. This suggests that there may have been some biologicallymediated interactions involved in the removal of resin acids in the MBR, such as adsorption of resin acids onto the surface of biological solids (Hall and Liver, 1996) or biological degradation of resin acids (Liu et al, 1993b). In the MBR system, the rate of fouling of the membrane was lower with increasing water recovery fraction (section 5.3.3.2) and as such, required less frequent cleanings, possibly allowing for a build up of a gel layer of resinous materials on the membrane over time.  104  5.3.2.4 Cationic Demand Figure 5-23 and Figure 5-24 present the concentrations of cationic demand in the influent, MBR and UF permeate streams over the course of the experimental period.  Cationic demand removal efficiencies are plotted in Figure 5-25 and Figure 5-26.  The  ultrafiltration system was very effective at removing cationic demandfromthe influent stream, with efficiencies ranging from 85 - 67%.  In general, the effectiveness of the UF system  decreased with increasing water recovery fraction.  0.12  0 -I '-'  1  1  00  «-H  CS  h *o  Day | — • — Influent — • — M B R ~ |  Figure 5-23: Cationic Demand Concentration in the Membrane bioreactor System as a Function of Time  Cationic demand removal efficiencies in the membrane bioreactor were not as high, ranging from 29 - 48 %. Unlike the ultrafiltration system, the MBR system appeared to exhibit improved removal of cationic demand with increasing water recovery fraction.  105  Figure 5-24: Cationic Demand Concentrations in the Ultrafiltration System as a Function of Time  Figure 5-25: Cationic Demand Removal for the Membrane Bioreactor System as a Function of Water Recovery Fraction  Cationic demand, or "anionic trash" is composed primarily of small, negatively charged polysaccharides (Reside, 1996), which, in the case of the MBR may have actually been produced during hydrolysis of larger polysaccharides, or during cell lysis (Chaize and Huyard,  106  1991). The increased removal of cationic demand in the MBR at a water recovery fraction of 0.983 would likely have been a result of the shorter hydraulic residence time resulting in lower overall biological degradation and hydrolysis.  100 90  J  T3 B  80 \  |  70 --  I  50 --  1  40  E (2  30  s  20  CQ  a •1  i  60-  10 0 0.9  0.95  0.975  0.983  Water Recovery fraction  Figure 5-26: Cationic Demand in the Ultrafiltration System as a Function of Water Recovery Fraction  5.3.2.5 UV-lignin The concentrations of UV-lignin in both the influent and the permeates from the MBR and UF treatment systems appeared to be highly variable over the course of the entire experimental period (Figure 5-27 and Figure 5-28). This may have resulted from variations in wood furnish as evidenced by high variation in the concentrations of total and dissolved solids, and COD.  Removal efficiencies for UV-lignin (205 ran) are presented in Figure 5-29 and Figure 5-30. UV-lignin concentration was determined by a procedure involving the acidification, filtration and dilution of samples, and measurement of the absorbance at 205 nm. In the samples from the UF system, UV-lignin was not removed at any water recovery fraction, and UV-lignin  107  appeared to increase in UF-treated whitewater at water recoveryfractionsof 0.9 and 0.983. This increase may be a result of absorbance by other components in the UF-treated effluent.  Figure 5-27: UV-Lignin Concentration in the Membrane Bioreactor System as a Function of Time  Figure 5-28: UV-Lignin Concentration in the Ultrafiltration System as a Function of Time  108  100  80  60  S  40  as ft" 20  0.9  0.95  0.975 Water Recovery  0.983  fraction  Figure 5-29: UV-Iignin Removal in the Membrane Bioreactor System as a Function of Water Recovery Fraction  Figure 5-30: UV-lignin Removal in the Ultrafiltration System as a Function of Water Recovery Fraction  A small amount of UV-lignin was removed in the whitewater treated by the MBR system, rangingfrom8 - 12%. Improved removal efficiencies were observed at lower water recovery fractions (longer hydraulic residence times).  Dufresne et al. (1996) demonstrated an  accumulation of lignin in the reactor contents of an MBR system operating in parallel to an  109  activated sludge system, which did not exhibit a similar accumulation. These results indicate poor biodegradability of lignin in an aerobic MBR.  5.3.3 Permeate Flux As discussed in chapter two, a variety of factors control the flux through an ultrafiltration membrane.  Figure 5-31 presents the flux through each of the membranes used in this  experiment over the course of the entire experimental period.  5.3.3.1 Maximum Flux  Day I •  MBR  O UF~  Figure 5-31: Permeate Flux in the Membrane Bioreactor and the Ultrafiltration System over the Experimental Period  Maximum attainable flux and the rate of loss of flux are two important parameters in the determination of the feasibility of an ultrafiltration system. Paleologou et. al (1994) suggested that a flux of at least 140 L/(m »hr) must be maintained to make ultrafiltration a viable 2  economic alternative to vapor recompression evaporation or freeze crystallization for treatment of pulp and paper effluents for reuse within the mill. Maximum flux and loss of flux  110  are a function of properties of both the filter and the solution (solute and solvent)being filtered. The contributing properties of thefilterinclude pore size, pore size distribution and the electrostatic nature of the surface of the membrane (Dufresne et al, 1996). In addition, UF operational parameters such as the velocity through the membrane and transmembrane pressure are important.  The contributing properties of the solution include viscosity,  molecular size and distribution, pH, temperature, mineral salt, protein and lipid content (Cheryan, 1986).  Figure 5-32 is a plot of the maximum flux recorded in the MBR and UF treatment systems at each of the experimentally imposed water recovery fractions. The maximum flux was always observed immediately following cleaning of thefilter,presumably due to the unclogging of the filter pores during the cleaning process.  Cleaning was performed as necessary and varied  between once per run and five times per run.  During periods of acclimatization between runs, each of the systems at times exhibited fluxes higher than those reported in Figure 5-32, but those were not observed under experimental conditions.  Maximal flux was attained in the ultrafiltration system under conditions of low loading (low water recovery fraction) and declined sharply with increasing water recovery fraction. Reported fluxes for ultrafiltration applications of mechanical newsprint Whitewaters are in the range of 54 -62 L/(m «hr) (Nystrom et al, 1992; Nuortila-Jokinen et al, 1995; Nuortila2  Jokinen et al, 1993b). The higher fluxes found in this present research may be a result of the  ill  larger pore size (500 Angstroms), narrow pore size distribution and low fouling potential for ceramic membranes.  Ekengren et al. (1993), in their examination of the ultrafiltration of bleach plant effluents, reported that the maximum attainable flux through a particular filter decreased with increasing volume reduction fraction, and that the rate of decrease increased with increasing volume reduction factor, similar to the findings in the present study.  a S  a  s  a  200 180-1 160 140 120 100 80 60 40 20 0  •  MBR  HI U F  0.9  0.95  0.975  W ater Recovery Fraction  0.983 (Y)  Figure 5-32: Maximum Flux Flux in the MBR also decreased with increasing water recovery fraction, but not to the same degree. The build up of pitch and other resinous materials may have been responsible for the sharp decline in flux in the ultrafiltration system, as was apparent from a visual observation of the reactor contents, while in the MBR the decline in flux was more likely attributable to the increase in suspended solids (as is apparent in Figure 5-5), primarily of biological origin  112  (Magara and Itoh, 1991) and the deposition of hydrolysis products and inorganic precipitates as detailed in Chapter 2.  5.3.3.2 Rate of Fouling Membrane flux is associated with three resistances: Rm - the intrinsic resistance associated with a particular membrane; Rp - the plugging of membrane pores and adsorption of effluent components onto the walls of the membrane, responsible for the initial decrease in flux (Ramamurthy et al, 1995) and; Rc - the resistance associated with the accumulation of material on the surface of the membrane due to concentration polarization and consolidation of an accumulated cake, also referred to as "fouling". Choo and Lee (1996) determined that for the treatment of an alcohol distillery wastewater by a membrane coupled anaerobic bioreactor (MCAB) these contributed 0.5%, 16.6% and 82.8% to the loss of flux, respectively.  Similar findings have been reported by a number of authors - that is, flux is  limited almost exclusively by Rc (Shimizu et al, 1993). Fouling of an ultrafiltration membrane is primarily attributable to the accumulation of colloidal particles in the size range of 0.1 - 1 um (Ramamurthy et al, 1995). Deposition of these colloidal particles is controlled by several factors including cross flow velocity (the velocity of the retentate across the surface of the membrane) (Pejot and Pelayo, 1993), concentration of nutrients in solution (Choo and Lee, 1996) and presence of larger macromolecules in solution (Upton et al, 1997).  Figure 5-33 indicates the operating time over which a 20% loss of flux occurred in each of the experimental runs. Cleaning was performed as required to maintain sufficient flux through the system: The "set point" flux was different for each experimental run, and was determined by the hydraulic residence time in the reactor. A 20% reduction of the original (post cleaning) 113  maximal flux was chosen as a reference point to demonstrate differences in the rate of filter fouling in each treatment system, an arbitrary reference point which has been used by other authors (Pejot and Pelayo, 1993, Ramamurthy et al, 1995).  In the ultrafiltration system studied here, fouling was most likely controlled by the concentration of colloidal particles in the liquid being filtered - as the concentration of colloidal materials in the retentate increased (as with increasing water recovery fraction) the rate of fouling sharply increased.  200 180  o  e  c o  "•8 3 ©  u  a s  160  n  140 120  •  100  •  80  MBR UF  60 40 20 0 0.9  0.95  0.975  0.983  W ater Recovery Fraction (Y) Figure 5-33: Time for a 20% Reduction in Permeate Flux in the Membrane Bioreactor and Ultrafiltration Systems as a Function of Water Recovery Fraction  In the case of the membrane bioreactor, fouling of the membrane surface was likely caused by a number of factors, including: inorganic precipitation of phosphorus compounds (e.g. struvite MgNFLjPC^ • 6H 0); extracellular matrix excreted by certain bacteria in the mixed liquor 2  (Fane et al, 1994; Hodgson and Fane, 1992) and granular cell material (e.g. glycogen and cell  114  wall fragments) released during cell lysis resulting from shear stresses induced by pumping (Shimizu etal, 1994).  The rate of fouling significantly decreased with increasing water recovery fraction, suggesting that these factors played a less significant role as the hydraulic residence time was decreased (and the concentration of mixed liquor volatile suspended solids increased), possibly due to changing composition of the mixed microbial culture.  5.3.4 Characteristics of Retentate Suspended solids (SS) and mixed liquor suspended solids concentrations were estimated in two different ways. In thefirstcase, the dissolved solids were subtracted from the total solids and in the second case (demarked with an asterisk) the average total solids in the effluent (which was equivalent to the dissolved solids in the effluent) were subtracted from the total solids in the retentate. It was noted that biomass was able to pass through thefilterused for the determination of suspended solids in this experiment, such that the traditional procedure used for the determination of MLVSS concentration, as a measure of biomass, was inaccurate.  Table 5-2 and Table 5-3 present the characteristics of the concentrate in the MBR treatment system for each of the experimental conditions. All values were rounded to the nearest 5 mg/L.  115  Table 5-2: Characteristics of the MBR Retentate (pt. I) Y  TS VDS VS TDS SS* MLVSS MLVSS* SS mg/L mg/L mg/L mg/L mg/L mg/L mg/L mg/L 0.95 17675 12280 13460 8485 4220 14460 3795 13010 0.975 27585 20910 15625 10015 11960 23870 10890 21735 0.983 31470 25425 23545 18045 7930 27820 7380 25885 (asterisk (*) refers to calculation of suspended solids by means of subtracting permeate solids from total solids - see explanation previous) SS* = Suspended Solids (TS - MBR Solids) MLVSS* = SS* * (VS/TS)  MLVSS* concentrations in the MBR system appeared to increase substantially with lower HRT, while MLVSS concentrations did not. MLVSS* appears to be a better indication of active biomass, based on its dependence to hydraulic residence time.  Table 5-3 presents the chemical oxygen demand and the resin and fatty acid concentrations in the MBR retentate. Chemical oxygen demand appeared to accumulate to a greater extent than resin and fatty acids in the MBR with increasing water recovery fraction. This indicates a greater degree of degradation of resin and fatty acids than COD at short hydraulic residence times. Table 5-3: Characteristics of the MBR Retentate (pt. n) Y 0.95 0.975 0.983  COD mg/L 25425 44770 52655  Resin Acids mg/L 225 410 590  Fatty Acids RFA mg/L mg/L 270 595 365 775 490 1080  Table 5-4 and Table 5-5 present the equivalent information for the ultrafiltration system.  116  Table 5-4: Characteristics of the UF Retentate (pt. I) Y  TS  mg/L 0.9 12690 0.95 16795 0.983 29030  VS  TDS  VDS  SS  SS*  mg/L 9306 12635 24580  mg/L 10490 13580 21800  mg/L 7380 9555 17730  mg/L 2204 3215 7230  mg/L 8710 13090 24990  MLVS c mg/L 1930 3080 6855  MLVSS* mg/L 7620 12430 23680  Solids concentrations in the UF system were generally lower than in the MBR system, where a greater proportion of the solids entering the reactor were retained in the system, and biomass growth would account for the retention of contaminants as biological solids. Table 5-5: Characteristics of the UF Retentate (pt. U) Y  COD mg/L 0.9 19420 0.95 20523 0.983 48325  Resin Acids mg/L 431 538 1274  Fatty Acids RFA mg/L mg/L 384 515 650 1288 1421 2695  Similarly, the Chemical Oxygen Demand of the concentrate in the MBR system was found to be higher than that of the UF system, as a result of the higher retention of particulate COD by the MBR and the higher solids (biomass and influent) concentration in the MBR.  Resin and fatty acid concentrations were markedly higher in the UF system, most likely a result of two factors. A greater fraction of RFA were retained by the UF system (and would be present in the concentrate), and the biological oxidation of resin and fatty acids within the membrane biological reactor would result in lower concentrations in the MBR retentate.  117  Some deposition of contaminants was evident on the walls of each of the treatment systems resulting in some operational difficulties (sticking of floats and fouling of membranes). In the MBR system, these deposits were dark brown in color, and would often float on the surface of the reactor contents, while in the UF system, the deposits were primarily on the walls of the reactor and were light brown in color.  5.3.5 Solids Mass Balance Figure 5-34 and Figure 5-35 present cumulative solids mass balance data for each of the treatment systems. Cumulative mass balances were determined by calculation of mass flow rates of solids entering the systems (via the influent) and leaving the system (via the effluent and the concentrate wasting) plus the mass of solids retained in the system.  Sampling for  chemical analysis was always performed from material already being wasted, such that it did not contribute to solids loss. In both systems, some fraction of solids was unaccounted for in the balance.  Total solids out of the system was calculated using the following equation: Total Solids out (g) = Permeate Solids (g) + MBR Solids (g)  (51)  Figure 5-34 indicates that not all solids were accounted for in the balance - i.e. The Total Solids out (g) was always less than the Total Solids in(g), indicating that some solids were destroyed in the MBR system.  118  In the case of the MBR system, solids could have left the system by two mechanisms: deposition as particulate matter on the walls and bottom of the reactor; and destruction by aerobic metabolism., although these were not accounted for in the balance, nor were they measured  7000  6000  5000 -Total Solids in g -Disssolved Solids in i 5  -Total Solids out g  4000  - Permeate Solids g - M B R Solids g 3000  2000  Figure 5-34: Cumulative Solids Mass Flows: MBR, as a Function of Time  The complete biological oxidation of organic solids would result in the mineralization of solid material to final products of carbon dioxide and water. Measurements of the specific oxygen uptake rate (SOUR), which ranged from 1.38 - 2.00 mg 0 / (g MLVSS*»min) 2  over the  course of the experimental period indicated that aerobic respiration was occurring.  Tardif  (1996) reported SOUR values of 0.35 - 2.42 mg 0 / (g MLVSS**min) for a similar system. 2  119  6000  —•—Total Solids in g —•— Disssolved Solids in g —*—Total Solids out g — A — Permeate Solids g - * — UF Solids g  59  79  99  119  139  159  179  Day  Figure 5-35: Cumulative Solids Mass Flows: UF, as a Function of Time  Figure 5-35 indicates that the mass balance discrepancy for solids was greater in the case of the ultrafiltration system than for the MBR. As was the case with the MBR, abiotic solids loss was likely attributable to precipitation and deposition. As noted earlier, significant deposition was evident in the UF system.  These depositions were not measured in the solids mass  balance, and deposits were allowed to accumulate over the course of the experiment.  The solids mass balance in the ultrafiltration system shows no change from day 125 to day 140 as the ultrafiltration system was taken offline, and feeding was ceased.  120  An additional loss of solids in the UF system may have occurred as a result of anaerobic biological activity, since no aeration was provided. The concentration of anaerobes in closed whitewater systems has been reported to be extremely high, and was attributed to high concentrations of organic material and to environmental conditions ideally suited to anaerobic biological growth. The presence of anaerobes in whitewater systems has been linked to operational difficulties, corrosion and problems with paper quality in closed mills (Gudlauski, 1996).  5.4 Biological Activity in the MBR  5.4.1 MLVSS Mixed liquor volatile suspended solids (MLVSS) concentrations were calculated in two fashions for the purpose of this experiment (MLVSS, and MLVSS*) as discussed in section 5.3.4. As reported in Section 5.3.4, some biomass was unaccounted for in the protocol used for the determination of MLVSS. MLVSS*, however, accounted for all biomass present in the mixed liquor samples.  decreased hydraulic residence time, as predicted by Monod first order kinetics. Figure 5-37 presents the variation of MLVSS* concentration in the MBR observed over the course of the experiment.  Two  of the primary operating advantages of the membrane biological reactor over  conventional biological treatment are the complete retention of biosolids and the ability to  121  operate at high concentrations of MLVSS - allowing for higher loading rates, and lower food-to-microorganism ratios.  30000 25000 "I* 20000 aT 15000  > J  10000 5000 00.3  0.4  0.5  0.6 0.7 HRT  0.8  0.9  1  + — MLVSS* - • — MLVSS  Figure 5-36: MLVSS and MLVSS* Concentrations in the Membrane Bioreactor as a Function of HRT  g  20000  g  15000  S  10000 5000 -J 0  79  61  Day  Figure 5-37: MLVSS * Concentrations in the MBR as a Function of Time  122  112  5.4.2 Food to Microorganism Ratio The food-to-microorganism (F/M) ratio is a parameter used in the design and operation of activated sludge systems. Strict control of the food-to-microorganism ratio is important in determination of the type of microorganisms which thrive within a mixed microbial culture and for the prevention of such problematic occurrences as sludge bulking (Metcalf & Eddy Inc., 1991).  The F to M ratio is calculated by the following equation:  JL= A . M  (5.2)  0X  where: F/M = food-to-microorganism ratio (d") 1  9 = HRT (d) X = MLVSS* concentration (mg/L)  For the MBR, the substrate was considered to be the biodegradable chemical oxygen demand (BCOD).  In order to determine whatfractionof the Whitewater COD was biodegradable at 55 °C, a modified BOD test was performed. 5  123  The average concentration of COD from a triplicate series of batch biodegradation tests containing Whitewater, nutrients and biomass (at a concentration of 2000 mg/L) was determined and plotted as a function of incubation time.  The 5 day consumption of  biodegradable COD (BCOD) was plotted and determined to represent approximately 58% of the COD (Figure 5-38).  12000 10000 8000  o o u  6000 4000 2000 0 0  2  3  Tim e (days) Figure 5-38: Determination of BCOD (mg/L) in the Membrane Bioreactor  Determination of the F/M ratio for 5 day biodegradable COD was as follows:  F  F (BCOD) = 0.58  M  *  (5.3)  (COD)  M  Table 5-6 presents the F/M (COD) and F/M (BCOD) for each of the three experimental runs in the MBR.  124  Table 5-6: F / M Ratios Y 0.95 0.975 0.983  HRT (d) F/M COD (d ) F/M BCOD (d") 1 0.388 0.225 0.50 0.539 0.313 0.33 0.665 0.386 1  1  Typical values for a complete mix activated sludge system are 0.2 - 0.6 mg BOD /(mg 5  MLVSS* d) (Metcalf & Eddy Inc., 1991). One of the primary advantages of an MBR system #  over activated sludge is the ability to maintain a low F/M ratio under high loading rates, thus minimizing sludge yield (Chiemchaisri and Yamamoto, 1994). The MBR studied in this experiment exhibited F/M ratios ranging from 0.2-0.39, lower than those recommended for activated sludge systems.  5.5 Effect of VRF on Operation of the UF System One of the objectives of this study was to examine the behavior of an ultrafiltration system operating in a continuous mode over a range of volume reduction factors (VRF). Ultrafiltration systems normally operate at volume reduction factors in the range of 15-20 (Pejot and Pelayo, 1993), and filtration is often performed as a batch operation. At low volume reduction factors the flux through thefiltersis high, and fouling is kept to a minimum.  In the present study, the operation of the ultrafiltration system in continuous mode at VRF 10, 20 and 60 yielded the following observations. •  Contaminant removal efficiency was only minimally affected by the VRF. Removal of total solids, total COD and dissolved COD was improved with increasing VRF, resin acid, and fatty acid removal decreased slightly with increasing VRF.  125  •  Removal of cationic demand markedly decreased with increasing VRF. As discussed in Section 5.3.2.4, this may have been a result of anaerobic microbial activity resulting in the production of anionic trash at the higher volume reduction factors.  •  Maximum flux decreased almost linearly with increasing volume reduction factor. At volume reduction factors of 10 and 20, the UF flux was high enough to be considered an economically viable treatment option (Pejot and Pelayo, 1993).  •  The time for a 20% loss of flux decreased almost exponentially with increasing volume reduction factor. At a VRF of 60, the effects of fouling were evident very quickly, and a 20% loss was apparent in less than 48 hours. Other authors have reported similar findings (Pejot and Pelayo, 1993; Ekengren etal., 1993).  •  Operation of the UF system at a volume reduction factor of 60 was not possible and was abandoned prior to completion of the run due to the inability to maintain an adequate flux through the filter without daily cleanings.  Operation of an ultrafiltration system at high volume reduction factors would be preferable since smaller volumes of concentrate would require disposal. At a VRF of 60, however, this advantage is offset by the requirement for frequent cleaning and high costs associated with downtime as a result of the high rate of fouling rate. Based on the results from this study, it would appear that the ideal operating capacity for the UF system is at a VRF of 20.  5.6 Comparison to Other Research The findings in this study indicate that the design criteria for the MBR and UF systems, when operated under ideal conditions, would be quite different. The MBR system, although not  126  optimized in this study (it may have been feasible to operate at even lower HRTs) appeared to operate best under a VRF of 60- corresponding to a long SRT and a short HRT while the UF system appeared to operate best at a VRF of approximately 20. This difference in optimal VRF's would result in dramatically different design criteria, with the mixing tank (reactor) of the MBR system being approximately one third the size of that of the UF system, and the UF system producing three times the concentrate requiring disposal. The MBR, however, would require additional equipment (such as nutrient addition and aeration systems) not required by the UF system, increasing the capital and operating costs associated with this treatment system.  Optimal operating conditions for an MBR would differ substantially from the optimal operating conditions for a UF system. Table 5-7 presents a comparison of the two systems. Confidence intervals (90%) are presented in brackets following each percentage removal value.  The resultsfromthis suggest that operation of a membrane bioreactor appears to offer no real advantage over an ultrafilter alone for the treatment of low-water use integrated TMPnewsprint Whitewater.  The MBR did offer marginally improved removals of solids and  chemical oxygen demand, and a slight removal of short chained lignins, but the UF system exhibited fewer operational difficulties, lower rate of fouling, and exhibited higher removal efficiencies for both resin acids and cationic demand.  127  Table 5-7: Comparison of Optimal Operating Conditions Parameter  MBR System  UF System  VRF  60  20  Water Recovery Fraction (Y)  0.983  0.950  Fraction Concentrate (requiring treatment/disposal)  0.017  0.050  HRT (days)  0.33  1  SRT (days)  20  20  Maximum Flux (L/(m »hr)  164  164  Time for 20% loss of flux (hrs)  110  170  Removal of total solids (%)  28.8 (30.4-27.1)  23.3 (24.9-21.6)  Removal of Dissolved Solids (%)  21.5 (23.3-19.7)  17.8 (18.9-16.5)  Removal of COD (%)  48.3 (50.8-45.9)  31.8 (34.2-29.4)  Removal of Dissolved COD (%)  34.2(37.4-31.0)  3.7(13.8-(-6.4))  Removal of RA (%)  68.0 (76.2-59.9)  95.3 (100-89.7)  Removal of FA (%)  99.0 (99.1-98.8)  98.7 (99.2-98.2)  Removal of Cationic Demand (%)  47.9(52.8-43.0)  74.2 (79.4-68.9)  Removal of UV- Lignin (%)  7.21 (10.0-4.4)  -1.2(2.9-(-5.4))  2  The conclusion that the MBR system offered no particular advantage over an UF system is specific to this particular study. Different operating conditions, such as lower temperatures and lower hydraulic residence times, or the use of a membrane with a smaller pore size or a hollow-fiber type membrane system would likely improve the performance of the MBR system.  Additional research into the treatment of a minimum effluent TMP-newsprint  whitewater could include the examination of the use of a hollowfiberMBR.  128  6. CONCLUSIONS This chapter summarizes the findings of this thesis and the research to date on treatment options for a minimum effluent integrated TMP-newsprint Whitewater.  A summary of the current literature on systems closure and fresh water minimization in a mechanical newsprint mill yielded the following findings regarding the composition of a minimum effluent Whitewater. •  The reduction of fresh water levels from current usage of 10-150 m /adt, to 2-5 m /adt, 3  3  will require the implementation of such practices as pulp washing and countercurrent flow. •  Closure or partial closure of an integrated mechanical newsprint mill would result in an increase in suspended solids, dissolved and colloidal solids, chemical oxygen demand, resin and fatty acids, lignin and temperature. A decrease in dissolved oxygen in the Whitewater would occur.  •  To simulate a minimum effluent mechanical newsprint Whitewater, TMP-newsprint wastewater streams which would comprise the Whitewater in a mechanical newsprint mill following fresh water use reductions should be used to produce a Whitewater containing higher levels of the aforementioned contaminants than an open mill Whitewater.  6.1 Comparison : MBR and UF Treatment of Minimum Effluent Whitewater 1. The MBR was found to be a relatively stable form of biological treatment at 55 °C but contaminant removals were generally lower than had been found in previous studies. Tardif (1996) using a membrane of nominal pore size of 0.08um was able to better  129  remove all contaminants of interest. Although the MBR was able to completely retain suspended solids, removal efficiencies for total and dissolved solids were only 34% and 28% respectively.  Maximum removal of other contaminants were as follows: total  chemical oxygen demand - 58%; dissolved chemical oxygen demand - 36%; resin acids 76%; fatty acids - 99%; cationic demand - 48%; and UV-lignin (205 nm) - 12%. 2. Solids, COD and UV-lignin removal efficiencies in the UF system were slightly lower than those in the MBR system. Removal efficiency ranges were as follows: total solids: 22 20 %, dissolved solids: 18 - 12%; total COD: 37 - 22%; dissolved COD: 14 - (-3)%, UVlignin: -1 - (-6)%. 3. Removals of resin and fatty acids and cationic demand in the UF treatment system were high: fatty acids: 100 - 93%; resin acids: 100 - 98%; cationic demand: 88 - 68%. 4. Maximum flux through the MBR was high (175-162 L/(m 'hr)) and was relatively stable 2  at hydraulic residence times of 0.33, 0.5 and 1 day, corresponding to volume reduction factors of 20, 40 and 60. 5. At low volume reduction factors, maximum flux through the UF system was very high 198 L/(m hr) at a VRF of 10, and 160 L/(m «hr) at a VRF of 20. Flux in the UF system 2  2  decreased linearly with increasing volume reduction factor. Maximum flux at a VRF of 60 was 118L/(m »hr). 2  6. Fouling of the UF filter in the MBR system was substantial - a 20% loss of flux was observed in 39 hours at an HRT of 1 day; but decreased with increasing volume reduction factors.  The time for a 20% loss of flux increased linearly with decreasing hydraulic  retention time. The rate of fouling of the UF filter in the ultrafiltration treatment system was highly dependent on volume reduction factor. At a low VRF (i.e. 10) fouling was  130  slow - 192 hours for a 20% loss of flux, but the time for fouling decreased exponentially with increasing volume reduction factor. 7. Retentate from the MBR system was higher in solids and COD concentrations than the retentate from the UF system, and lower in resin and fatty acids concentrations, when operated at the same VRF, perhaps making it easier to dispose of. 8. Some solids were destroyed in both the MBR and UF systems - most likely as a result of biological degradation and deposition on the walls and bottom of the reactor.  6.2 Conclusions: MBR Biokinetics 1. The MBR system was able to function at high concentrations of mixed liquor volatile suspended solids, up to 25,000 mg/L at an FfRT of 8 hours (0.33 days). 2. The imposed HRTs and SRTs used in this experiment produced F/M ratios in the MBR that were lower than typical values for a complete mix activated sludge.  This would  suggest that the use of an MBR could minimize sludge production.  6.3 Conclusions: Operation of a UF at Varying VRF 1. Most contaminant removal efficiencies were only minimally affected by the VRF - removal of total solids, total COD and dissolved COD was improved with increasing VRF, resin acid, and fatty acid removal decreased slightly with increasing VRF. 2. Removal of cationic demand decreased substantially with increasing VRF. This may have been a result of anaerobic microbial activity resulting in the production of anionic trash at the higher volume reduction factors.  131  3. Maximum flux decreased almost linearly with increasing volume reduction factor. At volume reduction factors of 10 and 20, the UF flux was high enough to be considered an economically viable treatment option. 4. The time for a 20% loss of flux decreased almost exponentially with increasing volume reduction factor. At a VRF of 60, the effects of fouling were evident very quickly, and a 20%) loss was apparent in less than 48 hours.  6.4 Most Viable Treatment Option Treatment alternatives for the purging of contaminants from a minimum effluent TMPnewsprint Whitewater which have been studied to date are: ultrafiltration (10-50 °C); sequencing batch reactor (SBR) at an HRT of 2 days (20-50 °C); ultrafiltration of the SBR effluent (20-40 °C); membrane bio-reactor treatment at HRTs of 0.7-2.8 days (40-55 °C); and a comparative parallel study of ultrafiltration and MBR treatment at HRTs of 0.33 - 1 day(s), VRFs of 10-60 at 55 °C.  A determination of the most appropriate technology requires analysis of the following factors: A. The removal capabilities of each system with respect to identified contaminants of interest; B. Time required for treatment (flow through time, or flux), which would determine the space and size requirements of a treatment system; and operational requirements and stability of each system.  The research to date examining potential contaminant purging treatment systems for a minimum effluent TMP-newsprint Whitewater, has yielded the conclusion that ultrafiltration of  132  the Whitewater to a volume reduction factor between 10 and 20 would be the most appropriate treatment technology for this application.  This research showed that when an MBR and UF treatment system were operated in parallel there were only marginal differences in contaminant removal, and in some cases the UF outperformed the MBR.  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