Abstracts of Oral Presentations Exhibitor & Sponsor Guide Schedule ...

International Ozone Association 

International Ultraviolet Association 

May 3-6, 2009 

Hyatt Regency Cambridge, Massachusetts 

Abstracts of 

Oral Presentations 

Exhibitor & Sponsor Guide 

Schedule of Events 

Thanks to our Primary Sponsor :

International Ultraviolet Association & International Ozone Association 

Conference Schedule at a Glance 

Boston - 2009 

Primary Conference Sponsor: ITT Water & Wastewater 

Saturday, May 2 nd , 2009 

NOON - 5 PM 

IOA & IUVA Committee Meetings 

NOON - 5 PM 

IUVA & IOA PAG Task Force Meetings 

Sunday, May 3 rd , 2009 

7:30 AM - 4:30 PM 

Ozone & UV Technology Workshops 

**see order forms for these standalone events** 

Sponsored and Organized By: AECOM 

www.io3a.org/boston2009/ozone_workshop.pdf 

www.io3a.org/boston2009/uv_workshop.pdf 

9 AM - NOON 

IOA PAG Board Meeting 

1:30 PM - 4:30 PM 

IUVA Board Meeting 

7 PM - 9 PM 

WELCOME ATTENDEES - 2009 Opening Reception 

Sponsored By: CDM 

Monday, May 4 th , 2009 

8:15 AM - 9:30 AM 

General Opening Session 

9:30 AM - 10:15 AM 

Coffee Break 

10:15 AM - 11:55 AM 

Session 1 - UV Validation 

Session 2 - UV Regulatory 

Session 3 - Ozone Design and Operation 

NOON - 1:15 PM 

Conference Luncheon 

Sponsored By: Ozonia North America 

1:15 PM - 2:55 PM 

Session 4 - UV Case Studies 

Session 5 - Ozone Case Studies 


2:55 PM - 3:40 PM 


3:40 PM - 5:20 PM 

Session 7 - UV Case Studies 

Session 8 - Ozone Case Studies 


5:30 PM - 7:30 PM 

SPRING FLING RECEPTION 

Please join us for refreshments & hors d'oeuvres 

as we celebrate springtime in Boston with our 

technical program speakers and exhibitors. 

Sponsored By: Black & Veatch 

and Hyatt Regency Cambridge 

Tuesday, May 5 th , 2009 

8:15 AM - 9:30 AM 

Session 10 - UV Disinfection Design 

Session 11 - Advanced Oxidation of Contaminants 

Session 12 - Perozone and AOP processes 

9:30 AM - 10:15 AM 


10:15 AM - 11:55 AM 

Session 13 - UV Disinfection Research 

Session 14 - Advanced Oxidation of Contaminants 

Session 15 - Perozone and AOP processes 

NOON - 1:15 PM 

Conference Luncheon 

Sponsored By: Fuji Electric 

1:15 PM - 2:55 PM 


Session 17 - AOP and Ozone Byproducts 

Session 18 - Modeling UV Systems 

2:55 PM - 3:40 PM 


3:40 PM - 5:20 PM 


Session 20 - AOP and Ozone Byproducts 

Session 21 - Modeling UV Systems 

Wednesday, May 6 th , 2009 

8:00 AM - 4 PM 

Ozone Technical Tour (includes transport & lunch) 

- Walter J. Sullivan Water Purification Facility 

at Cambridge Water Department 

- MWRA John J. Carroll Water Treatment Plant 

- Optional drop off by 3 PM at Logan Int’l Airport 

before returning to the Hyatt Regency Cambridge 

Sponsored By: Fuji Electric 

UV Technical Tour (includes transport & lunch) 

- Brockton, MA Advanced Waste Water Treatment Plant 

- Pawtucket, RI Water Treatment Plant 

- Optional drop off by 3 PM at Logan Int’l Airport 


Ozone Operations Workshop 

- MWRA John J. Carroll Water Treatment Plant 

(includes transport & lunch) 

- REGISTRATION DESK HOURS - 

SUNDAY 

7:30 AM - 8:30 AM 

(Sunday Workshops Only!) 

NOON - 7 PM 

(Conference Registration 

Begins) 

MONDAY 

7:30 AM - 12:15 PM 

1:15 PM - 5 PM 

TUESDAY 

7:30 AM - 12:15 PM 

2


Upcoming Events 

2009/2010 

Singapore 

IUVA 1-Day Workshop 

June 22, 2009 

Suntec Singapore International 

Convention & Exhibition Centre 

http://docs.iuva.org/IUVA_SIWW_22_June.pdf 

Tokyo 

IOA 19 th World Congress 

August 31 - September 3, 2009 

Tower Hall Funabori 

Edogawa-ku, Tokyo, Japan 

http://www.j-ozone.org/info/info001.html 

Amsterdam 

IUVA 5 th World Congress 

September 20-23, 2009 

NH Grand Hotel Krasnapolsky 

Amsterdam, The Netherlands 

http://docs.iuva.org/Registration_Amsterdam_2009.pdf 

Seattle / Bellevue 

IOA Annual Conference 

September, 20-22 2010 

Hyatt Regency Bellevue 

Washington, USA 

MORE INFORMATION - COMING SOON 

3

WELCOME MESSAGE & ORGANIZING COMMITTEE 

Dear Conference Participant, 

We welcome you to the Hyatt Regency Cambridge in Massachusetts, USA on behalf of the 

International Ozone Association – Pan American Group and the International Ultraviolet Association. 

We are pleased to have you join us for our 2009 North American Conference which features both UV 

and Ozone Basics Workshops, an Ozone Operations Workshop and both Ozone and UV Technical 

Tours that provide an inside look at some of New England’s most cutting edge Drinking Water and 

Wastewater Treatment Plants. 

UV and Ozone directly improve our quality of life. The strong technical contributions of this year’s 

speakers will make that abundantly clear. We proudly present this diverse and comprehensive look 

at each technology’s benefits, both stand-alone and when used in combination, and thank our 

talented speakers for their time and effort. 

We especially wish to acknowledge the work of Professor Mohamed Gamal El-Din, Ph.D., P.Eng., and 

Professor Karl Linden, Ph.D., who coordinated all of the sessions as well as organized and edited all 

of the abstracts and papers for this unique technical program. Many thanks to our hosts, the 

Massachusetts Water Resources Authority (MWRA), for producing this year’s CD of conference 

proceedings and inviting us into their facilities. Thanks also to our Primary Conference Sponsor, ITT 

Water & Wastewater. We greatly appreciate the support of all of our generous exhibitors and 

sponsors, who make this annual event possible. 

Welcome and enjoy! 

Linda Gowman, Ph.D., P.Eng. 

IUVA President 

Jeff Neemann 

IOA PAG Chair 

Technical Program Committee 

- Mohamed Gamal El-Din, Ph.D., P.Eng., University of Alberta, Co-Chair (IOA) 

- Karl Linden, Ph.D., University of Colorado at Boulder, Co-Chair (IUVA) 

- Jim Bolton, Ph.D., Bolton Photosciences 

- Pamela Chelme-Ayala, Ph.D., University of Alberta 

- Theping Chen, AECOM 

- Jim Constantacos, Constant America 

- Larry Forney, Ph.D., Georgia Tech 

- Ronald Gehr, Ph.D., McGill University 

- Dennis Greene, Ph.D., AECOM Water 

- Mirat Gurol, Ph.D., San Diego State University 

- Dr. Ron Hofmann, Ph.D., University of Toronto 

- Paul Overbeck, IOA & IUVA 

- Erik Rosenfeldt, Ph.D., University of Massachusetts-Amherst 

- Mike Santelli, Light Sources, Inc. 

- Diana Schoenberg, IOA & IUVA 

IOA & IUVA 2009 North American Conference – May 4-5, 2009 – Boston, MA, USA 

4

TECHNICAL PROGRAM 

ORAL PRESENTATIONS 

Monday May 04 th 2009 

General Opening Session – Monday May 04, 2009 

Charles View Ballroom (16 th Floor) 

Start 

End 

8:15 9:30 Welcome and Guest Speakers 

9:30 – 10:15 Coffee Break 

Session 1 – UV Validation – Monday May 04, 2009 

Meeting Room: Crispus Attucks 

Start End Title Authors Affiliations 

10:15 10:40 A Uniform Protocol for Wastewater 

UV Validation Applications - IUVA 

Manufacturers Council Position 

Oliver Lawal 1 , Paul Ropic 1 , 

Elliott Whitby 2 , Stan Shmia 3 , 

and Bertrand Dussert 4 

10:40 11:05 Overcoming Validation Report Complexity Phyllis Posy 1 , Karl Scheible 2 , 

and Chengyue Shen 2 

11:05 11:30 Validation of UV Reactors for Water 

and Wastewater Applications: 

What is the State-of-the-Art 

11:30 11:55 Standardized Lagrangian Actinometry 

Protocol for UV Reactor Validation 

O. Karl Scheible and 

Chengyue Shen 

Chengyue Shen 1 , Ernest R. 

Blatchley III 2 , Eric Cox 2 , 

and O. Karl Scheible 1 

1 ITT-WEDECO. 2 Calgon Carbon Corp. 

3 

Severn Trent Water Purification. 

4 

Siemens Water Technologies. 

1 

Atlantium Technologies. 2 UV Validation 

Center, HydroQual, Inc., Mahwah, NJ. 

HydroQual, Inc., Mahwah, NJ. 

1 

HydroQual, Inc. Mahwah, NJ. 

2 

Purdue University, West Lafayette, IN. 

Session 2 – UV Regulatory – Monday May 04, 2009 

Meeting Room: William Dawes 


10:15 10:40 Commissioning and Obtaining Regulatory 

Approval for Drinking Water UV 

Disinfection Systems 

10:40 11:05 Biodosimetry of a Full-Scale UV 

Disinfection System to Achieve 

Regulatory Approval for Drinking 

Water Disinfection 

11:05 11:30 Integrating UVDGM Operational 

Requirements in Small System 

Regulatory Compliance: 

The People Perspective 

11:30 11:55 Achieving UV Disinfection Credit 

for Pre-UVDGM Era UV Facilities: 

Experiences of Two UV Facilities 

David Gaithuma, Harold Wright, 

and Mark Heath 

Bruno Ferran, Robert Kelly, 

and Wei Yang 

Phyllis Posy 1 , Ytzhak Rozenberg 2 , 

and Peter Bugg 3 

Christine Cotton, P.E., 

and James Collins 

Carollo Engineers, 12592 West Explorer 

Drive, Suite 200, Boise, ID 83713. 

Infilco Degremont, Inc., Degremont North 

American Research & Development Center 

510 East Jackson Street, Richmond, 

VA, 23219. 

1 

Atlantium Technologies. 

2 

R&D, Atlantium Technologies. 

3 

EWT. 

Malcolm Pirnie, Inc., S. Church Ave, 

Suite 1120, Tucson, AZ. 

IOA & IUVA 2009 North American Conference – May 4-5, 2009 – Boston, MA, USA

Session 3 – Ozone Design and Operation – Monday May 04, 2009 

Meeting Room: Molly Pitcher 


10:15 10:40 Ozone Measurement and Control in 

Drinking Water Treatment Plants 

10:40 11:05 The Potential Use of Ozone 

in Municipal Waste Water 

11:05 11:30 Control of Iron and Manganese 

Ozone Removal by Differential 

Turbidity Measurements 

11:30 11:55 Optimizing an Intermediate Ozone 

System used for Primary Disinfection at a 

55 MGD Surface Water Treatment Plant 

Andrew Wright, Ph.D., 

and Victor Dosoretz 

A. Ried, J. Mielcke, 

and A. Wieland 

Vadim Malkov, Mike Sadar, 

Jon Schiller, and Eric Lehman 

Russ Navratil 1 , Chip England 1 , 

and Glenn Hunter 2 

IN USA Inc., 100 Morse St., Norwood, 

MA, 02062. 

ITT W&WW WEDECO, Boschstr. 4-14, 

32051 Herford, Germany. 

Hach Company, 5600 Lindbergh Dr. 

Loveland, CO 80538, USA. 

1 

Henrico County, VA. 

2 

Process Applications Inc. 

11:55 – 13:15 Luncheon 

Session 4 – UV Case Studies – Monday May 04, 2009 



13:15 13:40 UV System Technology Evaluation 

Using UV Cost Analysis Tool for 

Metro Vancouver’s Coquitlam UV 

Disinfection Project 

13:40 14:05 Brockton, Massachusetts Commissions 

a 60-mgd (227-ML/d) UV Wastewater 

Disinfection System 

14:05 14:30 Site Specific Testing of UV Disinfection 

at a Trickling Filter Plant 

14:30 14:55 Ultraviolet Light Disinfection System 

Conceptual Design for the Massachusetts 

Water Resources Authority John J. Carroll 

Water Treatment Plant 

Ayman Shawwa, P.E., Ph.D., 

BCEE 1 , Chris Schulz, P.E., 

BCEE 2 , Inder Singh, M.A.Sc. 

P.Eng. 3 , and James Kim, P.E. 1 

William C. McConnell, P.E. 1 , 

and David A. Norton 2 

Gary Hunter, P.E. 1 , 

Anjana Kadava 1 , Jane Hood 2 , 

and Don Gilpin 2 

Albert J. Capuzzi 1 , 

Brian Loux 1 , Paul Swaim 1 , 

and James P. Malley 2 

1 CDM, Walnut Creek, CA. 

2 

CDM, Denver, CO. 

3 

Metro Vancouver, BC, Canada. 

1 

CDM, 56 Exchange Terrace, Providence, RI 

02903. 2 City of Brockton, MA, 303 Oak Hill 

Way, Brockton, MA 02301. 

1 

Black & Veatch, 8400 Ward Parkway, Kansas 

City, MO 64114. 2 City of St. Joseph, MO. 

1 

CH2M HILL. 2 University of New Hampshire. 

Session 5 – Ozone Case Studies – Monday May 04, 2009 



13:15 13:40 Multi-function Sidestream 

Ozone Treatment at a Drinking 


13:40 14:05 Rising Energy Costs and Frozen 

Budgets: Getting More from Our 

Operating Buck 

14:05 14:30 Key Water Quality Parameters 

that Determine Ozone Dose for 

Massachusetts Water 

Resources Authority 

14:30 14:55 Treatment of Wastewater with Ozone 

at the Southwest Wastewater 

Treatment Plant 

Maxime Beaulieu 1 , 

Patrick Niquette 1 , 

Pierre Cullen 2 , 

and Denis Allard 2 

David W. Coppes 

Windsor Sung, Ph.D., P.E. 

Nick Burns 1 , Jeff Neemann 1 , 

Tom Holst 2 , and Jim Burks 2 

1 Dessau Inc., Water, Industry and Waste 

Management, 1080, Côte du Beaver Hall, 

Suite 300, Quebec, Canada, H2Z 1S8. 

2 

City of Laval, Department of environmental 

city management, Laval (Quebec), Canada, 

H7V 1A0. 

Western Operations, Massachusetts Water 

Resources Authority, 266 Boston Road, 

Southborough, MA 01772. 

MWRA, 260 Boston Road, Southborough, 

MA 01772. 

1 

Black & Veatch, 8400 Ward Parkway, Kansas 

City, MO 64114. 2 Springfield Utilities, 

3301 S. FF Hwy, Springfield, MO 65807. 


6




13:15 13:40 Optimization Considerations for an 

Ozone Side Stream Injection System 

13:40 14:05 Evaluating Options for Retrofitting a Large 

Scale Ozonation System in Texas 

Bill Mundy, C.E.T. 1 , 

Kerwin Rakness 2 , 

and Glenn Hunter 2 

Jeff Neemann 1 , David 

Timmerman 1 , Robert Hulsey 1 , 

Buford Green 2 , and Steve Long 2 

14:05 14:30 Keeping Ozone Generators Dry and Cool Kerwin L. Rakness 1 

and James Muri 2 

14:30 14:55 Application of Ozone for Contaminant 

Oxidation in Wastewater 

Eric C. Wert, Fernando Rosario- 

Ortiz, and Shane Snyder 

1 Regional Municipality Of Halton, 

1151 Bronte Road, Oakville, ON, Canada, 

L6M 3L1. 2 Process Applications Inc., 

Fort Collins, CO, USA, 80526. 

1 

Black & Veatch, Kansas City, MO. 2 North 

Texas Municipal Water District, Wylie, TX. 

1 

Process Applications, Inc., 2627 Redwing 

Rd., Suite 340, Fort Collins, CO 80526. 

2 

John J. Carroll Water Treatment Plant, 84 

D’Angelo Drive, Marlborough, MA 01752. 

Southern Nevada Water Authority, 

P.O. Box 99955, Las Vegas, NV USA. 


Session 7 – UV Case Studies – Monday May 04, 2009 



15:40 16:05 Approach for Achieving Sustainable 

Operation of the 2-bgd Catskill/Delaware 

UV disinfection Facility 

16:05 16:30 Feasibility of Ultraviolet Disinfection 

of A WWTP Final (Blended) Effluent 

under Wet Weather Flow Conditions 

16:30 16:55 Bidding, Testing, and Start-Up of a Reuse 

UV Disinfection System in Florida 

16:55 17:20 Validation of the Catskill/Delaware UV 

Reactor: A Comparison of Biodosimetry 

and Lagrangian Actinometry Methods 

Matthew T. Valade, P.E. 1 , 

Steven Farabaugh 2 , 

Paul D. Smith, P.E. 3 , 

and Gary Kroll, P.E. 4 

Khalil Z. Atasi, Ph.D., 

P.E., BCEE, F.ASCE 

Josefin M. Edeback, E.I. 

and Melanie A. Mann, P.E. 

Chengyue Shen 1 and Karl 

Scheible 1 , Matthew Valade 2 , 

and Ernest R. Blatchley 3 

1 Hazen and Sawyer, P.C., 24 Federal Street, 

Suite 302, Boston, MA 02129. 2 Hazen and 

Sawyer, P.C., 498 Seventh Avenue, 11 th 

Floor, New York, NY 10018. 3 NYC Dept. of 

Env. Protection, 96-05 Horace Harding Expy, 

Corona, NY 11368. 4 CDM, Raritan Plaza 1, 

Raritan Center, Edison, NJ 08817. 

Camp Dresser & McKee Inc., 2301 Maitland 

Center Parkway, Suite 300, Maitland, 

FL 32751. 

Hazen and Sawyer, P.C., 10002 Princess 

Palm Avenue, Tampa, FL 33619. 

1 

HydroQual, Inc. Mahwah, NJ. 2 Hazen and 

Sawyer, P.C., Boston, MA. 3 Purdue 

University, West Lafayette, IN. 

Session 8 – Ozone Case Studies – Monday May 04, 2009 



15:40 16:05 Updating Ozone for the 

Lincoln Water System 

16:05 16:30 Eastern Treatment Plant 

- Melbourne Water’s Approach to 

One of the World’s Most Complex 

Wastewater Technology Trials 

16:30 16:55 Operations Experience and 

Enhancements to the Two-stage 

Ozone System for the Cary/Apex, NC 


16:55 17:20 Treated Water Quality 

Enhancements from Ozonation 

in a Tertiary Plant Upgrade 

Jeff Neemann 1 , Nick Burns 1 , 

Robert Hulsey 1 , Andrew Hansen 1 , 

Eric Lee 2 , and John Miriovsky 2 

Mark Lynch 1 , John Mieog 1 , 

Clare McAuliffe 1 , Bruce Long 2 , 

Sock-Hoon Koh 2 , 

and Johanna Steegstra 3 

Bill Dowbiggin and Kelvin Creech 

John Mieog 1 , Mark Lynch 1 , 

Clare McAuliffe 1 , Bruce Long 2 , 

Sock-Hoon Koh 2 , 

and Johanna Steegstra 3 

1 Black & Veatch, Kansas City, MO. 

2 

Lincoln Water System, Lincoln, NE. 

1 

Melbourne Water Corporation; 

Melbourne, Australia. 2 Black & Veatch, 

Kansas City, MO. 3 Kellogg Brown & Root 

Pty Ltd, Melbourne, Australia. 

1 

CDM. 

2 

Town of Cary. 

1 

Melbourne Water Corporation; 

Melbourne, Australia. 2 Black & Veatch, 

Kansas City, MO. 3 Kellogg Brown & Root 

Pty Ltd, Melbourne, Australia. 

7 





15:40 16:05 Inline Multi-Jets Ozone Contactors: 

Performance and Scalability 

16:05 16:30 Operator-Friendly Technique and 

Quality Control Considerations for 

Indigo Colorimetric Measurement 

of Ozone Residual 

16:30 16:55 Highly Efficient High Concentration 

Photochemical Ozone Generation 

16:55 17:20 The Study on the Ceramic Membrane 

Wastewater Reuse System with 

Pre Ozonation and Coagulation 

Mahad S. Baawain 1 , 

Mohamed Gamal El-Din 2 , 

Daniel W. Smith 2 , 

and Angelo Mazzei 3 

Kerwin L. Rakness 1 , 

Eric C. Wert 2 , Michael Elovitz 3 , 

and Suzanne Mahoney 4 

Daniel E. Murnick 

M. Noguchi 1 , M. Aoki 1 , 

H. Kozono 1 , 

H. Kouchiwa 2 , 

and Y.Yoda 2 

1 Department of Civil & Architectural 

Engineering, Sultan Qaboos University, 

Muscat, Oman. 2 Department of Civil & 

Environmental Engineering, University of 

Alberta, Edmonton, Canada. 3 Mazzei 

Injector Corporation, Bakersfield, CA. 

1 

Process Applications, Inc., 2627 Redwing 

Rd., Suite 340, Fort Collins, CO 80526. 

2 

Southern Nevada Water System, Las Vegas, 

NV 89193. 3 Treatment Technology and 

Evaluation Branch, Water Supply & Water 

Res. Division, U.S. EPA, Cincinnati, OH 

45268. 4 Little Falls Water Treatment Plant, 

Passaic Valley Water Commission, 800 

Union Boulevard, Totowa, NJ 07512. 

UV Solutions Inc. and Rutgers University, 

Newark NJ 07102. 

1 

Metawater Co., LTD., Shiroyama Trust 

Tower. 4-3-1 Toranomon, Minato-ku, 

Tokyo 105-6029, Japan. 2 Tokyo Metropolitan 

Government, 2-8-1 Nishishinjuku, 

Shinjuku-ku, Tokyo 163-8001, Japan. 

Tuesday May 05 th 2009 

Session 10 – UV Disinfection Design – Tuesday May 05, 2009 



8:15 8:40 Disinfection Alternatives and Sustainability: 

Energy Optimization, Disinfection Efficiency, 

and Sustainability 

8:40 9:05 Airing it Out: Design Considerations 

for UV Disinfection Installations 

9:05 9:30 Impact of Biodosimetry-Based Validation 

on UV System Design Specifications 

Gary Hunter 1 , Andy Shaw 1 , 

Dr. Leonard W. Casson 2 , 

and Dr. Joe Marriott 2 

Aaron W. Duke, P.E. 

Bryan R. Townsend 1 

and Gary Hunter 2 

1 Black & Veatch, 8400 Ward Parkway, Kansas 

City, MO 64114. 

2 

Department of Civil and Environmental 

Engineering, 944 Benedum Engineering Hall, 

University of Pittsburgh, Pittsburgh, PA. 

11242 Waples Mill Road, Suite 250, Fairfax, 

VA 22030. 

1 

Black & Veatch, 8520 Cliff Cameron Drive, 

Suite 210, Charlotte, NC 28269. 

2 

Black & Veatch, 8400 Ward Parkway, 

Kansas City, MO 64114. 

Session 11 – Advanced Oxidation of Contaminants – Tuesday May 05, 2009 



8:15 8:40 A Bench-Scale Evaluation of UV and 

UV/H 2 O 2 Processes for the Removal 

of PPCPs in Secondary Treated Water 

of Sewage Treatment Plant 

8:40 9:05 The Effects of Vacuum-UV Radiation 

on Natural Organic Matter 

9:05 9:30 Predicting Hydroxyl Radical Activity 

and Trace Contaminants Removal 

in Ozonated Water 

Ilho Kim, Naoyuki Yamashita, 

and Hiroaki Tanaka 

Gustavo E. Imoberdorf 

and Madjid Mohseni 

Simon Vincent, Abderrahim Kotbi 

and Benoit Barbeau 

Research Center for Environmental Quality 

Management, Kyoto University, 1-2 

Yumihama, Otsu, Shiga 520-0811, Japan. 

Department of Chemical and Biological 

Engineering, The University of British 

Columbia, Vancouver, BC, Canada. 

Industrial-NSERC Chair in Drinking Water, 

École Polytechnique de Montréal, 

Département des Génies Civil, Géologique 

et des Mines, Montréal, QC, H3C 3A7. 


8

Session 12 – Perozone and AOP Processes –Tuesday May 05, 2009 



8:15 8:40 In-Situ 1,4 Dioxane Remediation 

in HVOC Sites 

8:40 9:05 Experiences of Perozone ® and 

C-Sparge TM at Two Former Dry 

Cleaner Sites in The Netherlands 

9:05 9:30 Non-Thermal Plasma - A Novel and Cost 

Effective Advanced Oxidation System 

Andrew Brolowski 

and William B. Kerfoot 

Bert Scheffer 1 

and Edward van de Ven 2 

Dvir Solnik 1 , Andreas Kolch 2 , 

Andrew Salveson 3 , Nitin Goel 3 , 

Nicola Fontaine 4 , 

Justin Sutherland 5 , 

and Chris Fennessy 6 

Kerfoot Technologies, Inc., 766-B Falmouth 

Road, Mashpee, MA 02649. 

1 

Verhoeve Milieu bv, Dorpsstraat 32, P.O. Box 

4, 6997 ZG Hoog-Keppel, The Netherlands. 

2 

Verhoeve Milieu bv, Aventurijn 600, P.O. Box 

3073, 3301 DB Dordrecht, The Netherlands. 

1 

Aquapure Technologies Limited, Israel. 

2 

Hytecon, Germany. 3 Carollo Engineers, 

Walnut Creek, CA. 4 Carollo Engineers, 

Walnut Creek, CA. 5 Carollo Engineers, 

Austin, TX. 6 Aerojet, Sacrament, CA. 


Session 13 – UV Disinfection Design – Tuesday May 05, 2009 



10:15 10:40 Use of Velocity Profiling to Assess 

to Effect of Piping Configuration 

on UV Dose Delivery 

10:40 11:05 Ultraviolet System Design Considerations 

for Uncovered Reservoir versus Water 

Treatment Plant Applications 

11:05 11:30 Costs and Sustainability Comparison 

of Chemical Disinfection and Medium 

Pressure Ultraviolet Disinfection for 

Virus Inactivation 

11:30 11:55 A Smart Way to Validate UV 

Systems for Reuse Applications 

Dennis J. Greene 1 , 

Keith Bircher 2 , 

and Harold B. Wright 3 

Jack Bebee, P.E. 1 

and Christine Cotton, P.E. 2 

James Collins 1 , 

Christine Cotton 1 , 

and Phyllis Posy 2 

1 AECOM Water, 276 Abby Road, 

Manchester, NH 03103. 2 UV Technologies 

Div., Calgon Carbon Corporation, 50 Mural 

Street, Unit#3, Richmond Hill, ON, Canada 

L4B 1E4. 3 Carollo Engineers, 12592 West 

Explorer Drive, Suite 200, Boise, ID 83713. 

1 

Malcolm Pirnie, Inc., 1525 Faraday Avenue, 

Suite 290, Carlsbad, CA 92008. 2 Malcolm 

Pirnie, Inc., One South Church Avenue, Suite 

1120, Tucson, AZ 85701. 

1 

Malcolm Pirnie, Inc., 1 S. Church Ave, 

Suite 1120, Tucson, AZ. 2 Atlantium 

Technologies, Har Tuv Industrial Park, 

POB 11071, Israel 99100. 

Matthias Boeker 1 , 

1 ITT Water & Wastewater U.S.A., 14125 

Andrew Salveson 2 , 

Madhukar Rapaka 3 , 

and Ronnie Bemus 1 

South Bridge Circle, Charlotte, NC 28273. 

2 

Carollo Engineers, 2700 Ygnacio Valley 

Road, Suite 300, Walnut Creek, CA 94598. 

3 

ITT Water & Wastewater Germany, 

Boschstrasse 4, 32051 Herford, Germany. 

Session 14 – Advanced Oxidation of Contaminants – Tuesday May 05, 2009 



10:15 10:40 A Kinetic Model for the Degradation 

of Natural Organic Matter during the 

Ultraviolet Hydrogen Peroxide 

Advanced Oxidation Process 

10:40 11:05 UV Photolysis of Pharmaceuticals and 

Personal Care Products (PPCPs) and 

Endocrine Disrupting Substances 

(EDS) in Drinking Water 

11:05 11:30 Advanced Oxidation Processes for 

Contaminant Destruction: Selecting 

between Ozone-Peroxide or UV-Peroxide 

11:30 11:55 Rapid Measurement of Background 

Hydroxyl Radical Scavenging in Water 

Sarathy, S.R., Bazri, M., 

and Mohseni, M. 

Jules Carlson 1 , Mihaela Stefan 2 , 

and Chris Metcalfe 1 

James Collins 

and Christine Cotton, P.E. 

Matthew Hross 

and Erik J. Rosenfeldt 

Department of Chemical and Biological 

Engineering, University of British Columbia, 

2360 East Mall, Vancouver, BC V6T 1Z3 

Canada. 

1 

Trent University, Peterborough, 

ON, Canada. 

2 

Trojan Technologies, London, ON, Canada. 

Malcolm Pirnie, Inc., 1 S. Church Ave, 

Suite 1120, Tucson, AZ. 

The University of Massachusetts, Department 

of Civil and Environmental Engineering. 

9 


Session 15 – Perozone and AOP Processes –Tuesday May 05, 2009 



10:15 10:40 Perozone Groundwater Sparging at the 

Days Inn Lake City Pre-Approval Site 

10:40 11:05 Characterization of Ozone 

Mass Transfer in Model Soils 

11:05 11:30 Ozone Oxidation for Source 

Removal And Prevention Barrier 

at a Fire Training Academy 

11:30 11:55 A Simplified Method for Modeling 

Chemical Intermediates in 

Advanced Oxidation Processes 

Edward M. Kellar 

and Chris Mickler, P.E. 

Alejandro García 1 , Tatyana 

Poznyak 2 , Jesús Rodríguez 2 , 

and Isaac Chairez 3 

Scott C. Michaud 

and Thomas C. Cambareri, LSP 

Joseph A. Drago, P.E., Ph.D. 

MACTEC, Inc., Gainesville, FL 32669. 

1 

Department of Automatic Control, 

CINVESTAV-IPN, Av. Instituto Politécnico 

Nacional, Col. San Pedro Zacatenco, 

C.P.07360, Mexico D.F., Mexico. 2 Superior 

School of Chemical Engineering National 

Polytechnic Institute of Mexico (ESIQIE- 

IPN), Edif 7, UPALM, C.P. 07738, Mexico 

D.F., Mexico. 3 Professional Interdisciplinary 

Unit of Biotechnology of National Polytechnic 

Institute (UPIBI-IPN), Av. Acueducto s/n., 

C.P. 07480, México, D.F, México. 

Cape Cod Commission, 3225 Main Street, 

PO Box 226, Barnstable, MA 02630. 

Kennedy/Jenks Consultants, 

San Francisco, CA. 

11:55 – 13:15 Luncheon 

Session 16 – UV Disinfection Research – Tuesday May 05, 2009 



13:15 13:40 Effect of Pre- and Post- UV Disinfection 

Conditions on Photoreactivation of 

Fecal Coliforms from a Physicochemical 

Wastewater Effluent 

13:40 14:05 Comparison of the Disinfection Effects 

of Vacuum-UV (VUV) and UV Light on 

Bacillus subtilis Spores at 172, 222, 

254 nm 

14:05 14:30 E. coli Repair in UV Water 

Treatment Conditions 

Catherine Hallmich 

and Ronald Gehr 

Ding Wang, 1,2 

Thomas Oppenländer, 3 

Mohamed Gamal El-Din, 1 

and James R. Bolton 1 

Bohrerova, Z. and Linden, K.G. 

Department of Civil Engineering and Applied 

Mechanics, McGill University, 817 Sherbrooke 

Street West, Montreal, Quebec, H3A 2K6. 

1 


Engineering, University of Alberta, Edmonton, 

AB, T6G 2W2, Canada. 2 Current address, 

Department of Civil Engineering, University of 

Toronto, Galbraith Building, 35 St. George St., 

Toronto, ON, Canada, M5S 1A4. 

3 

Hochschule Furtwangen University (HFU), 

Campus Villingen-Schwenningen, Fakultät 

Maschinenbau und Verfahrenstechnik, 

Jakob-Kienzle-Str. 17, 78054 

Villingen-Schwenningen, Germany. 


10

Session 17 – AOP and Ozone Byproducts – Tuesday May 05, 2009 



13:15 13:40 Novel UV LED Advanced Oxidation 

System for Disinfection and Removal 

of Organic and Heavy Metal 

Contaminants in Water 

13:40 14:05 UV Advanced Oxidation Processes 

for Taste and Odor Treatment: 

Evaluation of Assimilable Organic Carbon 

Formation Potential at an Indiana WTP 

14:05 14:30 Toxicity Assessment and Identification 

of Oxidation Byproducts Generated 

During the Ozonation of Natural 

Water Containing Pesticide 

14:30 14:55 Evaluating the Effects of Source 

Water Quality on Bromate 

Mitigation Performance 

Tom Hawkins, Ph.D, and Mark 

Owen 

James Collins 1 , Christine Cotton 1 , 

Bruce Heeke 2 , David Dahl 3 , 

and Alan Royce 4 

Pamela Chelme-Ayala, 

Mohamed Gamal El-Din, 

and Daniel W. Smith 

Zaid Chowdhury 1 , David Eberle 1 , 

Laurel Passantino 1 , Joe Kurrus 2 , 

and Linda Bezy-Botma 2 

Puralytics, 15250 NW Greenbrier Pkwy, 

Beaverton, OR, USA 97006-5764. 

1 

Malcolm Pirnie, Inc., Tucson, AZ. 

2 

Patoka Lake Region Water and 

Sewer District. 3 Midwestern Engineers. 

4 

Trojan Technologies. 


Engineering, 3-133 Markin/CNRL Natural 

Resources Engineering Facility, University of 

Alberta, Edmonton, AB, T6G 2W2, Canada. 

1 

Malcolm Pirnie, Inc. 2 City of Peoria, AZ. 

Session 18 – Modeling UV Systems –Tuesday May 05, 2009 



13:15 13:40 Monte Carlo Ray Trace Model: 

A New Approach in Determining 

Fluence Rates in UV Systems 

13:40 14:05 A Comparison of Two Methods for 

Measuring the UV Output of Low 

Pressure Mercury Lamps in Air 

14:05 14:30 Method for Measurement of Output 

of Low Pressure Mercury Lamps 

14:30 14:55 Controlling Mercury Release with 

UV Lamp Sleeve Breaks 

Khoi Nguyen and Jaewan Yoon 

Old Dominion University, Civil and 

Environmental Engineering, Norfolk, VA. 

G. Elliott Whitby 1* , Bill Sotirakos 1 , 

1 Calgon Carbon Canada, 50 Mural St., Unit #3, 

and James R. Bolton 2 Richmond Hill, ON, Canada L4B 1E4. 2 Bolton 

Photosciences Inc., 628 Cheriton Cres., 

Edmonton, AB, Canada T6R 2M5. 

Volker Adam, Ralf Dreiskemper, 

Martin Kessler 

Harold Wright, Ed Wicklein, 

and Corianne Hart 

Heraeus Noblelight GmbH, Heraeusstr. 12- 

14, 63450 Hanau, Germany. 

Carollo Engineers, 12592 West Explorer 

Drive, Suite 200, Boise, ID 83713. 


Session 19 – UV Disinfection Research – Tuesday May 05, 2009 



15:40 16:05 High Energy Efficiency and 

Small Footprint with High-Wattage 

Low Pressure UV Disinfection for 

Water Reuse 

16:05 16:30 Impact of UV Disinfection Combined 

with Chlorination/Chloramination on the 

Formation of Nitrogenous Disinfection 

Byproducts in Drinking Water 

16:30 16:55 High Intensity Pulsed Lamps for 

Water Treatment: Review and Status 

16:55 17:20 An Empirical Method for Accurately 

Sizing Wastewater UV Reactors for 

Disinfection of any Microorganism 

Andrew Salveson 1 , 

Tavy Wade 1 , Keith G. Bircher 2 , 

and Bill Sotirakos 2 

Amisha D. Shah 1 , 

Aaron A. Dotson 2 , Karl G. Linden 2 , 

Howard S. Weinberg 3 , 

and William A. Mitch 1 

Ray Schaefer 

and Michael Grapperhaus 

1 Carollo Engineers. 

2 

Calgon Carbon Corporation. 

1 

Department of Chemical Engineering, Yale 

University, 9 Hillhouse Ave., New Haven, CT 

06520. 2 Department of Civil, Environmental, 

and Architectural Engineering, Engineering 

Center ECOT, University of Colorado at 

Boulder, Boulder, CO 80309. 3 Department of 

Environmental Sciences and Engineering, 

University of North Carolina at Chapel Hill, 

1303 Michael Hooker Research Center, 

Chapel Hill, NC 27599. 

Phoenix Science & Technology, Inc., 

Chelmsford, MA 01824. 

Harold Wright 1 , Andrew 

1 2700 Ygnacio Valley Road, Suite 300, 

Salveson 1 , Tavy Wade, 

Walnut Creek, CA 94598. 

Sean Poust 1 , Allan Slater 2 , 

2 Severn Trent Services, 580 Virginia 

Duncan Collins 2 , Jeremy 

Drive, Suite 300, Ft. Washington, 

Meier 2 , and Ian Dearnley 2 PA 19034. 

11 


Session 20 – AOP and Ozone Byproducts – Tuesday May 05, 2009 



15:40 16:05 Advanced Oxidation Process 

– Effective and Technical Suitable 

for Micropollutant Removal in 

Contaminated Water Sources 

16:05 16:30 Bromate Pre-systemic Detoxification 

Metabolism Research Progress 

16:30 16:55 Kinetic and Mechanistic Studies 

on Decomposition Reactions of 

Pyrrolidone Derivatives Using O 3 

16:55 17:20 Ozone Disinfection Reduces Disinfection 

Byproduct Formation to Comply with 

New Stage 2 DBP and LT2 Requirements 

J. Krüger1, A. Ried 1 , 

1 ITT W&WW WEDECO GmbH, Boschstr. 6, 

K. Teunissen 2 , A.H. Knol 2 , 

32051 Herford, Germany. 2 DZH & Delft 

and D. Csalovszki 3 University of Technology PO 34, 2270 AA 

Voorburg, The Netherlands. 3 ITT W&WW 

USA WEDECO Products, 14125 South 

Bridge Circle, Charlotte, NC 28273. 

Joseph Cotruvo 1* , Richard Bull 2 , 

Brian Cummings 3 , Jeffrey Fisher 3 , 

Zhongxian Guo 4 , Choon Nam 

Ong 5 , Oscar Quinones 6 , 

Shane Snyder 6 , Jason Keith 7 , 

Gilbert Gordon 7 , 

and Gilbert Pacey 7 

Yu Tachibana, Masanobu Nogami, 

Yuichi Sugiyama, 

and Yasuhisa Ikeda 

1 Joseph Cotruvo & Associates LLC, 

Washington, DC, USA. 2 MoBull Consulting, 

Richland, WA, USA. 3 University of Georgia, 

Athens, GA, USA. 4 PUB Waterhub Centre for 

Advanced Water Technology, Singapore. 

5 

National University of Singapore. 6 Southern 

Nevada Water Authority, Henderson, NV, USA. 

7 

Miami University, Oxford, OH, USA. 

Research Laboratory for Nuclear 

Reactors, Tokyo Institute of Technology, 

2-12-1-N1-34 Ookayama, Meguro-ku, 

Tokyo 152-8550, Japan. 

Michael A. Oneby 1 , Richard Lin 2 , 

1 MWH Americas, 789 N. Water St, Suite 430, 

James H. Borchardt 2 , 

Milwaukee, WI 53202-3558, USA. 

and Charles O. Bromley 3 2 MWH Americas, 618 Michillinda Ave., 

Suite 200, Arcadia, CA 91007, USA. 

3 

MWH Americas, 3010 W. Charleston Blvd, 

Suite 100, Las Vegas, NV 89102, USA. 

Session 21 – Modeling UV Systems –Tuesday May 05, 2009 



15:40 16:05 Comparison Testing of ‘Spot’ vs. ‘Pellet’ 

LPHO UV Lamps 

16:05 16:30 Measurements of UV Lamp Performance 

in Near-Field and Far-Field Apparatus 

16:30 16:55 Application of Computational Fluid 

Dynamics to Support Design of Full-Scale 

Wastewater UV Disinfection Channels 

16:55 17:20 A Genomic Model for the Prediction 

of Ultraviolet Inactivation Rate 

Constants for RNA and DNA Viruses 

Mike Santelli 1* 

and James R. Bolton 2 

G. Fang, D.G. Knight, 

R. Kilgour, and T. Molyneux 

Shanshan Jin 

and Melanie A. Mann 

1 Light Sources Inc., 37 Robinson Blvd., 

Orange, CT 06477. 2 Bolton Photosciences 

Inc., 628 Cheriton Cres., NW, Edmonton, 

AB, Canada, T6R 2M5. 

Trojan Technologies, 3020 Gore Road, 

London, ON, Canada N5V 4T7 

Hazen and Sawyer, P.C., 11242 Waples Mill 

Road, Suite 250, Fairfax, VA 22030. 

Wladyslaw J. Kowalski 1 , 

1 Immune Building Systems, Inc., 575 

William P. Bahnfleth 2 , 

Madison Ave., 10th Floor, New York, 

and Mark T. Hernandez 3 NY10022. 2 The Pennsylvania State 

University, Department of Architectural 

Engineering, University Park, PA 16802. 

3 

University of Colorado, Department of Civil, 

Environmental, and Architectural 

Engineering, Boulder, CO 80309. 


12

POSTER PRESENTATIONS 

Session P1 – Monday May 04, 2009 

President’s Ballroom Prefunction Area 


14:55 15:40 Passivation, Fabrication and Maintenance 

Issues in Ozone and Oxygen Systems 

14:55 15:40 Effect of additives on the degradation 

of Reactive Black 5 (RB5) 

by simple ozonation 

Patrick Banes, Michel Dalglish, 

Brent Ekstrand, Ph.D. 

and Daryl Roll, P.E. 

Arizbeth A. Pérez Martínez 

and Tatyana Poznyak 

Astro Pak Corporation, 270 E. Baker Street, 

Suite 100, Costa Mesa, CA 92626. 

Escuela Superior de Ingeniería Química e 

Industrias Extractivas – Instituto Politécnico 

Nacional,(ESIQIE-IPN), Edif. 7, UPALM, C.P 

07738, DF, México. 

Session P2 – Tuesday May 05, 2009 



9:30 10:15 Electrolytic Ozone Generation 

Using Solid Diamond Anodes 

9:30 10:15 Ozone-Based Clean-In-Place 

(CIP) of Bioreactors 

9:30 10:15 Noteworthy Nuances of Constructing 

and Starting Up an Ozone System 

9:30 10:15 Pilot Test Results Perozone TM Injection 

Technology Kitchener, Ontario 

Bill Yost 

Hossein Zarrin 1 , Brian Hagopian 2 , 

and Dr. Carl Lawton 3 

Ben Kuhne1 1 , Jack Bebee 1 , 

Robert W. Hoffman 2 , 

and Stephanie Bishop 3 

Dave Montgomery 

and Darko Strajin 

Electrolytic Ozone Inc, Cambridge Innovation 

Center, One Broadway, Cambridge MA 02142. 

1 

MKS Instruments Inc. 2 Mar Cor Purification. 

3 

University of Massachusetts-Lowell. 

1 

Malcolm Pirnie, Inc., 1525 Faraday Avenue, 

Suite 290, Carlsbad, CA 92008. 

2 

Malcolm Pirnie, Inc., 12400 Coit Road, Dallas, 

TX 75251. 3 Malcolm Pirnie, Inc., 2301 

Maitland Center Parkway, Suite 244, Maitland, 

FL 32751. 

Trow Associates, Inc., 1595 Clark Boulevard, 

Brampton, ON, Canada. 

Session P3 – Tuesday May 05, 2009 



14:55 15:40 The Bioassay Validation and Real-Time 

UV Dose Monitoring are Essential for 

Maintaining UV Disinfection Efficacy 

in Pharmaceutical Manufacturing 

14:55 15:40 Results of a CFD Simulation of the 

UV/H 2 O 2 Advanced Oxidation Process 

14:55 15:40 Regenerating Spent Zeolites with UV 

and UV/H 2 O 2 to Enhance Removal of 

Endocrine Disrupting Compounds 

14:55 15:40 Mixing Effects on the 

Chloramination Process 

Ismail Gobulukoglu, Ph.D. 

Scott M. Alpert, P.E. 1 

and Joel J. Ducoste, Ph.D. 2 

Safina Singh and Erik Rosenfeldt 

Khyati Jain 1 and Irvine Wei 2 

Science and Technology Department, 

Aquafine Corporation, 29010 Avenue 

Paine, Valencia, CA 91355, USA. 

1 

HDR Engineering, Inc. of the Carolinas, 

Charlotte, NC. 

2 

NC State University, Raleigh, NC. 


Engineering, University of Massachusetts- 

Amherst. 

1 

CDM Inc., Walnut Creek, CA. 2 Northeastern 

University, Civil and Environmental 

Engineering Department, Boston, MA. 

13 


ORAL PRESENTATIONS 

Monday AM – Session 1: UV Validation – S1-1 


A Uniform Protocol for Wastewater UV Validation Applications 

- IUVA Manufacturers Council Position 

Oliver Lawal 1 , Paul Ropic 1 , Elliott Whitby 2 , Stan Shmia 3 , and Bertrand Dussert 4 

1. ITT-WEDECO 

2. Calgon Carbon Corporation 

3. Severn Trent Water Purification 

4. Siemens Water Technologies 

The treatment objective of an ultraviolet disinfection system used in a wastewater application is to protect aquatic 

and ecological environments. To ensure this objective is adequately met it is important to validate, or verify 

equipment performance for a specific application. The widely accepted method for completing this validation is by 

determining the dose delivery performance using biodosimetry. Whilst several protocols exist for completing 

biodosimetry tests, or bioassays, for different applications, only two methods are in wide scale use in the industry 

worldwide; 

• Ultraviolet Disinfection Guidelines for Drinking Water and Water Reuse, 2 nd Edition, published by the 

National Water Research Institute (NWRI) in collaboration with the Awwa Research Foundation 

(AwwaRF). Specifically, chapter two; Water Reuse and chapter three; Protocols. Hereafter referred to as 

NWRI/AwwaRF. 

• Ultraviolet Disinfection Guidance Manual for the Final Long Term 2 Enhanced Surface Water Treatment 

Rule, published by the US EPA. Hereafter referred to as UVDGM. 

Both guidelines follow similar formats and are in wide scale use by UV Manufacturers, Engineering Consultants 

and Regulators. However, neither specifically makes reference to the particular challenges associated with 

completing bioassays in wastewater applications. Many stakeholders within the UV industry have called for such a 

uniform protocol for wastewater UV applications that can be widely adopted by the industry and regulatory bodies. 

In an effort to provide a positive contribution to the industry in this matter, the International Ultraviolet Association 

(IUVA) Manufacturers Council formed a task force in 2007. The objectives were to; 

• Evaluate the existing protocols to identify aspects that could be of use for a uniform wastewater protocol 

• Facilitate discussion with both regulators and engineering consultants on the issue of a uniform 

wastewater protocol 

• Outline a position on a potential solution for a uniform wastewater protocol 

After undertaking reviews and discussions with interested parties, this paper will represent the final portion of the 

task force objectives in describing a potential solution for a uniform wastewater protocol. 


14



Overcoming Validation Report Complexity 

Phyllis Posy 1 , Karl Scheible 2 , and Chengyue Shen 2 

1. Atlantium Technologies 

2. UV ValidationCenter, HydroQual, Inc., Mahwah New Jersey 

Validation Report complexity has turned out to be a hidden Achilles heel of the UV industry. When the United 

States Environmental Protection Agency finalized and published the Ultra Violet Disinfection Guidance Manual 

(UVDGM) for use in validating UV reactors in the end of 2006, they specifically covered both setpoint and dose 

pacing validations with a broad net for T1, MS2 and other challenge organisms. In focusing on disinfection 

required by the Long Term 2 Enhanced Surface Water Treatment Rule (LT2ESWTR) and the Groundwater Rule, 

they also gave the green light for the development of even more sophisticated validation techniques including dyed 

microspheres (DMS) validations and the direct use of target organisms (like adenovirus). The underlying message 

to regulators – who are generalists rather than UV specialists – is the more data the better. 

But turning an extensive data set into a simple enough report to support a decision-making process is another 

matter indeed. Validation reports must be understood by busy regulators and administered by small communities. 

This communication challenge falls on validators, manufacturers and the engineers who play a critical role in 

designing water treatment processes for regulatory compliance. And this is only the first step. 

The next step for a regulator or WTP operator is the persistent question of how to assure that the reactor received 

“conforms uniformly” to the reactor that had been validated without extensive and expensive retesting. 

Finally, without translating and converting the recordkeeping, calibration and correction factor requirements into an 

easy daily operating regimen, UV may become favored by larger systems, but never get to the small communities 

that need it. 

This paper will describe the following: 

• The critical factors in translating a validation dataset into a meaningful usable report 

• The development and use of a Validation Verification screen that enables the user to check that 

the reactor they installed “conforms uniformly” to the reactor that was validated. 

• Automating and integrating UVDGM operational requirements into WTP life. 

15 




Validation of UV Reactors for Water and Wastewater Applications: 

What is the State-of-the-Art 

O. Karl Scheible and Chengyue Shen 

HydroQual, Inc., Mahwah, NJ 

Considerable experience has been gained in the validation of UV reactors, addressing drinking water and wastewater 

applications with newly developed protocols, and new methods for analyzing the data and credited performance for a given 

reactor. This paper will compile and address the current state-of-the-art for validation, posed as a series of questions: 

What protocols are in play at this time, and how are they used in the industry? Status and comparison of the UVDGM 

(2006), ONORM and DVGW, NWRI, ETV and recent updates for a unified low-dose, reuse and related treated-wastewater 

validation applications. A formal protocol to validate with dyed-microspheres has also been drafted and demonstrated with 

several reactors. 

What is the status of biodosimetry for validation and what microbiological surrogates have been tested, or are being 

evaluated? We will review recent work and update the UVDGM biodosimetric approach, addressing advances with T1UV, 

T1, T7, Q, MS2 and other appropriate and practical surrogates. This will include work that is being reported regarding 

high-dose validations with A. niger, B. pumulus spores, and Adenovirus 2. A key advance has been the ability to access a 

wider variety of surrogates, the use of multiple surrogates and the concept of actual pathogen challenges to verify performance. 

What is Lagrangian actinometry using dyed microspheres and how does this method compare to biodosimetry? Cited 

as an emerging technique by the UVDGM, the use of dyed microspheres to directly measure dose-distribution has undergone 

considerable testing and demonstration, resulting in a new validation protocol for the UV industry. We will present an 

overview of this technique and how it compares to biodosimetry with respect to crediting log-inactivation and dose for 

alternative pathogens or pathogen indicators. 

Where is validation testing being done? Testing is being done both on-site at a commissioned facility, or off-site 

at a dedicated test facility. We will provide an update on general validation practices, and considerations of on- versus 

off-site locations. 

What are the more recent methods for analysis and use of the validation data and how are the validations being 

reviewed and accepted within the owner and regulator community? With continued experience and applications, the 

methods for testing and performance analysis are evolving. For example, the field is able to access alternate microbes and to 

use multiple microbes for biodosimetry, a practice that can effectively eliminate the RED bias promulgated by the UVDGM. 

Validation practices for wastewater applications are incorporating the approaches used by the UVDGM protocols for drinking 

water, allowing more and more for a uniform validation approach. Dyed-microspheres offer the ability to address the 

inactivation of pathogens directly, without the use of surrogate microbes. 

What is the status of modeling as an alternative validation method? Extensive work is being done in the area of 

CFD-intensity modeling to characterize UV reactors and related installation configurations. Will these techniques eventually 

supplant direct testing? We will review the current approaches and how they are affecting the validation process. 

What are the difficulties and bottlenecks that are being experienced with this validation process, and how can these be 

resolved? The intent of the process was to assure that the equipment being offered can be fully evaluated as to its performance 

and when installed will perform successfully. Most critically, as we move beyond the development of these protocols into 

full-scale validations of a wide variety of UV systems, owners and regulators must accept the equipment for installation. We 

will discuss alternatives for streamlining the review process, preventing the potential for costly multiple reviews and the need 

for multiple submittals and acceptances within the regulatory community. There is a clear need to facilitate this in order to 

avoid slowing the industry simply because an onerous and unwieldy review and acceptance process. 


16



Standardized Lagrangian Actinometry Protocol for UV Reactor Validation 

Chengyue Shen 1 , Ernest R. Blatchley III 2 , Eric Cox 2 , and O. Karl Scheible 1 

1. HydroQual, Inc. Mahwah, NJ 

2. Purdue University, West Lafayette, IN 

Validation of UV reactors is an established practice, which until recently has relied exclusively on biodosimetry to 

define the reduction equivalent dose (RED) delivered across a targeted operating range. This validation concept is 

driven by regulatory- and owner-related requirements and is used in both water and wastewater disinfection 

applications. In particular, the US EPA’s Ultraviolet Disinfection Guidance Manual (UVDGM) prescribes 

full-scale validation of UV reactors installed for Cryptosporidium, Giardia and viral disinfection credit. The 

UVDGM provides protocols for validation testing and the determination of credited RED and corresponding log 

inactivation. These rely solely on the use of biodosimetric techniques, although the UVDGM leaves open the 

possibility that new techniques may be developed for use at the validation level. 

This paper presents the final draft of a standardized protocol for application of Lagrangian actinometry in the 

validation of UV disinfection systems (it updates presentation given at the WQTC-2008, which addressed the 

status of the protocol development). The protocol allows measurement of the dose-distribution delivered by a 

reactor, which, when integrated with the dose-response kinetics of a targeted pathogen, predicts the log-inactivation 

of the targeted pathogen. The new protocol responds to the regulatory validation requirements directly, and, in 

effect provides a clear understanding of the performance and behavior of a reactor when addressing any pathogen 

of concern. Results of work done at Purdue University and the UV Center in New York have been presented 

at several venues, including, most recently at ACE 2008 and WQTC-2008. This new presentation builds on 

these prior discussions of the dyed-microspheres technology, providing the final protocol by which the 

dyed-microspheres approach can be used to validate a UV reactor. 

Supported by NYSERDA, AwwaRF, NYCDEP and others, the protocol has been developed in the context and 

format of the UVDGM. Field efforts to demonstrate and refine the method entailed three large scale validations 

that included T1 and MS2 coliphage biodosimetry in conformance with the US EPA Ultraviolet Disinfection 

Guidance Manual, and simultaneous actinometry with dyed-microspheres. The validation of the NYC DEP 

Catskill/Delaware UV reactor demonstrated the method. Some of these data will be presented as examples are 

carried through the body of the presentation. These will show the field and lab methods, the data analysis 

techniques to transform the raw dose-response and field test measurements to dose-distributions, and the 

integration of the dose distribution with the dose-response kinetics of targeted pathogens to determine 

log-inactivation as a function of the reactor operation variables. The QA protocols associated with the method will 

be presented, as will the development of the validation factor to determine credited log-inactivation. 

17 


Monday AM – Session 2: UV Regulatory – S2-1 


Commissioning and Obtaining Regulatory Approval 

for Drinking Water UV Disinfection Systems 

David Gaithuma, Harold Wright, and Mark Heath 

Carollo Engineers, 12592 West Explorer Drive, Suite 200, Boise, ID 83713 

Ultraviolet (UV) disinfection has been used to treat drinking water in Europe since the 1950s and in North America 

for nearly two decades now. Over the last 10 years, the practice of UV disinfection has evolved considerably in 

terms of regulations, commercial technologies, design and operation, and fundamental understanding. As a result, 

utilities, engineers and regulators see UV disinfection as an effective technology for inactivating chlorine-resistant 

pathogens such as Cryptosporidium and as an important process in achieving multi-barrier treatment and protecting 

public health. 

While this track record suggests UV disinfection is an established technology, most states have not established a 

framework for implementation of UV for disinfection credit almost three years after the promulgation of the US 

EPA Long Term 2 Enhanced Surface Water Treatment Rule (LT2ESWTR) and the completion of UV Disinfection 

Guidance Manual (UVDGM). This is indicative of the progress that remains to be made in obtaining regulatory 

buy-in for this technology. 

This paper highlights the process of commissioning UV systems at two utilities to ensure compliant operation, 

coupled with the experience of obtaining regulatory approval for UV disinfection. 


18



Biodosimetry of a Full-Scale UV Disinfection System to Achieve 

Regulatory Approval for Drinking Water Disinfection 

Bruno Ferran, Robert Kelly, and Wei Yang 

Infilco Degremont, Inc., Degremont North American Research & Development Center 

510 East Jackson Street, Richmond, VA, 23219 

This paper presents the findings of an extensive bioassay validation test that began last year at the UV Validation 

and Research Center of New York (UV Center) in Johnstown, New York with the objective to evaluate the 

performance of a large full-scale UV reactor for the disinfection of drinking water. The UV reactor is a 36-inch 

diameter cross-flow in-line reactor operating medium pressure lamps as a light source. Bioassay testing was 

conducted following both the DVGW W294 and the US EPA UVDGM test guideline using MS-2 and T1 phage as 

surrogate microorganisms. Curves of sensor UV Intensity Setpoint (ISP) versus flow rate were obtained following 

the DVGW W294 test methods for delivered doses of 20, 30 and 40 mJ/cm 2 . These curves can be used to size and 

operate UV systems for applications where the DVGW W294 guideline is considered as the basis for design. 

A first set of T1 phage dose-flow runs was conducted under conditions of reduced lamp output power. The 

resulting T1 phage REDs were combined with those obtained from MS2 phage and the entire set of REDs was 

correlated versus flow rate, ISP and UV sensitivity (UVS). The resulting fit equation can be used to size and 

operate UV systems for applications where the US EPA UVDGM is considered as the basis for design. Design 

dose values for the disinfection of Cryptosporidium and Giardia can be calculated for a given set of flow and ISP 

by computing 5 mJ/cm 2 /logI in the fit equation UVS term. As a result, the US EPA RED bias uncertainty factor is 

equal to that of T1 phage. A final set of bioassay test runs is planned for the spring of 2009 to incorporate high 

UVT REDs into the dataset and strengthen the master fit equation, specifically for US EPA applications. 

19 




Integrating UVDGM Operational Requirements in 

Small System Regulatory Compliance: The People Perspective 

Phyllis Posy 1 , Ytzhak Rozenberg 2 , and Peter Bugg 3 

1. Atlantium Technologies 

2. R&D, Atlantium Technologies 

3. EWT 

When the United States Environmental Protection Agency finalized the Ultra Violet Disinfection Guidance Manual 

(UVDGM) to provide information about how to evaluate and use UV for public drinking water treatment, 

specifically to fulfill the requirements of the Long Term 2 Enhanced Surface Water Treatment Rule (LT2ESWTR) 

and the Groundwater Rule, much thought was given to how validated technology might be kept in operational 

compliance. How could the guidance help regulators trust and measure UV for drinking water disinfection and 

assure operational reliability and consistent performance over time? 

Clearly translating all of the precautions and testing that underlie the EPA validation protocol and guidance and 

converting all that into monitoring, recordkeeping, calibration and correction factor requirements was a substantial 

task. Several drafts were circulated until a set of monitoring, reporting, maintenance and other regimens was 

finalized as required or recommended. 

The question remains: Are these provisions really understood or honored by regulators, manufacturers, engineers or 

users? Do states see these provisions as protecting small systems or burdening them? How do the small systems 

look at these provisions? How can they be turned into a daily operating regimen that can be implemented with 

minimal disruption and effort by a small system? 

This paper will catalogue some operational experiences and cases and focus on: 

• How regulators consider the UVDGM operational guidance in making their 

decisions about UV 

• How engineers consider the UVDGM operational guidance in their designs and cost analysis 

• How these issues surface in actually operating a UV system in a small community. 


20



Achieving UV Disinfection Credit for Pre-UVDGM Era UV Facilities: 

Experiences of Two UV Facilities 

Christine Cotton, P.E., and James Collins 

Malcolm Pirnie, Inc., S. Church Ave, Suite 1120, Tucson, Arizona 

The development of the United States Environmental Protection Agency (USEPA) Ultraviolet Disinfection 

Guidance Manual (UVDGM) was a six-year process, and the Final UVDGM was released in November 2006. 

However, several drinking water utilities did not wait for the UVDGM to be finalized to install UV disinfection 

because they wanted to provide additional public health protection earlier. Therefore, these utilities were designed 

and operated while the UVDGM was under development. 

Now that the UVDGM is finalized, some of these utilities desire UV disinfection credit for their operating UV 

facilities. However, there are key differences in the UV facilities validation, and operation compared to the Final 

UVDGM recommendations. This paper will describe the following items and how these items affect receiving 

disinfection credit. Also, two case studies are briefly described. 

• Design criteria refinement 

• UV equipment changes and ramifications 

• Validation calculation technique changes 

• UV disinfection monitoring and recording 

• Potential regulatory agency coordination 

21 


Monday AM – Session 3: Ozone Design and Operation – S3-1 


Ozone Measurement and Control in Drinking Water Treatment Plants 

Andrew Wright, Ph.D., and Victor Dosoretz 

IN USA Inc., 100 Morse St., Norwood, MA, 02062 

Effective process measurement of ozone in water treatment facilities, where ozone is used to disinfect drinking 

water, enables optimized ozone usage and enormous resultant cost savings on a daily basis. Dedicated sensors for 

process measurement often exhibit limitations such as excessive noise, signal interferences, and down time. UV 

absorption by ozone offers particular capabilities with regard to these limitations: Principles of measurement are 

presented, and sensor concepts for process measurement are discussed. 


22



The Potential Use of Ozone in Municipal Waste Water 

A. Ried, J. Mielcke, and A. Wieland 

ITT W&WW WEDECO, Boschstr. 4-14, 32051 Herford, Germany 

This paper will summarize the potential options applying ozone for the improvement of effluents from waste water 

treatment plants. A specific focus will be on the technical aspects how to integrate ozone technique in existing or 

new conventional treatment plants. Additionally some large scale projects will be illustrated, where this technique 

is in operation yet. The following aspects are of interest and will be discussed: 

• necessary ozone dose range (depends on application, water matrix and contaminants) 

• required components of ozone systems (ozone generator, gas supply, reaction system, off-gas handling) 

• process control, online measurement 

• potential parameters to be used for process control 

• design guidelines for the integration of ozone systems 

• cost calculations. 

23 




Control of Iron and Manganese Ozone Removal 

by Differential Turbidity Measurements 

Vadim Malkov, Mike Sadar, Jon Schiller, and Eric Lehman 

Hach Company, 5600 Lindbergh Dr. Loveland, CO 80538, USA 

A new method for continuous monitoring of ozone concentration and the effective removal of iron and manganese 

was tested. 

The offered alternative to the ORP system was comprised of two self-cleaning turbidimeters. The turbidimeters 

were installed at the same locations as the ORP sensors and initial calibration test was performed with different 

ozone dosage. 

The conducted long term monitoring study showed stable performance of the differential turbidity system. 

The system confirmed the continuous and desired result of increased turbidity immediately after oxidation of the 

unwanted iron and manganese species. Therefore, the method can be expanded to other similar applications 

involving ozone. 


24



Optimizing an Intermediate Ozone System used for Primary 

Disinfection at a 55 MGD Surface Water Treatment Plant 

Russ Navratil 1 , Chip England 1 , and Glenn Hunter 2 

1. Henrico County, Virginia 

2. Process Applications Inc. 

The Henrico County VA Water Treatment Facility has been in operation since April 2004, making use of 

intermediate ozone for primary disinfection to take advantage of both the disinfection and DBP benefits. Since the 

summer of 2007 the staff at the Henrico WTF have embarked on an optimizing journey with their ozone system. 

This paper summarizes the significant milestones accomplished on this journey as well as ongoing improvements. 

Optimizing efforts to reduce operating costs while achieving disinfection goals are reviewed relative to: 

• Staff training workshops 

• Automating ozone data collection and access 

• Operating ozone generators in optimum ozone concentration range 

• Optimizing ozone contactor operation including residual sampling locations and number 

of contactors 

• Overcoming minimum gas flow limitations 

• Contactor solenoid ozone residual sampling system issues and improvements 

• Cost savings achieved through optimization 

Each of these items will be discussed following an overview of this 55 MGD surface water treatment facility. 

25 


Monday PM – Session 4: UV Case Studies – S4-1 


UV System Technology Evaluation Using UV Cost Analysis Tool 

for Metro Vancouver’s Coquitlam UV Disinfection Project 

Ayman Shawwa, P.E., Ph.D., BCEE 1 , Chris Schulz, P.E., BCEE 2 , 

Inder Singh, M.A.Sc. P.Eng. 3 , and James Kim, P.E. 1 

1. CDM, Walnut Creek, CA 

2. CDM, Denver, CO 

3. Metro Vancouver, BC, Canada 

Metro Vancouver is planning a new 1,200 ML/day UV disinfection facility for the Coquitlam supply to meet 

Health Canada’s new requirements for 3-log Cryptosporidium inactivation. To select a UV system that will provide 

high disinfection performance cost effectively, medium-pressure (MP) and low-pressure high-output (LPHO) UV 

systems were evaluated using UV Cost Analysis Tool (UVCAT) computer model. 

UVCAT results confirmed that all UV systems could meet UV dose delivery requirement for 3-log 

Cryptosporidium inactivation for the full range of design flow and UVT and with a 10-unit train configuration. 

UVCAT also confirmed that capital and operations and maintenance costs for UV systems designed based on T1 

RED (reduction equivalent dose) were significantly lower than those based on MS2 RED design. 


26



Brockton, Massachusetts Commissions a 60-mgd (227-ML/d) 

UV Wastewater Disinfection System 

William C. McConnell, P.E., and David A. Norton 2 

1. CDM, 56 Exchange Terrace, Providence, RI 02903 

2. City of Brockton, MA, 303 Oak Hill Way, Brockton, MA 02301 

The Brockton Advanced Wastewater Treatment Facility (WWTF) recently completed an $80 million capital 

improvement program increasing design capacity to 20.5 million gallons per day (mgd) (77.5 million liters per day 

(ML/d)). A key component of the facility improvements was replacing the effluent disinfection system. The 

existing sodium hypochlorite disinfection and sodium bisulfite dechlorination systems were replaced with an 

ultraviolet (UV) disinfection system capable of treating peak flows up to 60 mgd (227 ML/d). The new UV 

disinfection system became operational in August 2008 and has successfully completed its first disinfection season, 

which runs from April 1 through October 31 each year. 

27 




Site Specific Testing of UV Disinfection at a Trickling Filter Plant 

Gary Hunter, P.E. 1 , Anjana Kadava 1 , Jane Hood 2 , and Don Gilpin 2 

1. Black & Veatch, 8400 Ward Parkway, Kansas City, MO 64114 

2. City of St. Joseph, MO 

The St. Joseph WPCP currently has no existing disinfection facilities. With the Missouri Department of Natural 

Resources (MDNR) moving toward requiring all National Pollutant Discharge Elimination System (NPDES) 

permit holders to disinfect plant effluent. The e Coli permit limit indicated in a proposed permit received by the 

City on February 26, 2009 is anticipated to be a 30 day mean of 206 E. coli colonies per 100 ml with no single 

sample maximum. Both bench scale and demonstration testing were conducted for both: 

• UV Low Pressure – High Intensity UV 

• Bulk Sodium Hypochlorite 

Additional water quality data was also collected during the testing to help establish the design parameters for the 

UV systems. UV demonstration study was completed comparing the Trojan 3000+ and WEDECO TAK 55 from 

May 21, 2009 to August 31, 2008. This technical memorandum provides a summary of the results of both the 

bench and demonstration scale testing. Results of this study indicate that UV can be effectively used to achieve the 

disinfection requirements at this plant. 


28



Ultraviolet Light Disinfection System Conceptual Design 

for the Massachusetts Water Resources Authority 

John J. Carroll Water Treatment Plant 

Albert J. Capuzzi 1 , Brian Loux 1 , Paul Swaim 1 , and James P. Malley 2 

1. CH2M HILL 

2. University of New Hampshire 

Massachusetts Water Resources Authority (MWRA) currently treats its water supply to 2.3 million people in the 

metropolitan Boston area at its 405 million gallon per day John J. Carroll Water Treatment Plant located in 

Marlborough, Massachusetts. The plant came on-line in July 2005. The Carroll WTP does not include filtration 

due to the high quality of the source water. MWRA will add UV disinfection to comply with the Long Term 2 

Enhanced Surface Water Treatment Rule requirements for a second primary disinfectant and Cryptosporidium 

inactivation. This paper will discuss the Existing Ozonation Facility, Regulatory Requirements, Water Quality, 

including the impact of ozone on ultraviolet light transmittance, the overall Disinfection Strategy, the conceptual 

design, Ultraviolet Reactor Technology Comparative Analysis and UV reactor procurement, final design and 

construction process. The design is underway and construction of the UV facilities is scheduled to be completed in 

early 2014. 

29 


Monday PM – Session 5: Ozone Case Studies – S5-1 


Multi-function Sidestream Ozone Treatment 

at a Drinking Water Treatment Plant 

Maxime Beaulieu 1 , Patrick Niquette 1 , Pierre Cullen 2 , and Denis Allard 2 

1. Dessau Inc., Water, Industry and Waste Management, 1080, Côte du Beaver Hall, Suite 300, 

Montreal (Quebec), Canada, H2Z 1S8. 

2. City of Laval, Department of environmental city management, 3810 Levesque West, Laval (Quebec), 

Canada, H7V 1A0. 

With the increasing demands placed upon water treatment plants to provide higher quality water and the advent of 

high concentration oxygen fed ozone generators, ozone treatment is becoming ever more useful. This article looks 

at the design of a new multi-function intermediate ozonation system for a treatment plant in Laval, Quebec, that 

poses particular design challenges. A three sidestream, multiple injection manifold using variable speed pumps and 

oxygen degassing, was found to provide efficient disinfection, taste and odor control and pretreatment for 

downstream biological filtration. The ozone injection system is designed for maximum flexibility in order to meet 

the large flow rate and ozone dose range required at this particular plant. 


30



Rising Energy Costs and Frozen Budgets: 

Getting More from Our Operating Buck 

David W. Coppes 

Western Operations, Massachusetts Water Resources Authority, 266 Boston Road, Southborough, MA 01772 

The Massachusetts Water Resources Authority (MWRA) uses ozone at its 405-MGD John J. Carroll Water 

Treatment Plant. The purpose of ozonation is to attain primary disinfection to provide for Cryptosporidium 

inactivation, plus meet or exceed regulated values for Giardia and virus log inactivation credit. 

While ozone production has gotten more efficient with the advent of medium-frequency ozone generators, it still 

consumes a lot of power. A recent energy audit prepared for MWRA determined that ozone generation accounts 

for approximately 66% of the electricity used at the plant. MWRA has made a commitment to reducing energy 

consumption at its facilities in an effort to reduce both operating costs and the environmental impacts of its 

daily operations. 

This paper will describe the ways that MWRA tracks its ozone production costs, will describe some of the 

operating decisions made to improve efficiency, and show a trade-off between efficiency and system reliability. 

Some of the items to be covered include: Dose control: improved performance reduces overall cost; Selecting the 

optimum ozone concentration operating point and modifying control strategy to maintain the selected target. 

31 




Key Water Quality Parameters that Determine Ozone Dose 

for Massachusetts Water Resources Authority 

Windsor Sung, Ph.D., P.E. 

MWRA, 260 Boston Road, Southborough, MA 01772 

MWRA supplies unfiltered surface water to over 2 million people in the metropolitan Boston area. Primary 

disinfection to inactivate giardia and crypto is achieved by ozone. Control of ozone dose is determined by 

a computer algorithm that uses a pre-determined ratio of required versus achieved CT and measured ozone 

residuals. On a monthly averaged basis the ozone dose is mainly dependent on only two main water quality 

parameters: temperature and ultra-violet absorbance at 254 nm. Development and use of the regression equation 

will be presented. 


32



Treatment of Wastewater with Ozone at the 

Southwest Wastewater Treatment Plant 

Nick Burns 1 , Jeff Neemann 1 , Tom Holst 2 , and Jim Burks 2 


2. Springfield Utilities, 3301 S. FF Hwy, Springfield, MO 65807 

The City of Springfield, MO has selected Black & Veatch to upgrade the ozonation facilities at its Southwest 

Wastewater Treatment Plant. Design challenges included a lack of operable instrumentation that prevented 

evaluation of historical operating data, and operation of upstream processes that resulted in rapid changes in ozone 

demand. The paper will include a discussion of the impacts of upstream processes on ozone demand; the results of 

the bench-scale analyses in terms of log reductions of fecal coliforms and E-coli; and the impact of ozone on UVT 

in primary and tertiary treated wastewater. 

33 


Monday PM – Session 6: Ozone Design and Operation – S6-1 


Optimization Considerations for an Ozone Side Stream Injection System 

Bill Mundy, C.E.T. 1 , Kerwin Rakness 2 , and Glenn Hunter 2 

1. Regional Municipality Of Halton, 1151 Bronte Road, Oakville, Ontario, Canada, L6M 3L1 

2. Process Applications Inc., 2627 Redwing Drive, Fort Collins, Colorado, USA, 80526 

The Oakville Water Purification Plant (OWPP), located in the Regional Municipality of Halton, Oakville, Ontario 

has a capacity of 110 ML/d. The OWPP has an ozonation sidestream injection system designed for 

cryptosporidium inactivation, including taste & odour removal capability. 

The OWPP side stream injection system has three side stream injection systems, (2 firm capacity and one standby) 

each with variable speed controllers for process optimization. 

It was demonstrated through optimized process control that the Gas/Liquid ratio can be adjusted to balance ozone 

transfer and cost effectiveness. Other sidestream parameters evaluated included outlet venturi pressure, ozone 

demand and initial residual. 


34



Evaluating Options for Retrofitting a Large Scale Ozonation System in Texas 

Jeff Neemann 1 , David Timmerman 1 , Robert Hulsey 1 , Buford Green 2 , and Steve Long 2 

1. Black & Veatch, Kansas City, Missouri 

2. North Texas Municipal Water District, Wylie, TX 

The North Texas Municipal Water District (NTMWD) is in the process of preliminary engineering design of 

ozonation at the 770 million-gallons-per-day Wylie Water Treatment Plant (WTP) Complex. The design will 

include the addition of ozone technology for drinking water disinfection as well as taste and odor control at the 

Wylie, Texas, complex that serves more than 1.5 million customers. Preliminary design was completed by April 

2009, and final design is expected to be completed in April 2010. The project should be operationally complete in 

2013. 

The preliminary design has included pilot testing of preozonation and intermediate ozonation to evaluate the 

advantages and disadvantages of both application points. Testing was completed to evaluate the TOC removal, 

disinfection by-product formation potential, and filter productivity of both ozonation locations. Additional testing 

was done to evaluate the use of chlorine dioxide, chlorine/ammonia, ammonia only, and pH adjustment to limit 

bromate formation during background and spiked bromide concentrations. Taste and odor testing was conducted to 

determine the ozone dose required to remove MIB and Geosmin and sampling showed substantial removal in the 

biological filters with GAC. 

35 




Keeping Ozone Generators Dry and Cool 

Kerwin L. Rakness 1 and James Muri 2 

1. Process Applications, Inc., 2627 Redwing Rd., Suite 340, Fort Collins, Colorado 80526 

2. John J. Carroll Water Treatment Plant, 84 D’Angelo Drive, Marlborough, MA 01752 

Ozone generators perform efficiently and continuously (less maintenance) when kept dry and cool while in service, 

and dry when in standby condition. It is the authors’ experience that ozone generators at some plants operate years 

and years without maintenance, while generators at other plants require maintenance within months or a few years. 

In review, commonality of well performing ozone generators is dry operating condition. 

Feed-gas “wetness” is monitored during normal ozone operation via dew point temperature. Alarm and shut-down 

occurs at elevated dew point temperature, such as -60 o C, which is 7-ppm wt moisture content at 1-atm pressure. 

Normal operation is dew point temperature of -80 o C, which is 1-ppm wt moisture content. 

Generator “dryness” during standby and at startup when power is applied is also important. Off-line generators 

might become “wet” when idle due to improper standby conditions. Pre-purging with dry gas is normally 

implemented, but purge time might be insufficient for “wet” generators. Nitric acid is formed in the presence of 

dinitrogen pentoxide (formed during ozone production) and water, thus dry conditions are high priority at startup, 

during normal operation and when in standby. Methods to maintain dry conditions are discussed in this paper. 

Cooling water keeps generators “cool” and electrically efficient. Generator cooling water flow rate maintains 

generator inlet-versus-outlet cooling water below 10 o F temperature rise, and often below 5 o F rise. Non-corrosive 

and non-scaling cooling water is critically important for long-term (20+ years) maintenance-free performance. 

Closed-loop-open-loop cooling systems promote this desired outcome. Cooling water flow and temperature details 

are outlined in this paper. 


36



Application of Ozone for Contaminant Oxidation in Wastewater 

Eric C. Wert, Fernando Rosario-Ortiz, and Shane Snyder 

Southern Nevada Water Authority, P.O. Box 99955, Las Vegas, NV USA. 

Ozone has been shown to be a promising treatment technique for the oxidation of trace organic contaminants in 

wastewater. However, achieving significant ozone oxidation in wastewater can be challenging due to higher 

concentrations of total organic carbon (TOC). Greater TOC concentrations can increase ozone demand and 

accelerate ozone decay rates, which reduces ozone exposure. In the current study, several trace organic 

contaminants (i.e. pharmaceuticals and endocrine disrupting compounds) were studied under a range of ozone 

exposures in three wastewaters. Contaminant oxidation was assessed using ozone exposure and the O 3 :TOC ratio. 

Results showed that the ozone exposure was different for each wastewater based upon the O 3 :TOC ratio. Second 

order reaction rate constants were used to identify whether contaminants were removed primarily by O 3 or 

hydroxyl radicals. When O 3 exposure was measurable, >95% removal was observed for contaminants that were 

fast-reacting with ozone. UV 254 removal was also found to be a good surrogate to assess contaminant oxidation in 

the absence of measurable dissolved ozone residual (



Approach for Achieving Sustainable Operation of the 

2-bgd Catskill/Delaware UV disinfection Facility 

Matthew T. Valade, P.E. 1 , Steven Farabaugh 2 , Paul D. Smith, P.E. 3 , and Gary Kroll, P.E. 4 

1. Hazen and Sawyer, P.C., 24 Federal Street, Suite 302, Boston, MA 02129 

2. Hazen and Sawyer, P.C., 498 Seventh Avenue, 11 th Floor, New York, NY 10018 

3. NYC Dept. of Env. Protection, 96-05 Horace Harding Expy, Corona, NY 11368 

4. CDM, Raritan Plaza 1, Raritan Center, Edison, NJ 08817 

Recent advances in testing methods are being applied to the validation of NYC’s Catskill/Delaware UV equipment. 

These advanced methods will allow the full scale facility to operate in a more sustainable manner with up to 50% 

reduction in operating power requirements (and corresponding reduction in carbon dioxide emissions) and savings 

of over $1 million annually. 


38



Feasibility of Ultraviolet Disinfection of A WWTP Final 

(Blended) Effluent under Wet Weather Flow Conditions 

Khalil Z. Atasi, Ph.D., P.E., BCEE, F.ASCE 

Camp Dresser & McKee Inc., 2301 Maitland Center Parkway, Suite 300, Maitland, FL 32751 

Ultraviolet light (UV) disinfection has gained tremendous popularity in wastewater disinfection over traditional 

chemical disinfection processes using chlorine gas and other chlorine compounds for many reasons. Mainly, UV 

disinfection offers a safe process by eliminating the use of a dangerous gas and eliminates the production of toxic 

disinfection byproducts. UV also eliminates the need for chlorine residual removal (dechlorination) using another 

chemical reducing reagent. Thus, UV disinfection replaces two processes, eliminates completely the on-site storage 

of dangerous chemicals, and eliminates the whole effluent toxicity (WET) that may result from chlorine based 

disinfection process. 

A wastewater treatment plant (WWTP) located in ten Midwest has conducted an evaluation for the feasibility of 

UV disinfection to replace its existing chlorine disinfection process and dechlorination process. This large plant, 

nested in a residential area, handles by NPDES permit 36 MGD of dry weather flow and up to 60 MGD of wet 

weather flow. The plant is a tertiary treatment facility that employs multimedia gravity filtration to meet a tight 

NPDES permit effluent limits for total suspended solids, BOD5, and ammonia. Because of the significant wet 

weather flow component, the UV disinfection process has to be carefully evaluated as to its effectiveness. UV light 

transmission can be a limiting factor to achieve final effluent disinfection permit requirement. 

The presentation will provide information useful to other treatment plants, particularly those with significant wet 

weather flow component, considering UV disinfection as a replacement of the traditional chlorine disinfection 

process. Specifically, the presentation will discuss, among other things, the following: 

• Required testing to evaluate the UV transmission under worst case scenario of “blended” final 

effluent quality 

• Various technology of UV disinfection form the perspective of lamp pressure and light intensity 

• Impact of the process foot print and retrofit within the existing chlorine contact chamber 

• Life cycle cost of the various UV technology (pressure/intensity) 

• Impact on the plant hydraulic profile 

39 




Bidding, Testing, and Start-Up of a Reuse UV Disinfection System in Florida 

Josefin M. Edeback, E.I. and Melanie A. Mann, P.E. 

Hazen and Sawyer, P.C., 10002 Princess Palm Avenue, Suite 200, Tampa, Florida 33619 

Hillsborough County, Florida recently installed a new UV disinfection system for reuse at the Falkenburg 

Advanced Wastewater Treatment Plant (AWTP) as part of a plant expansion from 9.0 MGD to 12.0 MGD annual 

average daily flow (AADF). The Falkenburg AWTP must meet Florida’s requirements for high level disinfection 

(HLD) for both its surface water discharge permit and its public access reuse permit. Construction plans and 

specifications allowed the UV facility to use equipment with either horizontal or vertical UV lamps and allowed 

bidders to select from three named manufacturers. During construction, before the bidder-selected UV equipment 

submittal was approved for fabrication, the UV manufacturer was required to prove the effectiveness of its 

mechanism for controlling lamp sleeve fouling with a pilot-scale demonstration at the Falkenburg AWTP. Once 

installed, Hillsborough County was required to obtain approval from the Florida Department of Environmental 

Protection (FDEP) of a UV Operating Protocol prior to placing the new UV system in service. Performance testing 

of the UV system is in progress and results to date are summarized. 


40



Validation of the Catskill/Delaware UV Reactor: 

A Comparison of Biodosimetry and Lagrangian Actinometry Methods 

Chengyue Shen 1 and Karl Scheible 1 , Matthew Valade 2 , and Ernest R. Blatchley 3 

1. HydroQual, Inc. Mahwah, NJ 

2. Hazen and Sawyer, P.C., Boston, MA 

3. Purdue University, West Lafayette, IN 

The LPHO UV disinfection system designed for the New York City Catskill/Delaware UV Disinfection Facility 

will be validated in parallel by UVDGM biodosimetric protocols and by Lagrangian actinometry using dyed 

microspheres. This validation will complement and supplement prior validation testing that had been performed on 

the unit, covering a broader operating range and allowing for improved operating efficiencies by directly measuring 

and characterizing the dose-distribution of the UV unit within its anticipated operating envelope. The ability 

to directly measure the dose-distribution in a UV reactor significantly impacts the UVDGM uncertainty factors 

(e.g., RED bias) associated with the design sizing and subsequent operating energy and lamp replacement costs of 

an installation, particularly for larger water utilities. All testing was conducted at the UV Validation and Research 

Center in Johnstown, NY. This presentation will show the field data analysis techniques and a direct comparison 

of the Lagrangian actinometry validation approach to that of conventional biodosimetry. 

This work has been conducted as a tailored collaboration supported by the NYCDEP, Trojan Technologies, Water 

Research Foundation (formerly Awwa Research Foundation). The project demonstrates the Lagrangian 

actinometry validation protocol that was developed with the support of AwwaRF in partnership with the New York 

State Energy Research and Development Authority. All biodosimetry and related technical testing is in 

conformance with the UVDGM. The validation test matrix encompasses simultaneous validation via Lagrangian 

actinometry using dyed microspheres and biodosimetry using MS2 and T1 coliphage. The test matrix was designed 

to validate an operating envelope defined by four operating variables: Flow, UVT, Power Input, and Number of 

Lamps. QA protocols presented in the UVDGM are carried through to the Lagrangian actinometry protocols. 

These establish field and lab practices and QC limits with respect to microbiology, flow cytometry and field 

sampling activities. 

The advantages associated with the test series, particularly with respect to using the dyed microspheres to measure 

the dose distribution lie primarily in the ability to reduce the validation factor, which, in turn, reduces the system’s 

operating requirements. This does not represent a reduction in safety – rather, it is a reduction in the uncertainty of 

the validation tests. Additionally, by having this information, one can determine the log inactivation of other 

pathogens and newly identified microorganisms of concern that can be accomplished by the UV units, without the 

need for extensive full-scale re-validation testing. Measuring the actual dose-distribution delivered by the UV unit 

across its validated operating range also allows one to validate CFD-intensity models that can be used for 

optimization of the system’s operations, and for interpolation of process performance at operating conditions that 

are intermediate to those applied in the test matrix. 

41 




Updating Ozone for the Lincoln Water System 

Jeff Neemann 1 , Nick Burns 1 , Robert Hulsey 1 , Andrew Hansen 1 , Eric Lee 2 , and John Miriovsky 2 


2. Lincoln Water System, Lincoln, NE 

The Lincoln Water System (LWS) in the process of replacing their three existing ozone generators with two larger 

generators. The new, state-of-the-art ozone system will use less energy to produce more ozone for disinfection at 

their East Water Treatment Plant. The upgrade will increase the total ozone generation capacity at the treatment 

plant from 1,050 pounds per day (ppd) to 2,600 ppd. The new generators will use liquid oxygen rather than air to 

produce ozone, which will also increase efficiency. Another aspect of the project is replacement of all controls, 

computers and electronics in the plant. This work will be coordinated with the construction activities scheduled for 

a Supervisory Control and Data Acquisition (SCADA) system upgrade to improve system efficiency. The SCADA 

system monitors and controls transmission and distribution of raw and potable water supplies. Preliminary design 

and equipment procurement services were completed in 2008, with final design slated for completion in May 2009 

and construction set to begin September 2009. The project is anticipated to be complete in April 2010. 

The existing air fed system will be replaced with liquid oxygen and ambient vaporizers to generate ozone at high 

weight percent. A cost evaluation was conducted and it was determined that it was most cost effective to complete 

replace the existing ozone generators with new more efficient generators. The existing closed loop cooling water 

system will be expanded to handle the higher cooling water flows. The existing diffuser system will be replaced 

with a sidestream injection system that uses injectors and specially designed nozzles that will retrofitted in to the 

existing concrete contactors. The ozone destruct system will be modified to handle the reduced gas flows after the 

conversion to oxygen feed. 


42



Eastern Treatment Plant - Melbourne Water’s Approach to One of the 

World’s Most Complex Wastewater Technology Trials 

Mark Lynch 1 , John Mieog 1 , Clare McAuliffe 1 , Bruce Long 2 , 

Sock-Hoon Koh 2 , and Johanna Steegstra 3 

1. Melbourne Water Corporation; Melbourne, Australia 


3. Kellogg Brown & Root Pty Ltd, Melbourne, Australia 

In October 2006 the Victorian Government announced that Melbourne Water’s Eastern Treatment Plant (ETP) 

would be upgraded to produce ‘Class A’ effluent by 2012. The ETP treats approximately 42 percent of the sewage 

from Melbourne’s southern and eastern suburbs. At average and peak flows of around 370 and 700 MLD 

respectively, the ETP tertiary treatment plant will be amongst the largest of its kind in the world. 

Tertiary filtration followed by UV and chlorine disinfection is capable of achieving Class A effluent quality; 

however it will not address the residual aesthetic issues of colour and odour associated with the ETP effluent. 

The opportunity exists to implement tertiary treatment in such a way that achieves Class A effluent quality, but also 

addresses the residual aesthetics through the use of advanced treatment processes such as ozone/ biologically 

activated carbon. 

Due to the scale of the tertiary treatment at ETP, the likely cost implications, and the need to assess the viability of 

advanced treatment on ETP effluent, a trial facility was designed, constructed and commissioned within 12 months. 

The facility includes all feasible tertiary treatment technologies for a plant the scale of ETP, including dual, cloth 

and mono media filtration, micro and ultrafiltration membranes, ozone, biologically activated carbon, UV and 

chlorine disinfection and reverse osmosis. 

Through the innovative design and construction process of the plant, it is possible to operate multiple process train 

configurations and all 16 individual process units simultaneously. Each process train treats approximately 100kL/d 

making the total flow through the plant approximately 2ML/d. 

This paper will discuss the design of the trials, construction of the plant and operation of the site to achieve the key 

objective of deciding on a preferred process train for the full scale plant. 

43 




Operations Experience and Enhancements to the Two-stage 

Ozone System for the Cary/Apex, NC Water Treatment Plant 

Bill Dowbiggin and Kelvin Creech 

1. CDM 

2. Town of Cary 

Ozonation was added to the Cary/Apex North Carolina Water Treatment Plant in 2001 with the primary purpose of 

taste and odor control and secondary desire to provide an extra treatment barrier in terms of oxidation/disinfection. 

This presentation will overview the results and recent enhancements that are being considered and some that have 

already been implemented. Ozone, for example, has allowed great reduction in the use of powdered activated 

carbon (PAC) for taste and odor control, which provided significant saving in terms of both PAC purchase and in 

terms of sludge disposal. 

Recent enhancements to be overviewed relate to process control, system corrosion control including the results of 

diagnostic testing of some corrosion, and considerations for control of taste and odor and for providing a 

disinfection barrier. 

Discussion of recent findings by others that ozone can provide a barrier to many endocrine disruptors, 

pharmaceuticals and personal care products will be discussed briefly with respect to how those results and doses 

compare to the Town’s typical ozone doses. 

The requirements of the State of North Carolina for ozone primary disinfection will also be overviewed. 


44



Treated Water Quality Enhancements 

from Ozonation in a Tertiary Plant Upgrade 

John Mieog 1 , Mark Lynch 1 , Clare McAuliffe 1 , Bruce Long 2 , 

Sock-Hoon Koh 2 , and Johanna Steegstra 3 

1. Melbourne Water Corporation; Melbourne, Australia 


3. Kellogg Brown & Root Pty Ltd, Melbourne, Australia 

The Victorian Government announced in 2006 that Melbourne Water would implement upgrades to its Eastern Treatment Plant 

(ETP) to enable it to produce ‘Class A’ recycled water quality in 2012 which will necessitate the implementation of a tertiary 

treatment plant comprising filtration and advanced disinfection. 

The ETP treats approximately 42 percent of the sewage from Melbourne’s southern and eastern suburbs. At average and 

peak flows of around 370 and 700 MLD respectively, the ETP tertiary treatment plant will be amongst the largest of its kind in 

the world. 

Melbourne Water elected to consider going beyond Class A criteria to address residual aesthetic parameters, colour and odour, in 

particular. This would address amenity impacts of the plant’s marine discharge, provide greater opportunities for reuse of the 

reclaimed water and thereby further reduce environmental impact through recycling diversions, and provide a valuable additional 

tool to help Victoria cope with extended drought periods such as the one being experienced today. 

Numerous treatment technologies were investigated and the most promising ones were chosen for application-specific testing. 

Due to the large scale at which these technologies would be applied, Melbourne Water elected to design and construct a 

tertiary technology trials plant in which to confirm the effectiveness of individual unit processes as well integrated process trains. 

Ozonation followed by biologically active media filtration (BMF) was selected to improve the aesthetic quality of the 

treated water. 

Pilot trials run to date have demonstrated considerable water quality improvements as well as synergistic impacts on downstream 

treatment processes. Ozone doses between 8 and 15 mg/L have been tested and found to effect substantial reductions in true 

colour as well as increased UV transmittance (UVT). The 5 th percentile unfiltered secondary effluent UVT is increased from 33 % 

to 55% at ozone doses between 8 and 10 mg/L. This has a dramatic impact on the capital and operating costs for possible 

downstream UV irradiation. Cost comparisons of process trains that include ozone/BMF preceding UV irradiation compared with 

those that did not include ozone/BMF concluded that the ozone process more than pays for itself in reduced UV costs. 

Suspended solids challenge testing was performed to evaluate the effectiveness of ozone at removing true colour and increasing 

UVT at elevated concentrations of feed water total suspended solids. Data revealed that equivalent amounts of true colour were 

removed per milligram of ozone transferred for influent suspended solids levels as high as 45 mg/L. The same performance was 

found for UVT increase at elevated influent suspended solids concentrations. At an influent suspended solids concentration of 214 

mg/L, the colour change reduced from 82 to 65%. 

Ozone/BMF together were also found to achieve a high degree of nitrification of influent ammonia. BMF effluent ammonia 

concentrations were achieved following filtration through either anthracite or granular activated carbon media and at empty bed 

contact times less than 10 minutes. This is a particularly significant benefit as it enables the use of free chlorine as an additional 

viricidal barrier for the production of high quality reclaimed water. 

Operation of ultrafiltration membranes before and after ozone/BMF has demonstrated the capability of these membranes to 

operate effectively at flux rates around double the sustainable flux when treating direct secondary effluent. Ozone followed by 

BMF has been found to be a valuable process addition to the treatment process trains we have trialed. The further effectiveness of 

ozone at achieving substantial virus inactivation (as presented in a separate abstract submission) while concurrently achieving the 

multiple benefits described above has clearly demonstrated a valuable role that ozone can play in enhancing the acceptability of 

reclaimed water schemes. 

45 




Inline Multi-Jets Ozone Contactors: Performance and Scalability 

Mahad S. Baawain 1 , Mohamed Gamal El-Din 2 , Daniel W. Smith 2 , and Angelo Mazzei 3 

1. Department of Civil & Architectural Engineering, Sultan Qaboos University, Muscat, Oman 

2. Department of Civil & Environmental Engineering, University of Alberta, Edmonton, Canada 

3. Mazzei Injector Corporation, Bakersfield, CA 

The hydrodynamic characteristics of three scales of in-line multi-jets ozone contactors were studied by using 

a laser flow map particle image velocimetry coupled with planar laser induced fluorescence (PIV/PLIF). All 

measurements were conducted under total liquid flow rate of about 10 L/s (for 0.10 m diameter contactor), 5.5 L/s 

(for 0.075 m diameter contactor) and 2.5 L/s (for 0.051 m diameter contactor) with gas flow rate ranging from 0.05 

to 0.4 L/s (for 0.10 m diameter contactor), 0.03 to 0.24 L/s (for 0.075 m diameter contactor) and 0.05 to 0.1 L/s (for 

0.051 m diameter contactor). The gas was introduced to the contactors through side injectors aligned in opposing or 

alternating positions. Results showed that for the same number of jets and at the same gas flow rate, the liquid 

dispersion coefficient (D L ) was higher when the alternating alignment was applied. D L increased as the size of the 

reactor increased. On the hand, higher ozone mass transfer rates were observed when using opposing alignment. 

Furthermore, as the cross-sectional area (i.e., the size) of the reactor increases, the mass transfer rate increases. 


46



Operator-Friendly Technique and Quality Control Considerations 

for Indigo Colorimetric Measurement of Ozone Residual 

Kerwin L. Rakness 1 , Eric C. Wert 2 , Michael Elovitz 3 , and Suzanne Mahoney 4 

1. Process Applications, Inc., 2627 Redwing Rd., Suite 340, Fort Collins, Colorado 80526 

2. Southern Nevada Water System, P.O. Box 99955, Las Vegas, NV 89193 

3. Treatment Technology and Evaluation Branch, Water Supply & Water Res. Division, U.S. EPA, 26 West 

M.L. King Drive, Cincinnati, OH 45268 

4. Little Falls Water Treatment Plant, Passaic Valley Water Commission, 800 Union Boulevard, Totowa, NJ 

07512 

Drinking water ozone disinfection systems document ozone residual concentration, C, for regulatory compliance 

reporting of concentration-times-time, CT, and resultant log inactivation of virus, Giardia and Cryptosporidium. 

The indigotrisulfonate (ITS) “colorimetric” procedure is the Standard Method for manually measuring ozone 

residual. Although the method as currently written in Standard Methods is relatively easy to implement, its 

accuracy nonetheless depends on specific ITS quality control considerations. Also, Standard Methods protocol is 

based on specific quantities of materials and sample volumes, making the method somewhat inflexible. Tests are 

often performed in plant surroundings by operating staff, as opposed to in “certified” laboratories by analytical 

chemists. In this paper a more flexible, quality-assured and “operator-friendly” technique for the ITS method 

is presented. 

Indigo colorimetric testing described in this paper includes methods to account for apparent ozone residual due to 

oxidized manganese. Also described are special study results that document consequences for ignoring certain 

conditions. For example, ITS solution stored on a shelf for several days can cause an appreciable under-estimation 

of true ozone residual. Storage for several weeks can cause a major under-estimation of true ozone residual. Other 

special study results suggest increased flexibility is possible without negative consequence, as compared to the 

method currently outlined in Standard Methods. 

47 




Highly Efficient High Concentration Photochemical Ozone Generation 

Daniel E. Murnick 

UV Solutions Inc. and Rutgers University, Newark NJ 07102 

Using new highly efficient long lived 172 nm lamps we have demonstrated photochemical production of ozone at 

specific energy of 3 kWh/lb (6.6 kWh/kg, 150 gm/kWh) at 5% O 3 by weight with air as a feed gas. Similar results 

have been obtained using oxygen as a feed gas at 10% O 3 by weight. No NO x is produced as nitrogen is invisible to 

172 nm light. 

Test results agree well with theoretical predictions i and indicate significant O & M cost reduction opportunities for 

large facilities, and the potential of eliminating the need for LOX storage facilities. Capital costs are projected to be 

similar to, or less than those for discharge production systems- depending on system size. 

The all quartz 172 nm lamps operate in most gas or liquid environments resulting in the possibility of generating 

ozone with a wide range of concentrations and process parameters such as pressure and temperature. The lamps are 

instant start and stop, with VUV light production efficiency essentially independent of duty cycle. The high 

efficiency of the lamps and the photochemical ozone production lower cooling requirements compared to those of 

existing systems. As with existing ozone generators, ozone yield and upper ozone concentration limit are strongly 

influenced both by water vapor in the process gas stream and the ambient temperature. 

i 

Influence of Water Vapor on Photochemical Ozone Generation with Efficient 172nm Xenon Excimer Lamps, 

Manfred Salvermoser, Daniel E. Murnick and Ulrich Kogelschatz, Ozone Science and Engineering, 30, 228-237 

(2008) 


48



The Study on the Ceramic Membrane Wastewater Reuse System 

with Pre Ozonation and Coagulation 

M. Noguchi 1 , M. Aoki 1 , H. Kozono 1 , H. Kouchiwa 2 , and Y.Yoda 2 

1. Metawater ,Co., LTD., Shiroyama Trust Tower. 4-3-1 Toranomon, Minato-ku, Tokyo 105-6029, Japan 

2. Tokyo Metropolitan Government, 2-8-1 Nishishinjuku, Shinjuku-ku, Tokyo 163-8001, Japan 

In recent years, reclaimed water from municipal wastewater treatment plants is becoming increasingly significant 

water resource around the urban areas in Japan. Therefore, new wastewater reuse system using ozonation, 

coagulation and ceramic MF membrane (0.1µm) was developed. This study is the collaborative development with 

Bureau of Sewerage Tokyo Metropolitan Government. The testing equipment is located inside the Shibaura Water 

Reclamation Center in Tokyo Metropolitan Government. The testing was performed using secondary effluent 

treated at the center. The volume of treated water is about 90m 3 /day. We confirmed that a small amount of ozone 

addition and coagulation could significantly improve the membrane filtration performance. The combination of pre 

ozonation and coagulation processes achieves continuous stable membrane filtration with the high filtration flux of 

4m 3 /m 2 /day (167 LMH). A stable membrane filtration could be maintained by controlling ozone dosing rate 

depending on raw water quality fluctuation. The removal of COD (Mn) in raw water was 50 to 60%, and the 

color removals satisfied 80% or higher. The filtrate that was obtained from our pilot study was better than 

Californian standards. 

49 


Tuesday AM – Session 10: UV Disinfection Design – S10-1 


Disinfection Alternatives and Sustainability: 

Energy Optimization, Disinfection Efficiency, and Sustainability 

Gary Hunter 1 , Andy Shaw 1 , Dr. Leonard W. Casson 2 , and Dr. Joe Marriott 2 


2. Department of Civil and Environmental Engineering, 944 Benedum Engineering Hall, 

University of Pittsburgh, Pittsburgh, PA 15261 

The dramatic rise in energy and chemical costs is spurring additional focus on optimizing efficiency of wastewater 

disinfection processes. At the same time, sustainability of disinfection in an increasingly-urbanized world will 

depend in part on the ability to reuse treated effluent as a resource instead of a waste product. 

Following the terrorist attacks of September 11, 2001, and devastation of Hurricane Katrina, the engineering design 

paradigm was broadened to include safety, security and a response to all hazards. The “3-S Design Concept” for 

drinking water and wastewater infrastructure systems was developed 

The “3-S Design Concept” can be used to provide practical guidance for the design and operation of disinfection 

processes and treatment systems in today’s economic environment in a manner that embraces sustainable solutions 

that benefit future generations instead of short-sighted solutions with hidden future costs. Sustainability 

incorporates a triple bottom line approach incorporating economic, environmental, and social factors in to the 

selection of a UV disinfection system. 


50



Airing it Out: Design Considerations for UV Disinfection Installations 

Aaron W. Duke, P.E. 

11242 Waples Mill Road, Suite 250, Fairfax, Virginia 22030 

The use of ultraviolet light for disinfection in drinking water treatment has become increasingly prevalent since the 

findings of Clancy et al., were published in 1998. This increased use has been helped by the promulgation of the 

Long Term 2 Enhanced Surface Water Treatment Rule and the requirement for additional Cryptosporidium 

inactivation for certain source waters. UV disinfection use has also been aided by the increased awareness of 

endocrine disruptors and potential for advanced oxidation to deal with these compounds. The purpose of this paper 

is to provide guidelines for UV disinfection designs relative to air entrainment based upon lessons learned from 

recent installations. 

51 




Impact of Biodosimetry-Based Validation 

on UV System Design Specifications 

Bryan R. Townsend 1 and Gary Hunter 2 

1. Black & Veatch, 8520 Cliff Cameron Drive, Suite 210, Charlotte, NC 28269 


Fueled by recent UV system validations that have been conducted in accordance with testing protocols based on the 

UV Disinfection Guidance Manual, the need for a modernized protocol for the validation, sizing and operation of 

UV systems for the disinfection of secondary wastewater effluent has become increasingly evident. Although the 

development of a modified validation protocol is an important first step in the advancement of wastewater UV 

system design, it is one of several key components to the successful implementation of advanced methods for more 

accurate and reliable UV system design and operation. 

An increasing amount of design specifications are allowing for or require UV system sizing based on validation 

testing, however, many of these specifications do not properly address requirements that should be applied to the 

design and operation of UV systems based on biodosimetry-derived performance models. Many concepts that are 

key to the proper application of biodosimetry results for UV system design are commonly overlooked or 

misunderstood, potentially resulting in under or over design of UV systems and inadequate or inefficient operating 

strategies. Fully understanding the impact of various validation approaches on UV system design will equip 

engineers with the added knowledge to develop proper specifications for safe, accurate and efficient design of UV 

systems that will attain required disinfection goals, while accounting for the site-specific UV dose-response 

requirements of the target microorganism. 


52

Tuesday AM – Session 11: Advanced Oxidation of Contaminants – S11-1 


A Bench-Scale Evaluation of UV and UV/H 2 O 2 Processes for the Removal 

of PPCPs in Secondary Treated Water of Sewage Treatment Plant 

Ilho Kim, Naoyuki Yamashita, and Hiroaki Tanaka 

Research Center for Environmental Quality Management, Kyoto University, 

1-2 Yumihama, Otsu, Shiga 520-0811, Japan 

The side effects of PPCPs on the aquatic environment and human body have not been known yet. However, PPCPs in 

water environment should be removed in aspect of precautionary principles. The performance of UV and UV/H 2 O 2 

processes for the PPCPs removal was investigated using secondary effluent. 38 PPCPs were detected in secondary 

effluent used for tested water in this study. Only 17 of 38 PPCPs were removed by more than 90% despite UV dose of 

2,768 mJ/cm 2 during UV process, showing that considerable UV dose will be required for the effective PPCPs removal 

by UV alone process. This also shows that it will be difficult to accomplish good PPCPs removals by typical UV 

disinfection process (UV dose : 40 mJ/cm 2 ~ 140 mJ/cm 2 ). On the other hand, the PPCPs removal by UV alone process 

improved significantly by the combination of H 2 O 2 with UV process. Except naproxen (>89%), 37 PPCPs were removed 

by more than 90% at the operational condition of UV dose of 923 mJ/cm 2 (contact time : 5 min) and initial H 2 O 2 

concentration of 6.2 mg/L. As a consequence, the combination of UV and H 2 O 2 made it possible to reduce UV dose at 

least by more than 3 times comparing with for UV alone process. Electrical energy required for the effective PPCPs 

removal by UV/H 2 O 2 process was 0.54 kW/m 3 target water (Operational condition : UV dose : 923 mJ/cm 2 , H 2 O 2 : 6.2 

mg/L), showing that UV/H 2 O 2 process can reduce energy consumption and operating cost considerably, comparing with 

UV process. 

53 




The Effects of Vacuum-UV Radiation on Natural Organic Matter 

Gustavo E. Imoberdorf and Madjid Mohseni 

Department of Chemical and Biological Engineering, 

The University of British Columbia, Vancouver, B.C. Canada 

This research focused on examining the efficacy of vacuum-UV (VUV and H 2 O 2 /VUV) processes to degrade NOM 

present in raw water. Both VUV and H 2 O 2 /VUV were very effective at mineralizing NOM. After 90 minutes of 

irradiation, TOC of the water decreased from 4.95 ppm to 0.8 ppm. At shorter irradiation times, partial degradation 

of NOM led to significant changes in water characteristics, such as modifications in the molecular weight 

distribution of NOM as well as formation of oxidation by-products (e.g., aldehydes). 


54



Predicting Hydroxyl Radical Activity and 

Trace Contaminants Removal in Ozonated Water 

Simon Vincent, Abderrahim Kotbi and Benoit Barbeau 

Industrial-NSERC Chair in Drinking Water, École Polytechnique de Montréal, Département des Génies Civil, 

Géologique et des Mines, CP 6079, succ. Centre-Ville, Montréal, QC, H3C 3A7 

There is a renewed interest in predicting R CT following growing evidence that AOP is effective against many 

emerging contaminants. Five surface waters were investigated to evaluate the OH-radical activity using the R CT 

concept, predict R CT using traditional water quality characteristics and predict contaminants removal by ozonation 

and peroxone. It was shown that R CT was dependant on water quality characteristics and could be modeled 

(R 2 =0.97), for four out of five waters, using water characteristics and treatment conditions. Predictions of MIB 

oxidation closely matched the published data of Kawamura (2000) and bench-scale assays performed on one of the 

water under investigation. 

55 


Tuesday AM – Session 12: Perozone and AOP Processes – S12-1 


In-Situ 1,4 Dioxane Remediation in HVOC Sites 

Andrew Brolowski and William B. Kerfoot 

Kerfoot Technologies, Inc., 766-B Falmouth Road, Mashpee, MA 02649 

Increasingly, 1,4 dioxane is found as a co-contaminant at chloroethene spill sites. The compound has shown limited 

removal (



Experiences of Perozone ® and C-Sparge TM 

at Two Former Dry Cleaner Sites in the Netherlands 

Bert Scheffer 1 and Edward van de Ven 2 

1. Verhoeve Milieu bv, Dorpsstraat 32, P.O. Box 4, 6997 ZG Hoog-Keppel, The Netherlands 

2. Verhoeve Milieu bv, Aventurijn 600, P.O. Box 3073, 3301 DB Dordrecht, The Netherlands 

C-Sparge TM , better known as ozone sparging (microbubble ozone), is used for treatment of the plume zone area 

with VOCl, mainly PCE, at a former dry cleaner site in Utrecht . The City of Utrecht has had good results with 

C-Sparge TM in combination with pump and treat. Prior to the application of C-Sparge TM , pump and treat was used 

for removal of mass in the plume until tailing of the groundwater concentrations occurred. The concentrations of 

PCE in the extracted groundwater stagnated at 2,000 ppb. Before start-up of the C-Sparge TM system, a 3-week 

field pilot test funded by the Dutch organization SKB was conducted to study mobilization effects. In the plume 

area, no mobilization effects were found. After that, in September, 2005, C-Sparge TM was started. Together the 

pilot test and full-scale system lowered PCE groundwater concentrations from ppm-level (max. 15 ppm) to low 

ppb-level (400 ppb) in about 125 days. After about 700 days of treatment the PCE groundwater concentrations 

decreased to below the Dutch Intervention Level (40 ppb). At 13 m from the Spargepoints ® , a significant PCE 

concentration decrease was detected (from 2,000 ppb to 13 ppb). Currently, the source zone area is being treated 

with Perozone ® (peroxide-coated ozone) in conjunction with pump and treat. 

Perozone ® is also used on a former dry cleaner site in Terneuzen. After demolition of the dry cleaner facility and 

excavation of the hot spot in soil, MIP-CPT’s were done to investigate for possible DNAPL below the former dry 

cleaner facility. At least at one point on depth DNAPL was detected (PCE: 130,000 µg/L). Previous investigations 

indicate a large near-source zone area of 150 x 60 m. After installing 60 Laminar Spargepoints ® over 

approximately 100,000 m 3 soil volume, the system was started in October, 2005. The initial results indicate a quick 

removal of aqueous PCE concentrations. After allocation of the oxidant mass loading for the near-source zone 

treatment some rebound was found in the source zone area. Additional treatment is required to reach the cleanup 

goals. The experience indicates that treatment of the DNAPL with Perozone ® is possible. Mobilization effects 

were found in the source zone also. From extended monitoring appears a 99,8% reduction of this initial 

increased concentration. 

57 




Non-Thermal Plasma - A Novel and 

Cost Effective Advanced Oxidation System 

Dvir Solnik 1 , Andreas Kolch 2 , Andrew Salveson 3 , Nitin Goel 3 , 

Nicola Fontaine 4 , Justin Sutherland 5 , and Chris Fennessy 6 

1. Aquapure Technologies Limited, Israel 

2. Hytecon, Germany 

3. Carollo Engineers, Walnut Creek, CA 

4. Carollo Engineers, Walnut Creek, CA 

5. Carollo Engineers, Austin, TX 

6. Aerojet, Sacramento, CA 

Aquapure is a novel and energy efficient method for the generation and transfer of various oxidants into water, 

including the hydroxyl radical. This method is characterized as non-thermal plasma. Depending on the target 

compound, the EE O of UV/hydrogen peroxide system is 42% to 78% higher than the EE O of the Aquapure system. 


58



Use of Velocity Profiling to Assess to Effect 

of Piping Configuration on UV Dose Delivery 

Dennis J. Greene 1 , Keith Bircher 2 , and Harold B. Wright 3 

1. AECOM Water, 276 Abby Road, Manchester, NH 03103 

2. UV Technologies Div., Calgon Carbon Corporation, 50 Mural Street, Unit#3, 

Richmond Hill, ON, CAN L4B 1E4 

3. Carollo Engineers, 12592 West Explorer Drive, Suite 200, Boise, ID 83713 

The USEPA UVDGM allows for use of pre-validated reactors when point velocities measured upstream and 

downstream of a reactor fall within ± 20% of the average pipe velocity (v avg ) at the validation and WTP sites. This 

guidance is somewhat limited in application because internal reactor components typically create a reactor outlet 

velocity profile with points that exceed the ± 20% V avg criterion. A method for applying pre-validated reactors 

based on alternative velocity criteria is presented: if measured velocity profiles at a WTP are closer to v avg than the 

validation velocity profiles based on statistical analysis, then pre-validation dose delivery results should apply to 

the WTP site. 

59 




Ultraviolet System Design Considerations for Uncovered Reservoir 

versus Water Treatment Plant Applications 

Jack Bebee, P.E. 1 and Christine Cotton, P.E. 2 

1. Malcolm Pirnie, Inc., 1525 Faraday Avenue, Suite 290, Carlsbad, CA 92008 

2. Malcolm Pirnie, Inc., One South Church Avenue, Suite 1120, Tucson, AZ 85701 

The objective of this paper is to summarize the applications and specific approaches used during design and 

development of operational strategies for both UV disinfection of uncovered reservoir and Water Treatment Plants 

(WTP). These projects are in California, which has more stringent off-specification requirements than the Long 

Term 2 Enhanced Surface Water Treatment Rule (LT2ESWTR); therefore, the UV facility design needed 

additional controls and equipment to meet the requirements. 

This paper identifies key items that need to be evaluated during UV facility design for both WTP and uncovered 

reservoir applications and provide examples of how these items were addressed on real-world projects. Some key 

items that are discussed include: 

• Design modifications to improve hydraulic operation 

• Operation during reactor start-up/shut down 

• Operation during a power outage or interruption 

• Control and operation of UV reactor flow control valves 


60



Costs and Sustainability Comparison of Chemical Disinfection and 

Medium Pressure Ultraviolet Disinfection for Virus Inactivation 

James Collins 1 , Christine Cotton 1 , and Phyllis Posy 2 

1. Malcolm Pirnie, Inc., 1 S. Church Ave, Suite 1120, Tucson, Arizona 

2. Atlantium Technologies, Har Tuv Industrial Park, POB 11071, Israel 99100 

Previously, it was thought that using UV disinfection for 4-log virus inactivation would be cost prohibitive due to 

the high doses required in the Long Term 2 Enhanced Surface Water Treatment Rule (LT2ESWTR). However, 

recent studies (Linden, 2007) have shown that the dose necessary for 4-log adenovirus inactivation is 

approximately 40% to 50% lower than the doses published in the LT2ESWTR when polychromatic UV lamps are 

used (Linden et al 2007). A recent validation using adenovirus2 demonstrated this in full scale. 

This study evaluated the costs (i.e., capital and operation and maintenance costs) and sustainability of using 

chlorine or UV disinfection for virus inactivation of groundwater and surface waters. The results of this study 

show that UV disinfection is a cost effective option for select disinfection scenarios. UV disinfection was also 

shown to have environmental and risk benefits when compared to traditional chemical disinfection. 

61 




A Smart Way to Validate UV Systems for Reuse Applications 

Matthias Boeker 1 , Andrew Salveson 2 , Madhukar Rapaka 3 , and Ronnie Bemus 1 

1. ITT Water & Wastewater U.S.A., 14125 South Bridge Circle, Charlotte, NC 28273 

2. Carollo Engineers, 2700 Ygnacio Valley Road, Suite 300, Walnut Creek, CA 94598 

3. ITT Water & Wastewater Germany, Boschstrasse 4, 32051 Herford, Germany 

The NWRI/AwwaRF 2003 Ultraviolet Disinfection Guidelines describe a methodology for validating UV Systems 

for reuse applications. 

The validation testing of pilot plants using modular, open channel configurations allows for an easy upscale of the 

bioassay results to full-scale UV systems. Because closed vessel UV reactors employ different number of lamps 

and may have variations in lamp arrangement, individual reactor certification would be required. 

Sometimes viewed as “magic”, this paper describes a robust methodology for combining the use of CFD prediction 

models with full scale biodosimetric testing, to obtain sound, consistent results that allow a design engineer to 

dependability size a UV system within the boundaries of the NWRI/AwwaRF guidelines. 


62



A Kinetic Model for the Degradation of Natural Organic Matter during the 

Ultraviolet Hydrogen Peroxide Advanced Oxidation Process 

Sarathy, S.R., Bazri, M., and Mohseni, M. 

Department of Chemical and Biological Engineering, University of British Columbia, 

2360 East Mall, Vancouver, BC V6T 1Z3 Canada 

A completely dynamic, kinetic model was developed to predict the degradation of chromophoric natural organic 

matter (CNOM) and H 2 O 2 during the UV/H 2 O 2 . Model parameters were estimated numerically by optimizing 

fitting to experimental results obtained with a “synthetic water” using Suwannee River NOM. The reaction rate 

constant for the reaction between hydroxyl radicals ( • OH) and NOM was estimated at 1.14E4 L mg -1 s -1 , in close 

agreement with past literature reports. The reaction rate constant for the reaction between • OH and CNOM was 

estimated at 3.08E8 L mol -1 s -1 . Considering the change in CNOM helped improved prediction of H 2 O 2 degradation 

but the model still under predicted experimental measurements. This discrepancy is hypothesized to be due to the 

model’s neglect of the reaction between H 2 O 2 and carbon-centered radicals, formed when • OH react with NOM. 

63 




UV Photolysis of Pharmaceuticals and Personal Care Products (PPCPs) 

and Endocrine Disrupting Substances (EDS) in Drinking Water 

Jules Carlson 1 , Mihaela Stefan 2 , and Chris Metcalfe 1 

1. Trent University, Peterborough, ON, Canada 

2. Trojan Technologies, London, ON, Canada 

There is potential for contamination of drinking water by pharmaceuticals and personal care products (PPCPs) and 

endocrine disrupting compounds (EDCs). UV treatment processes will be described along with the parameters 

needed to evaluate their efficacy for removal of 15 PPCPs and EDCs. UV irradiations were performed using both 

low- and medium pressure mercury light sources. Analytical methods involved solid phase extraction (SPE) and 

quantification by LC/MS/MS. The photo-degradation kinetics of investigated PPCPs and EDCs indicated that 

some compounds can be removed by direct photolysis. Characteristic UV absorption spectra were determined for 

both protonated and deprotonated forms of all compounds, along with pK a estimates determined using 

spectrophotometric titration procedures. The quantum yields at 254 nm and the OH radical rate constants were 

determined and used to interpret the experimental removal efficiency of these emerging contaminants through 

direct photolysis and advanced oxidation processes. Irradiation in the presence of 4 mg/L H 2 O 2 was an efficient 

removal method for all target compounds. With the exception of the sulphamethoxazole and triclosan which 

undergo rapid degradation by direct photolysis, reaction with OH radicals was the dominant removal pathway 

when the irradiations were performed in the presence of H 2 O 2 . The impact of water constituents, such as nitrate 

and dissolved organic matter were also investigated and will be presented. 


64



Advanced Oxidation Processes for Contaminant Destruction: 

Selecting between Ozone-Peroxide or UV-Peroxide 

James Collins and Christine Cotton, P.E. 

Malcolm Pirnie, Inc., 1 S. Church Ave, Suite 1120, Tucson, Arizona 

Interest in advanced oxidation processes (AOPs) has grown in recent years as water utilities considering the use 

impaired drinking water sources to meet system demand. The impaired sources can be contaminated with a variety 

of contaminants (e.g., volatile organic compounds (VOCs), 1,4-dioxane, N-Nitrosodimethylamine (NDMA), and 

taste and odor compounds). 

AOPs are technologies that are capable of removing multiple contaminants simultaneously using the hydroxyl 

radical. Currently, the two most commonly used AOPs are UV/peroxide (UV AOPs) and ozone/peroxide 

(ozone AOPs). Both technologies have distinct advantages over more traditional treatment technologies. The 

paper discusses some of the design issues that should be considered when evaluating UV AOPs and ozone AOPs. 

65 




Rapid Measurement of Background Hydroxyl Radical Scavenging in Water 

Matthew Hross and Erik J. Rosenfeldt 

The University of Massachusetts, Department of Civil and Environmental Engineering 

A synthetic water was evaluated using the R OH,UV concept to determine the overall background hydroxyl radical 

scavenging. Two probe compounds were used, the first being para-chlorobenzoic acid (pCBA), and then using 

methylene blue (MB) at concentrations of 5 µM. The water contained scavenging equivalent to 4 mg/L dissolved 

organic carbon (DOC). The tests were performed to evaluate the feasibility of using MB could be used a probe 

compound in place of pCBA in the R OH,UV concept. A new scavenging device was then introduced to determine the 

overall background scavenging of a water with the MB probe compound through a much quicker analysis. The new 

scavenging device predicted the overall background scavenging of the water as well as the original R OH,UV concept 

did. These predictions also agreed with theoretical calculations of the overall background scavenging. 


66



Perozone Groundwater Sparging at the Days Inn Lake City Pre-Approval Site 

Edward M. Kellar and Chris Mickler, P.E. 

MACTEC, Inc., Gainesville, FL 32669 

A full-scale microbubble Perozone sparging system using the patented Kerfoot Technologies, Inc. (KTI) 

C-Sparge process was installed on a former unleaded gas station site currently active as a Days Inn paved 

entrance. Gas phase ozone sparging with dilute liquid hydrogen peroxide injection was introduced in the source 

zone via five laminar spargepoints coupled with ozone only sparging into seven surrounding standard microbubble 

sparge points. The chemical oxidation system was fabricated in an 8-ft by 10-ft portable enclosure by MACTEC 

and installed with KTI startup assistance; operation was initiated in August, 2005. Groundwater volatile aromatic 

(BTEX) compound concentrations in source wells decreased from a historical maximum of 7,700 ug/L to 

non-detect in several monitor wells by the end of two quarters of operation. 

The site geology consisted of silty sand and fine sands with a treatment zone under asphalt paving extending from 

water table nominally at 3-ft bgs to the confining clay layer at 22-24 feet bgs. Past initial remedial actions included 

limited tank removal source excavation, and additional assessment under the FDEP Pre-approval program. 

Sparge point programming adjustments have focused oxidant application on a remaining area where limited 

sparging has shown the continued presence of desorbing BTEX mass. Two source zone wells with recalcitrant 

VOCs in an area of fine flowing sands are receiving additional attention to improve coverage because lower 

permeability with high formation back pressures has limited aggressive injection radius of influence. Perimeter 

ozone only sparge points have reduced groundwater to non-detectable BTEX and maintained an outer oxidative 

band with no re-bound; programmed operation has been reduced to a minimum. 

The presentation will focus on design and installation details, startup test sequences, in situ DO and ORP 

performance monitoring, remote telemetry alarm features, and lessons learned regarding maintenance 

requirements, materials of construction suitable with ozone in Florida heat, and the use of kinetics analysis to 

predict treatment time to endpoints. The system will be contrasted with a larger and more complex 28 point 

modular KTI Perozone system newly installed by MACTEC at a Mulberry, FL BTEX site. 

67 




Characterization of Ozone Mass Transfer in Model Soils 

Alejandro García 1 , Tatyana Poznyak 2 , Jesús Rodríguez 2 , and Isaac Chairez 3 

1. Department of Automatic Control, CINVESTAV-IPN, Av. Instituto Politécnico Nacional, Col. San Pedro 

Zacatenco, C.P.07360, Mexico D.F., Mexico 

2. Superior School of Chemical Engineering National Polytechnic Institute of Mexico (ESIQIE-IPN), Edif 7, 

UPALM, C.P. 07738, Mexico D.F., Mexico, E-mail: tpoznyak@ipn.mx 

3. Professional Interdisciplinary Unit of Biotechnology of National Polytechnic Institute (UPIBI-IPN), Av. 

Acueducto s/n., C.P. 07480, México, D.F, México. 

Many technological approaches based on ozone high oxidant capacity have been developed in the treatment of 

contaminated water. On the contrary, ozone application for the treatment of the contaminated air and soil has been 

few explored. In the particular case of soil treatment, there exist some important attempts that have been realized in 

order to determine the possible implementation of ozone as a component in a specific remediation technique in the 

presence of polyaromatic organic compounds. This situation has led to the realization of some studies about ozone 

mass transfer in porous media. However, this is not a trivial problem, overall if we consider complexities involved 

in a heterogeneous solid phase, where humidity and organic matter presence can influence on the ozone transfer. In 

this sense, some researchers have presented their results using soil packed columns and mathematical models based 

on partial differential equations. Nevertheless, the validation of mathematical model depends on the determination 

of all parameters involved, experimental procedure and for the case of some parameters a “trial and error 

calibration”. In the present work the ozone mass transfer characterization for different model soils (glass spheres, 

sand, and burned soil) in a packed glass reactor was studied. We consider the solid phase as a lumped system, 

based on this idea a characteristic ozone mass transfer global parameter k sat was proposed. This parameter by an 

expression derived from the ozone mass balance in the system was calculated, and it can be obtained 

experimentally from the ozone concentration measures at the output of the reactor in the gas phase. The k sat values 

for the four proposed model solids were calculated, and also a sensibility analysis of k sat was carried out. Besides a 

simple mathematical model in ordinary differential equation to prove the validity of k sat in the process was 

simulated and compared with the experimental data. 


68



Ozone Oxidation for Source Removal 

And Prevention Barrier at a Fire Training Academy 

Scott C. Michaud and Thomas C. Cambareri, LSP 

Cape Cod Commission, 3225 Main Street, PO Box 226, Barnstable, MA 02630 

The Barnstable Fire Training Academy is a multi-plume site resulting from chronic releases of petroleum 

hydrocarbons to the environment during simulated fire-fighting conditions over several decades as an 

“industrial/commercial” use in a Zone II public water-supply area. Use of petroleum at the site ended in 1986. 

Multiple source removals were conducted over the subsequent 20 years. While a pump-and-treat containment 

system was successful in reducing the down-gradient extent of petroleum in groundwater, source areas continued to 

release slugs of contamination to groundwater from contaminated soil at the water table. The site is located in a 

highly permeable aquifer suitable for an air-sparging system. The C-Sparge/Perozone® system manufactured by 

Kerfoot Technologies, Inc. was selected to treat residual smear zones. The system consists of 12 sparge points that 

deliver ozone-amended air and peroxide to contaminated areas. The sparge points are dual-stacked in source areas 

in recognition that a deep sparge point can influence a wider lateral area, while a shallow sparge point concentrates 

treatment closer to the point. The system was brought on line in March 2006 and continuous peroxide injection 

commenced in April 2006. Over the subsequent 6 months, significant reductions in concentrations of BTEX, 

naphthalene and associated volatile organics (VOC) were reported for groundwater samples collected from 

contaminant source areas. In other source areas, low dissolved oxygen and redox measurements and limited VOC 

reductions point to blocked treatment pathways in sediments around some sparge wells. Where significant 

reductions in contaminant concentrations were achieved, a subsequent rebound of VOC concentrations observed 

while the sparge system was temporarily inoperable indicates that contaminated soil in smear zones continue to be 

a source of contaminants leaching to groundwater. 

69 




A Simplified Method for Modeling Chemical 

Intermediates in Advanced Oxidation Processes 

Joseph A. Drago, P.E., Ph.D. 

Kennedy/Jenks Consultants, San Francisco, California 

This paper describes a simplified method for modeling the formation and destruction of chemical intermediates that 

are formed during advanced oxidation processes, such as UV-peroxide and ozone-peroxide, where OH• radical is 

the dominant oxidant and pseudo-first order reaction conditions (e.g., OH• at steady state) exist. The model 

employs equations, developed to describe radioactivity decay chains, to calculate the formation and degradation of 

chemical intermediates when the relative destruction rate and the decay scheme of a target compound are known. 

An example using methyl tert-butyl ether (MtBE) is included. 


70

Tuesday PM – Session 16: UV Disinfection Research – S16-1 


Effect of Pre- and Post- UV Disinfection Conditions on Photoreactivation 

of Fecal Coliforms from a Physicochemical Wastewater Effluent 

Catherine Hallmich and Ronald Gehr 

Department of Civil Engineering and Applied Mechanics, McGill University, 

817 Sherbrooke Street West, Montreal, Quebec, H3A 2K6 

Decreasing photoreactivation after wastewater UV disinfection can lead to considerable savings in capital and 

operating costs. Objectives of this study were to determine pre- and post-UV irradiation conditions able to decrease 

fecal coliform photoreactivation from Montréal Wastewater Treatment Plant wastewater effluents. Results indicate 

that delaying exposure to photoreactivating light for 3 hours suppresses photoreactivation at UV doses of 10 and 20 

mJ/cm 2 . Moreover, at least 440 lux of visible light is needed to initiate photoreactivation. Additionally, 

photoreactivation decreases significantly when visible light is simultaneously emitted prior to or during UV 

irradiation. This is more significantly observed for winter samples, where photoreactivation is decreased by 

nearly 50%. Finally, summer populations are more sensitive to inactivation and less able to photoreactivate than 

winter populations. 

71 




Comparison of the Disinfection Effects of Vacuum-UV (VUV) 

and UV Light on Bacillus subtilis Spores at 172, 222, 254 nm 

Ding Wang, 1,2 Thomas Oppenländer, 3 

Mohamed Gamal El-Din, 1 and James R. Bolton 1 

1. Department of Civil and Environmental Engineering, University of Alberta, Edmonton, 

AB, T6G 2W2, Canada. 

2. Current address, Department of Civil Engineering, University of Toronto, Galbraith Building, 

35 St. George St., Toronto, ON, Canada, M5S 1A4. 

3. Hochschule Furtwangen University (HFU), Campus Villingen-Schwenningen, Fakultät Maschinenbau 

und Verfahrenstechnik, Jakob-Kienzle-Str. 17, 78054 Villingen-Schwenningen, Germany. 

The efficacy of the ultraviolet (UV) disinfection of Bacillus subtilis spores in aqueous suspensions at wavelengths 

of 172, 222 and 254 nm was evaluated. A Xe 2 * excilamp, a KrCl * excilamp and a low-pressure mercury lamp were 

used as the UV light sources at these three wavelengths, respectively. The first-order inactivation rate constants at 

172, 222 and 254 nm were 0.0022, 0.122, 0.069 cm 2 mJ –1 , respectively. Therefore, the 2 log reduction of B. subtilis 

spores required fluences (UV doses) of 909, 21.6, and 40.4 mJ cm –2 at these respective wavelengths. This means 

that VUV exposure at 172 nm is much less efficient than the exposures at the other two wavelengths for 

the inactivation of B. subtilis spores, while UV exposure at 222 nm is more efficient than that at 254 nm. This 

research indicated quantitatively that VUV light is not practicable for microorganism disinfection in water and 

wastewater treatment. 


72



E. coli Repair in UV Water Treatment Conditions 

Bohrerova, Z. and Linden, K.G. 

The repair and regrowth of E. coli was followed in drinking and reuse water following LP and MP UV disinfection. 

The aim of this study was to perform repair experiments under more realistic conditions than has previously been 

attempted. The UV fluence levels used before repair were similar to fluences recommended for water disinfection 

(40 – 60 mJ/cm 2 and 100 – 120 mJ/cm 2 for drinking and reuse water, respectively). The relationship between UV 

fluence and the amount of repair was of particular interest, since it is known that with increasing UV fluence the 

extent of repair decreases. The exact quantification of dark repair after 48 h was also investigated and compared to 

the regrowth potential of E. coli after post disinfection conditions (including high numbers of inactivated cells in 

water and potential chemical byproducts of disinfection). The results indicated limited E. coli repair with an 

average photorepair of 0.3 (+- 0.19) log and no dark repair after 48 h when corrected for regrowth. The regrowth 

of the E coli in the presence of inactivated bacteria followed a logarithmic trend in every case with a sharp increase 

in E. coli numbers when the initial bacterial concentration was low and slower increase with the initial bacterial 

concentration being higher. The initial E. coli concentration usually at least doubled after 48 h of liquid holding and 

in some cases increased up to 4 logs from the initial concentration. In the future, more detailed studies should be 

performed regarding the regrowth of disinfection survivors after treatment since some of the regrowth rates 

reported herein could have significant impact on the safety of treated water. On the other hand we contributed to 

the literature that indicates E. coli repair in treated water and after using UV fluences for water disinfection should 

not be of concern to operators of water treatment plants, since the repair rates are negligible. 

73 


Tuesday PM – Session 17: AOP and Ozone Byproducts – S17-1 


Novel UV LED Advanced Oxidation System for Disinfection and 

Removal of Organic and Heavy Metal Contaminants in Water 

Tom Hawkins, Ph.D., and Mark Owen 

Puralytics, 15250 NW Greenbrier Pkwy, Beaverton, OR, USA 97006-5764 

A novel technology is described, suitable for point of use (POU)/point of entry (POE) water purification systems, 

that uses a dual wavelength UV LED system to excite a fixed-substrate photocatalyst. This advanced oxidation 

process rapidly mineralizes organic and inorganic contaminants in water without the chemicals, consumables, toxic 

waste, pressure drop, or water wastage of traditional solutions. With a self-cleaning fixed photocatalytic substrate, 

uniform LED illumination, and extremely high surface area, the system is inherently compact, lightweight, 

scalable, and low-maintenance. The process combines photolysis, germicidal disinfection, photocatalysis, and 

photo-adsorption to effectively eliminate many contaminants in water without creating any waste stream. Reported 

tests confirm successful disinfection of Raoultella Terrigena bacteria and MS2 phage virus, removal of heavy 

metals including arsenic and lead, and the elimination of a wide range of organic chemicals from water, including 

phenol, MTBE, and PCE. 


74



UV Advanced Oxidation Processes for Taste and Odor Treatment: 

Evaluation of Assimilable Organic Carbon 

Formation Potential at an Indiana WTP 

James Collins 1 , Christine Cotton 1 , Bruce Heeke 2 , David Dahl 3 , and Alan Royce 4 

1. Malcolm Pirnie, Inc., Tucson, Arizona 

2. Patoka Lake Region Water and Sewer District 

3. Midwestern Engineers 

4. Trojan Technologies 

In recent years, the Patoka Lake Water Regional Water and Sewer District is a utility that has experienced seasonal 

taste and odor events that have become a major water quality concern. In 2007, the lake experienced a taste and 

odor event with 2-Methylisoborneol (MIB) levels measured as high as 240 nanograms per liter. The District 

evaluated various treatment techniques that would be capable of achieving up to a 1.8-log reduction of MIB. 

The treatment techniques considered include UV advanced oxidation process (AOP), ozone, peroxone, granular 

activated carbon, and powdered activated carbon. 

UV AOPs has been shown to reduce taste and odor compounds such as MIB and Geosmin. One advantage of UV 

AOPs is the ability of the UV equipment to operate in either disinfection mode or taste and odor mode with one 

manufacturer’s equipment. This ability reduces the overall operation and maintenance costs due to reduced power 

consumption during non-taste and odor events. However, for disinfection, UV reactors are typically installed after 

the filters to treat the highest quality water available, to meet LT2ESWTR requirements, and to minimize capital 

and operation costs. Oxidation processes can have the potential disadvantage of generating assimilable organic 

carbon (AOC) that can stimulate microbial growth in the distribution system. AOC generation can be controlled if 

biofilters are installed after the AOP process, as is typical with ozone treatment. However, for UV disinfection to 

achieve disinfection credit, the UV AOP system needs to be installed downstream of the filters. 

The overall effectiveness of UV AOPs has been documented in the literature. However, to date, no data regarding 

AOC formation following UV AOPs for taste and odor treatment have been published. For UV AOPs used for 

treatment of other environmental pollutants, available data suggest that AOC can be created. However, the UV 

dose or Electrical Energy per Order of Destruction (EEOs) (typically used in UV AOP applications) for taste and 

odor compounds is lower for MIB and Geosmin compared to most environmental pollutants. Relatively, the 

formation of AOC by UV AOPs is expected to be lower than that of other technologies (e.g. ozone) given the 

fundamental reaction mechanisms at work in UV AOP systems. In general, the impact on AOC generation at the 

EEOs required for taste and odor reduction is not well characterized, is water quality dependant, and will determine 

whether UV AOP is feasible at this WTPs. 

This paper will describe the following items: 

• Mechanisms of UV AOP for taste and odor reduction 

• Evaluation of UV AOP effectiveness for MIB reduction 

• Evaluation of AOC generation in relation to MIB reduction, its affect on UV AOP placement within the 

WTP, and potential effects in the distribution system 

• A cost comparison of UV AOPs, ozone, peroxone, granular activated carbon, and powdered activated 

carbon for taste and odor treatment based on this study 

75 




Toxicity Assessment and Identification of Oxidation Byproducts Generated 

During the Ozonation of Natural Water Containing Pesticide 

Pamela Chelme-Ayala, Mohamed Gamal El-Din, and Daniel W. Smith 

Department of Civil and Environmental Engineering, 3-133 Markin/CNRL Natural Resources Engineering Facility, 

University of Alberta, Edmonton, Alberta, T6G 2W2, Canada 

The generation of intermediates, in some cases more toxic than the parent compounds, that can appear in the 

treated water is one of the drawbacks of advanced oxidation processes. In this study, the formation of byproducts 

generated during the treatment of a natural water containing the pesticide trifluralin by ozonation and ozone 

plus hydrogen peroxide was investigated. The results indicated that the primary oxidation byproducts were 

2,6-dinitro-4-trifluoromethyaniline and 4-trifluoromethyaniline. To examine the treatment efficiency, the acute 

toxicity of untreated and ozonated samples was assessed using the Microtox ® bioassay. The results showed 

a toxicity decrease in the initial stages of treatment. Then, the toxicity of the samples was found to increase at the 

end of treatment. 


76



Evaluating the Effects of Source Water Quality 

on Bromate Mitigation Performance 

Zaid Chowdhury 1 , David Eberle 1 , Laurel Passantino 1 , Joe Kurrus 2 , and Linda Bezy-Botma 2 

1. Malcolm Pirnie, Inc. 

2. City of Peoria, AZ 

Over the course of the past three years, mitigation of ozone-induced bromate by carbon dioxide and the innovative 

chlorine/ammonia processes was studied at the Greenway Water Treatment Plant located in Peoria, AZ. Following 

the results of a full-scale evaluation indicating that bromate mitigation via pH depression and chlorine/ammonia 

addition were able to reduce bromate formation by 35 percent or more, additional bench-scale testing was 

performed to assess the influence of source water quality on bromate formation, especially with respect to bromide 

concentrations. Results from the bench-scale testing indicated that, while both strategies were effective at 

mitigating bromate formation in some waters, neither process was expected to reduce bromate formation below 

8 µg/L on a consistent basis. Carbon dioxide addition appeared to perform slightly more consistently compared to 

the chlorine/ammonia process; however, based on other economic, social, and environmental considerations not 

discussed in this study, the chlorine/ammonia process appeared to be the best alternative to mitigate bromate 

formation in order to allow higher ozone dosages and thereby enhance taste, odor, and TOC removal. 

77 


Tuesday PM – Session 18: Modeling UV Systems – S18-1 


Monte Carlo Ray Trace Model: 

A New Approach in Determining Fluence Rates in UV Systems 

Khoi Nguyen and Jaewan Yoon 

Old Dominion University, Civil and Environmental Engineering, Norfolk, Virginia 

A robust Monte Carlo Ray Trace algorithm and model were recently developed to determine fluence rates in a 

three-dimensional space of UV systems. Using this model, millions of random light energy bundles are simulated 

from each UV lamp and are traced through the system. The model accounts for inherent variation in emissions 

from lamps and UV systems, effects of multiple reflections, lamp shadowing in multiple lamp systems, and other 

geometric factors of the systems, to truthfully reflect realistic physical settings. Consistent fluence rate estimates 

were successfully obtained, and model results were found to be in excellent agreement with observed experimental 

data obtained from two independent sources and the PSS Model. 


78



A Comparison of Two Methods for Measuring the 

UV Output of Low Pressure Mercury Lamps in Air 

G. Elliott Whitby 1* , Bill Sotirakos 1 , and James R. Bolton 2 

1. Calgon Carbon Canada, 50 Mural St., Unit #3, Richmond Hill, ON, Canada L4B 1E4 

2. Bolton Photosciences Inc., 628 Cheriton Cres., Edmonton, AB, Canada T6R 2M5 

A standard bioassay has never been accepted for sizing UV systems for disinfecting non-reuse wastewaters. The majority 

of UV systems for non-water reuse applications are sized using a computer program called UVDIS. This requires the use 

of the UV output of a lamp measured in air. Over estimates of lamp output can lead to undersized UV systems. A standard 

measurement method does not exist, but one has been proposed by the IUVA Manufacturers’ Council based on the Keitz 

method. This method and another method called ‘integration over a sphere’ were compared using a low pressure high 

output UV lamp. The two methods gave the same results within experimental error. The results also showed that the 

conditions for testing a lamp must be carefully defined for that particular lamp. A standard bioassay must be developed for 

UV systems for non-reuse wastewater. 

79 




Method for Measurement of Output of Low Pressure Mercury Lamps [1] 

Volker Adam, Ralf Dreiskemper, Martin Kessler 

Heraeus Noblelight GmbH, Heraeusstr. 12-14, 63450 Hanau, Germany 

Facing the challenge of designing UV systems to meet specific disinfection requirements has become increasingly 

more complex with the various lamp technologies and configurations available. Whether the chosen design method 

is a calculated sizing model, such as point source summation, or biological verification, it is important to adhere to 

strictly defined experimental protocols and quality controls. This is most apparent when considering technology 

comparisons from different manufacturers. In particular the lamp output measurement procedure used can 

significantly affect the outcome of measurement results. If the tests are conducted under identical protocols, a 

proper and fair comparison between competing lamps is feasible. Therefore the IUVA Manufacturers Council 

organized a taskforce in 2007, with the aim of preparing a consistent method for the determination and 

benchmarking of UV lamp output from monochromatic (254 nm) lamps operated by a corresponding power supply 

(ballast). The goal was for this method to be used for testing and comparing testing results from different 

laboratories. As a further step the taskforce arranged an intercomparison program for laboratory testing of a sample 

batch of LPM lamps in a number of locations in Europe and North America. This round robin test will help 

determine the suitability of this testing method and provide an indication of the measurement uncertainty. 

This paper outlines the lamp measurement method drafted by the task force and subsequently published in the 

IUVA News. In addition this paper will present the method and the results of the LPML intercomparison program. 

The paper which gave the basis for the talk and is cited here was published previously in the IUVA news 

April 2008 [1] 


80



Controlling Mercury Release with UV Lamp Sleeve Breaks 

Harold Wright, Ed Wicklein, and Corianne Hart 

Carollo Engineers, 12592 West Explorer Drive, Suite 200, Boise, Idaho 83713 

The Water Research Foundation funded an evaluation of mercury release and control with drinking water 

UV disinfection. Experimental studies show that the mass of mercury released when an amalgam low-pressure 

high-output lamp breaks is orders of magnitude less than when a MP lamp breaks. The difference is likely related 

to the amount of mercury in the vapor phase during lamp operation, which is notably greater with MP lamps 

because they operate at high temperatures. The advective-dispersion equation can be used to model mercury 

transport in pipes while tracer studies or CFD can be used to model transport through basins and other structures. 

Transport models can be used to locate valves to contain mercury release and define water-sampling plans. 

Low velocity zones, however, will not contain the initial mercury release. 

81 




High Energy Efficiency and Small Footprint with High-Wattage 

Low Pressure UV Disinfection for Water Reuse 

Andrew Salveson 1 , Tavy Wade1, Keith G. Bircher 2 , and Bill Sotirakos 2 

1. Carollo Engineers 

2. Calgon Carbon Corporation 

Wastewater treatment plants often use lamp racks oriented horizontally in the direction of flow in an open channel. The lamps 

emit Ultraviolet Light (UV) that inactivates pathogenic microorganisms rendering the water safe for discharge to a receiving 

water body or for re-use of the water (irrigation, indirect potable re-use, industrial use, gray water for non-potable use, etc.) 

The racks hold lamps in an array dispersed over the cross section of the channel such that none of the water flowing down the 

channel passes too far from any one lamp. 

Early UV systems using conventional low pressure mercury arc lamps have a lamp spacing of approximately 7.5 cm in a 

square array. With 2.5 cm diameter quartz tubes this means that the maximum distance from any lamp is approximately 4 cm. 

This provides sufficient space for the water to pass between the lamps without undue head loss and is close enough to achieve 

adequate penetration of the UV to all areas and hence adequate disinfection. These low pressure systems have lamps with a 

total power consumption of under 100 Watts and a UVC (germicidal UV) output of under 50 Watts. 

Subsequent advancement in lamp technology has produced low pressure lamps with higher output. Higher lamp output means 

that more water can be disinfected per lamp, and hence the flow of water must be increased proportional to the lamp UVC 

output. However due to head loss limits across a bank of lamps (too high a head loss means that the level of water upstream of 

the bank must increase and some of the water will spill over the top of the lamp bank and not be adequately treated), the lamp 

spacing must be increased to accommodate the greater water flow. For example lamps with an electrical consumption of 250 

Watts and UVC output of approximately 100 Watts must be accommodated in arrays with 10 cm lamp spacing. The additional 

area for the flow of water limits the velocity and hence head loss across the lamp bank. However this increased lamp spacing 

reduces the irradiance at the furthest point from the lamps resulting in some decrease in the performance efficiency. 

More recent development of even higher powered lamps (500 Watts, with 200 Watts UVC output) would potentially result in 

the number of lamps needed being reduced to half that of systems employing 250 Watt lamps. However this means that the 

flow per lamp must be doubled, resulting in a quadrupling in the head loss across a lamp bank unless the spacing of the lamps 

is increased further still. Increasing the spacing beyond 10 cm potentially results in a further reduction in treatment efficiency, 

negating the potential advantages of fewer higher power lamps. 

This paper presents results of bioassay testing at a WWTP in California of a Calgon Carbon C3500 system with 500 Watt Low 

Pressure amalgam lamps that has overcome this lamp spacing/pressure drop barrier. 

The pilot test consisted of 2 banks of lamps each with a 4 x 4 lamp array for a total of 32 lamps. Flow rates from 250 to 4000 

gpm and UVT’s from 35 to 70%T were tested. 

The main advantages of this system are that fewer lamps are needed than previous systems while still maintaining high 

electrical efficiency. This results in a system with a smaller footprint, reducing installation costs, and lower operating and 

maintenance costs. 

An economic analysis at a California Title 22 reuse site will be presented comparing the installed and operating costs of this 

system with a conventional lower powered LP system and a closed pipe medium pressure lamp system. 


82



Impact of UV Disinfection Combined with Chlorination/Chloramination on 

the Formation of Nitrogenous Disinfection Byproducts in Drinking Water 

Amisha D. Shah 1 , Aaron A. Dotson 2 , Karl G. Linden 2 , Howard S. Weinberg 3 , and William A. Mitch 1 

1. Department of Chemical Engineering, Yale University, 9 Hillhouse Ave., New Haven, CT 06520, 

2. Department of Civil, Environmental, and Architectural Engineering, Engineering Center ECOT, 

University of Colorado at Boulder, Boulder, CO 80309 

3. Department of Environmental Sciences and Engineering, University of North Carolina at Chapel Hill, 

1303 Michael Hooker Research Center, Chapel Hill, NC 27599 

Our study’s focus was to understand the role UV treatment had on forming selected nitrogenous DBPs, including 

haloacetonitriles, halonitromethanes, and nitrosamines under various operating and water quality conditions. 

Preliminary experiments investigated DOM isolates dosed with elevated nitrate concentrations. These samples 

were exposed to either low pressure (LP) or medium pressure (MP) UV sources combined with 

chlorination/chloramination where their order was varied. In certain cases, dichloroacetonitrile (DCAN) formation 

decreased when UV exposure was followed by chloramination in comparison to chloramination alone but remained 

constant when chloramination was added prior to UV exposure. Nitrosodimethylamine (NDMA) and 

dimethylnitramine (DMNA) concentrations were found to increase upon similar MP 1000 mJ/cm 2 UV exposure 

followed by chlorination in comparison to chlorination alone. We are pursuing bench scale experiments to better 

understand formation mechanisms. Overall, this study will assist in understanding the potential various 

UV/chlorination/chloramination treatment schemes will have on forming nitrogenous DBPs and therefore provide 

guidance for utilities considering UV treatment. 

83 




High Intensity Pulsed Lamps for Water Treatment: Review and Status 

Ray Schaefer and Michael Grapperhaus 

Phoenix Science & Technology, Inc., Chelmsford, MA 01824 

This talk reviews the characteristics of pulsed lamps and the limitations of commercial flash lamps for practical 

water treatment. Selected research on enhanced treatment rates from pulsed light is included. A status report 

is given on recent and ongoing research to increase lifetime and reduce the life-cycle cost of pulsed lamps. 


84



An Empirical Method for Accurately Sizing Wastewater 

UV Reactors for Disinfection of any Microorganism 

Harold Wright 1 , Andrew Salveson 1 , Tavy Wade, Sean Poust 1 , Allan Slater 2 , 

Duncan Collins 2 , Jeremy Meier 2 , and Ian Dearnley 2 

1. 2700 Ygnacio Valley Road, Suite 300, Walnut Creek, CA 94598 

2. Severn Trent Services, 580 Virginia Drive, Suite 300, Ft. Washington, PA 19034 

The reduction equivalent dose (RED) measured during biodosimetric UV validation depends on the test microbe’s 

UV dose-response kinetics as well as the reactor’s UV dose distribution. Because of these effects, the RED 

delivered to the test microbe will differ from the RED delivered to a target pathogen or indicator microbe if the 

dose-response of the test microbe differs from that of the pathogen or indicator. The difference is referred to as the 

RED bias. Recently, two approaches have been developed and demonstrated with drinking water UV reactors for 

analyzing validation data that accounts for the RED bias. This paper reports on the application of these methods 

with a wastewater UV reactor. The first approach incorporates a term for the UV sensitivity of the microbe into the 

equation used to fit the validation data. The second approach incorporates a lognormal prediction of the UV 

reactor’s dose distribution into the dose-monitoring algorithm and predicts log inactivation using the microbe’s UV 

dose-response curve. Both approaches calibrated using validation data measured using MS2 and T1 phage provided 

accurate predictions of the log inactivation of QB phage, fecal coliform, and total coliform. 

85 




Advanced Oxidation Process – Effective and Technical Suitable for 

Micropollutant Removal in Contaminated Water Sources 

J. Krüger1, A. Ried 1 , K. Teunissen 2 , A.H. Knol 2 , and D. Csalovszki 3 

1. ITT W&WW WEDECO GmbH, Boschstr. 6, 32051 Herford, Germany 

2. DZH & Delft University of Technology PO 34, 2270 AA Voorburg, Netherlands 

3. ITT W&WW USA WEDECO Products, 14125 South Bridge Circle, Charlotte, NC 28273 

Treatment concepts for drinking water supplies are often limited by their potential to remove emerging 

contaminants. Contamination of different water sources, e.g. river water, bank filtrate, lake water or ground water 

by micropollutants is a growing concern and is under investigation by several programs. 

Future treatment concepts need to be able to remove preferably all of the new discussed micropollutants. Therefore 

the right multiple barrier approach is required. Advanced oxidation is one option to upgrade treatment processes. 

Consulting engineers and end users are in need of a cost-effective solution to treat micropollutants of concern. 

As the concern about emerging contaminants grows, it is only a matter of time until they become regulated. 

Ozone treatment and ultraviolet (UV) irradiation are well known as individual treatment steps for oxidation or 

disinfection purposes. The combination of ozone and UV-radiation on one hand or ozone or UV and hydrogen 

peroxide on the other hand results in a more powerful process. These combined processes are able to remove many 

of the investigated micropollutants efficiently and in accordance with applicable regulations. 

Mobile pilot units were designed to test the different advanced oxidation processes based on ozone, UV and 

hydrogen peroxide. Pilot trials were conducted with different types of waters and varying contaminants. 

One groundwater studied was contaminated with 1.4 Dioxane and Trichlorethene, and pretreated river water was 

synthetically polluted by Atrazine, Isoproturone, Carbamazepine, Diclofenac, Ibuprofene, Amidotrizoic acid, 

Iohexol and MTBE. 

The achieved results indicated that all of these micropollutants could be removed by the advanced oxidation 

processes. The AOP O 3 /H 2 O 2 showed in both cases the best performance regarding the operational costs and the 

achieved degradation rates. 


86



Bromate Pre-systemic Detoxification Metabolism Research Progress 

Joseph Cotruvo 1* , Richard Bull 2 , Brian Cummings 3 , Jeffrey Fisher 3 , Zhongxian Guo 4 , 

Choon Nam Ong 5 , Oscar Quinones 6 , Shane Snyder 6 , Jason Keith 7 , 

Gilbert Gordon 7 , and Gilbert Pacey 7 

1. Joseph Cotruvo & Associates LLC, Washington, DC, USA. 

2. MoBull Consulting, Richland, Washington, USA. 

3. University of Georgia, Athens, Georgia, USA. 

4. PUB Waterhub Centre for Advanced Water Technology, Singapore. 

5. National University of Singapore. 

6. Southern Nevada Water Authority, Henderson, Nevada, USA. 

7. Miami University, Oxford, Ohio, USA. 

Bromate causes cancer in test animals at high doses and it limits use of ozone in desalination, indirect or direct water 

recycling, bottled water production and ground source drinking waters due to ozone’s ability to convert natural bromide to 

bromate. Bromate is also a contaminant in hypochlorite produced from electrolysis of salt that contains small amounts of 

bromide. National standards and the WHO Guidelines for bromate are 10 ug/l based upon a hypothetical incremental 

lifetime cancer risk of approximately 1/10,000 depending upon which risk model is applied. All of the standards are subject 

to being lowered as the result of improved analytical methods and quantitation that is now on the order of 1 ug/l. 

The critical issue for current and future standards is the potential cancer risk at low drinking water doses. We are 

conducting studies aimed at producing a physiologically based pharmacokinetic (PBPK) model for the rat and humans 

quantifying the detoxification after ingestion and before it would reach a target organ like the kidney. A revised risk 

assessment will be computed using that mechanistic information at environmentally relevant doses. Pre-systemic 

metabolism can occur to varying degrees at least in the stomach. Significant metabolism occurs in the liver and blood. We 

have studied the kinetics and conditions of bromate decomposition in simulated stomach acid, by intravenous injection and 

after ingestion. It would be ideal if ingestion doses could be identified where bromate will be virtually completely 

detoxified before reaching a target organ so that the more accurate dose response can be determined at low doses. If the 

initial results are verified it is possible that bromate might ultimately be considered to be a practical threshold carcinogen 

with essentially no risk below the threshold metabolism dose. 

87 




Kinetic and Mechanistic Studies on Decomposition 

Reactions of Pyrrolidone Derivatives Using O 3 

Yu Tachibana, Masanobu Nogami, Yuichi Sugiyama, and Yasuhisa Ikeda 

Research Laboratory for Nuclear Reactors, Tokyo Institute of Technology, 

2-12-1-N1-34 Ookayama, Meguro-ku, Tokyo 152-8550, Japan 

Decomposition reactions of pyrrolidone derivatives (NRPs: R = methyl(M), ethyl(E), propyl(Pro), n-butyl(B), 

pentyl(P), iso-butyl(iB), cyclohexyl(C) groups) using O 3 have been studied at pH 2.0 and 288 K. The reaction rate 

was found to be expressed as k[NRPs][O 3 ] D ([O 3 ] D = the concentrations of dissolved O 3 ). It was found that the rate 

constants (k) slightly increase with increasing the length of alkyl groups and that the k value (2.93 ± 0.01 M -1 s -1 ) 

of NBP is larger than that (2.67 ± 0.10 M -1 s -1 ) of more bulky NiBP. These results suggest that the decomposition 

reactions of NRPs with O 3 proceed through the attack of O 3 to N atom in NRPs. 


88



Ozone Disinfection Reduces Disinfection Byproduct Formation 

to Comply with New Stage 2 DBP and LT2 Requirements 

Michael A. Oneby 1 , Richard Lin 2 , James H. Borchardt 2 , 

and Charles O. Bromley 3 

1. MWH Americas, 789 N. Water St, Suite 430, Milwaukee, WI 53202-3558, USA 

2. MWH Americas, 618 Michillinda Ave., Suite 200, Arcadia, CA 91007, USA 

3. MWH Americas, 3010 W. Charleston Blvd, Suite 100, Las Vegas, NV 89102, USA 

Four conventional surface water treatment plants owned and operated by a California water agency (Agency) 

integrated an ozone disinfection process into existing conventional treatment trains that produce potable water for 

several communities. Ozone replaced chlorine gas enabling the agency to meet regulated disinfection byproduct 

(DBP) limits for regulated trihalomethane (THM) and haloacetic acid (HAA) compounds at all sample locations in 

the respective distribution systems as required by the Stage 2 Disinfectants and Disinfection Byproducts Rule 

(Stage 2 DBP). The Stage 1 and Stage 2 DBP Rules, intended to reduce the risk of adverse health effects, regulate 

two groups of chlorinated organic compound which are byproducts of chlorine disinfection, specifically four 

trihalomethane compounds known as total trihalomethane (TTHM) and five haloacetic acid compounds (HAA5). 

The existing treatment plants were able to meet the DBP limits with chlorine disinfection under the Stage 1 DBP 

Rule which allowed averaging of TTHM and HAA5 across all the distribution system sample points. Under the 

Stage 2 DBP Rule, community water systems must meet TTHM and HAA5 limits at each sample point using a 

calculation known as the locational running annual average (LRAA). To comply with the Stage 2 DBP Rule, the 

Agency authorized on a DBP control project which included construction of an ozone facility at each of its 

treatment plants. The agency’s treatment plants, classified as Bin 1 in the Long Term 2 Surface Water Treatment 

Rule (LT2), achieve inactivation requirements for Giardia lamblia and viruses using intermediate ozone. Under 

Bin 1, water systems are not required to achieve inactivation credits for Cryptosporidium in the primary 

disinfection process. Operation of the treatment plants employ control strategies that minimize the applied 

ozone dose and limit bromate formation. The ozone facilities were constructed in 2008 and began operation in 

early 2009. 

89 




Comparison Testing of ‘Spot’ vs. ‘Pellet’ LPHO UV Lamps 

Mike Santelli 1* and James R. Bolton 2 

1. Light Sources Inc., 37 Robinson Blvd., Orange, CT 06477 

2. Bolton Photosciences Inc., 628 Cheriton Cres., NW, Edmonton, AB, Canada, T6R 2M5 

Two types of amalgam low pressure high output lamps (one with a ‘spot’ amalgam and another with a ‘pellet’ 

amalgam) have been examined in a simulated UV reactor with a quartz sleeve and water flowing outside the quartz 

sleeve. These lamps were operated at 100%, 80% and 60% full power. It was found that the ‘pellet’ type amalgam 

lamps had superior performance at reduced power levels as compared to the ‘spot’ type lamps. 


90



Measurements of UV Lamp Performance 

in Near-Field and Far-Field Apparatus 

G. Fang, D.G. Knight, R. Kilgour, and T. Molyneux 

Trojan Technologies, 3020 Gore Road, London, Ontario, Canada N5V 4T7 

Low pressure mercury arc lamps have been widely used as an effective ultraviolet (UV) light source for 

disinfection of water. The UV flux of a lamp is normally measured in air, and referred as far-field (FF) 

measurement. When a UV lamp is operating in a sleeve in water, the measurement of the UV irradiance in water is 

referred as near-field (NF) measurement. The advantage of the NF measurement is that it represents the true lamp 

operating conditions, and the NF method has become acceptable in the UV industry. However, the NF 

measurement only detects the UV irradiance from a portion of the lamp, and it is difficult to directly obtain the UV 

flux of the lamp. The relationship between the NF and the FF measurements could be a key to determine how a 

lamp is performing under field operating conditions. It has been previously demonstrated that a NF measurement 

technique can reliably determine the UV lamp relative output, and there are several methods that could be applied 

to relate the FF results to those in the NF measurement. This paper examines the relationship between the UV flux 

from the FF measurement and the UV irradiance from the NF measurement when the lamp is overheated. The 

study includes the relationship at different water temperatures and at different input powers. It demonstrates that 

the maximum NF irradiance of a lamp in water is proportional to the maximum UVC flux of a lamp. The better 

understanding of the lamp performance when operating in water in terms of UV flux and efficiency could lead to 

further optimization in UV lamp and reactor design. 

91 




Application of Computational Fluid Dynamics to Support Design 

of Full-Scale Wastewater UV Disinfection Channels 

Shanshan Jin and Melanie A. Mann 

Hazen and Sawyer, P.C., 11242 Waples Mill Road, Suite 250, Fairfax, VA 22030 

An open channel UV disinfection facility using horizontal lamps was designed for disinfection of tertiary filter 

effluent at a peak flow of 37.5 MGD. Computational Fluid Dynamics (CFD) analysis was conducted to evaluate 

various UV channel configurations that could impact the velocity distribution approaching the UV lamps and affect 

UV dose delivery. Features evaluated included depth of the UV channel inlet, approach length upstream of the first 

UV bank, location of inlet isolation valves, and width of the UV channel inlet. For the configurations studied, 

the channel inlet depth and width affected the velocity distribution more than valve location and channel length. 

The final channel configuration was based on both modeling results and practical considerations. 


92



A Genomic Model for the Prediction of Ultraviolet 

Inactivation Rate Constants for RNA and DNA Viruses 

Wladyslaw J. Kowalski 1 , William P. Bahnfleth 2 , and Mark T. Hernandez 3 

1. Immune Building Systems, Inc., 575 Madison Ave., 10th Floor, New York, NY10022 

2. The Pennsylvania State University, Department of Architectural Engineering, University Park, PA 16802 

3. University of Colorado, UCB 428, Department of Civil, Environmental, and Architectural Engineering, 

1111 Engineering Drive #441, Boulder, CO 80309 

A mathematical model is presented to explain the ultraviolet susceptibility of viruses in terms of genomic 

sequences that have a high potential for photodimerization. The specific sequences with high dimerization potential 

include doublets of thymine (TT), thymine-cytosine (TC), cytosine (CC), and triplets composed of single purines 

combined with pyrimidine doublets. The complete genomes of 49 animal viruses and bacteriophages were 

evaluated using base-counting software to establish the frequencies of dimerizable doublets and triplets. The model 

also accounts for the effects of ultraviolet scattering. Constants defining the relative lethality of the four dimer 

types were determined via curve-fitting. A total 77 water-based UV rate constant data sets were used to represent 

22 DNA viruses. A total of 70 data sets were used to represent 27 RNA viruses. Predictions are provided for 

dozens of viruses of importance to human health that have not previously been tested for UV susceptibility. 

93 


POSTER PRESENTATIONS 

Monday PM – Session P1 – P1-1 

President’s Ballroom, Prefunction Area 

Passivation, Fabrication and Maintenance Issues 

in Ozone and Oxygen Systems 

Patrick Banes, Michel Dalglish, Brent Ekstrand, Ph.D. and Daryl Roll, P.E. 

Astro Pak Corporation, 270 E. Baker Street, Suite 100, Costa Mesa, CA 92626 

This paper addresses the corrosion resistance of stainless steel in ozone and oxygen systems as affected by 

fabrication, operation and passivation. Oxygen cleaning, passivation, proper fabrication techniques and 

maintenance will extend the life and improve the efficiency of ozone systems. Corrosion products and rouge are 

discussed regarding damage, remediation, maintenance and effective system monitoring. 


94

Monday PM – Session P1 – P1-2 


Effect of additives on the degradation of 

Reactive Black 5 (RB5) by simple ozonation 

Arizbeth A. Pérez Martínez and Tatyana Poznyak 

Escuela Superior de Ingeniería Química e Industrias Extractivas – Instituto Politécnico Nacional, 

(ESIQIE-IPN), Edif. 7, UPALM, C.P 07738, D.F, México. 

In this study, the oxidation with ozone of Reactive Black 5 (RB5) was performed. To simulate dye bath effluents 

from dyeing processes, Na 2 CO 3 (30 g/L) and Na 2 SO 4 (100 g/L) each one separately and in mixture were used. The 

operation conditions were following: ozonation in a semibatch reactor (250 mL) with a glass diffuser in the bottom 

was performed; the dye concentrations of 50 mg/L, with the initial ozone concentration of 35 mg/L and ozone flow 

of 0.5 L/min at the initial pH of solution (5.10). Ozonation procedure was carried out in two stages: first, the dye 

ozonation without additives and second, in the presence of additives. In both cases, the dye degradation dynamic 

was obtained by UV/VIS spectroscopy at λ=311 nm. To control the ozonation efficiency the ozone consuming, 

pH and the electrical conductivity (just for the first case) were measured. In base of the results obtained we can 

conclude that the effect of the additives is most evident in presence of Na 2 CO 3 (30 g/L), so, the decoloration time 

decrease at 82% (from 4.0 to 0.75 min) in comparison to dye solution without additives, also the pH remained 

constant along the ozonation (pH=11.0) and the UV/VIS spectroscopy showed that the total degradation was 

achieved at 30 seconds of the reaction. 

95 


Tuesday AM – Session P2 – P2-1 


Electrolytic Ozone Generation Using Solid Diamond Anodes 

Bill Yost 

Electrolytic Ozone Inc, Cambridge Innovation Center, One Broadway, Cambridge MA 02142 

Electrolytic ozone generation has been understood as a concept for many years and has been the focus of a 

substantial amount of practical research. Creating ozone directly in a stream of water from the water itself holds the 

promise of reducing system complexity when compared with conventional corona discharge technology. Indeed, 

many potential applications that cannot bear the expense of corona discharge systems could be addressed with 

small and inexpensive electrolytic cells. Unfortunately, efforts to commercialize electrolytic generators have been 

hampered by the lack of a suitable anode material. 

This paper explores the material properties essential to choosing an anode for use within an ozone generating cell. 

The specific criteria used for evaluation are: over-potential with respect to oxygen evolution, resistance to chemical 

wear, material stability and environmental impact. While noble metals (such as platinum) and lead dioxide exhibit 

sufficient over-potential to drive the reaction leading to the formation of O 3 from H 2 O, both suffer from reliability 

issues. Further the use of lead dioxide is restricted by the European Reduction of Hazardous Substances (RoHS) 

Directive of 2002. 

While diamond in its intrinsic state is a good electrical insulator, synthetic diamond can be doped with boron to a 

level that it exhibits metallic conduction. The combination of a strong resistance to chemical attack, electrical 

conductivity and a high over-potential makes diamond an ideal candidate for an anode material. This paper 

details the benefits of using boron-doped diamond and provides data on ozone output stability and expected 

anode lifetime. 

Since depositing diamond films on conductive substrates raises a series of concerns over coating integrity, adhesion 

and CTE mismatch, the focus of this paper is on thick-film (>400 µm) free-standing plates of CVD diamond. 

A novel cell configuration incorporating free-standing plates is shown to be a robust and cost-effective means 

for reliable, long-term electrolytic ozone generation. 


96



Ozone-Based Clean-In-Place (CIP) of Bioreactors 

Hossein Zarrin 1 , Brian Hagopian 2 , and Dr. Carl Lawton 3 

1. MKS Instruments Inc. 

2. Mar Cor Purification 

3. University of Massachusetts Lowell 

Ozone can replace chemicals, hot water, and steam in Clean-In-Place (CIP) of bioreactors, reducing rinse water and 

chemical usage while saving energy costs. CIP is a time-saving method of cleaning the interior surfaces of pipes, 

vessels, and process equipment, without disassembly. Conventional CIP processes require high temperatures and 

significant amounts of energy to heat the entire system for sanitization. Chemical detergents are often required for 

effective cleaning followed by large quantities of rinse water. Dissolved Ozone can improve the effectiveness of 

CIP at reduced temperatures, saving energy. This report describes a CIP system that demonstrates Ozonation as an 

effective alternative cleaning agent for CIP processes in biopharmaceutical applications. A practical example of 

the successful implementation of an Ozone-based CIP system using a typical mammalian cell culture media and a 

microbial cell culture media is discussed. Cleanness is measured by testing the final rinse water for traces of 

materials from the media using HPLC in comparison to traditional chemical CIP methods. 

97 


Tuesday AM – Session P2– P2-3 


Noteworthy Nuances of Constructing and Starting Up an Ozone System 

Ben Kuhne1 1 , Jack Bebee 1 , Robert W. Hoffman 2 , and Stephanie Bishop 3 

1. Malcolm Pirnie, Inc., 1525 Faraday Avenue, Suite 290, Carlsbad, CA 92008 

2. Malcolm Pirnie, Inc., 12400 Coit Road, Dallas, TX 75251 

3. Malcolm Pirnie, Inc., 2301 Maitland Center Parkway, Suite 244, Maitland, FL 32751 

Ozone systems have a number of critical system components that require specific attention throughout construction 

and start-up. These components are often critical to the overall success of the project and even if clearly detailed in 

the design documents, specific attention must be given to these items during construction and start-up. Three case 

studies will identify some of the key items and how they were addressed in an effort to increase awareness in 

planning for and implementing future ozone systems. The first case study involved the expansion of a 72 million 

gallon per day (mgd) water treatment plant (WTP) to 87 mgd including the addition of sidestream raw water 

ozonation for enhanced coagulation and settled water ozonation in a concrete contactor structure for primary 

disinfection and taste and odor control. The second case study includes the construction of a 200 mgd concrete 

ozone contactor structure and ozone system for primary disinfection and taste and odor control. The third study 

involved installation of a 9 mgd sidestream ozone injection system for hydrogen sulfide removal. 

Each of the above mentioned case studies had its own unique purpose however they presented similar challenges 

during construction and start-up of the ozone systems. Several items encountered that required attention during 

construction include: 

• Delineation of Programming Responsibilities and Location of Programming. 

• Placement of Concrete for the Contactors to Ensure Successful Testing of the Concrete Contactor Structure 

and Ozone Piping to Ensure that it is an Airtight System. 

• Development of a Strategy to Transfer Operation after Completion of the System Installation and Testing. 

• Coordination of Piping, Valves and Instrumentation with the Ozone Equipment Provided. 

Several items encountered that required attention during start-up include: 

• Programming of Control System 

• Determination of Alarm Setpoints 

• Calibration of Instruments (Flowmeters, Temperature, Pressure, Dewpoint, Etc.) 

• Maintenance of Ozone Analyzer Instruments 

• Transfer of Analyzer Maintenance Responsibility from Ozone System Supplier (OSS) to Owner 

• Approach for Phased Release of Constituents off of Existing Filter Media 

This paper will discuss the common challenges faced with ozone systems during construction and start-up while 

focusing on the resolutions that were necessary to implement ozone systems that provide robust controls and are 

properly maintained. 


98



Pilot Test Results Perozone TM Injection Technology Kitchener, Ontario 

Dave Montgomery and Darko Strajin 

Trow Associates, Inc., 1595 Clark Boulevard, Brampton, Ontario, Canada 

The subject property is located in Kitchener, Ontario. It houses a single storey shopping mall constructed in 

the 1950s. The building has a partial basement. 

Environmental investigations revealed the presence of Tetrachloroethylene (PCE) above the current standards in 

soil and groundwater. The PCE impacts originated from historical operation of a dry cleaning facility. The lateral 

and vertical extents of the impacts had been delineated. The groundwater plume is mostly located beneath the 

building and is approximately 120m in diameter. Predominant soil type is sandy silt with sand layers and some 

silty clay lenses. 

Based on the site conditions, Trow conducted a pilot test implementing the Perozone technology. 

The Perozone injection technology is an in-Situ process which involves the injection of two chemical oxidants, 

gas phase ozone and an aqueous phase hydrogen peroxide by means of a micro-bubble sparging system. 

To start the process an air/ozone mixture and aqueous hydrogen peroxide mixture are delivered separately via 

individual supply lines to strategically placed subsurface sparge points where they are mixed. This causes fine 

micro-bubbles of ozone-containing air coated by a thin film of aqueous hydrogen peroxide liquid to be released 

from the sparge points. These air micro-bubbles, by means of conventional sparging, act to strip dissolved and 

adsorbed volatile chemicals as they begin to migrate through the subsurface soil. Since both the ozone and 

hydrogen peroxide are both strong chemical oxidants, as the VOCs contract and diffuse within the air bubbles, they 

are then oxidized and broken down by the ozone and hydrogen peroxide into carbon dioxide or less harmful 

compounds which can be found in the natural environment. 

The combination of the two oxidants also forms hydroxyl radicals, a very reactive non-selective chemical species, 

which readily breaks down a number of organic contaminants. The ozone and hydrogen peroxide degrade into 

molecular oxygen, which is beneficial both as an oxidant and for enhancing biodegradation mediated by aerobic 

microbes present in the subsurface environment. The combination of the ozone and hydrogen peroxide is used as 

an advanced oxidation process to destroy slow-to-degrade and recalcitrant organic compounds in both soil and 

groundwater. The Perozone injection system runs continuously following a pre-programmed injection sequence 

and duration for each injection point. 

In order to evaluate the effectiveness of the Perozone TM injection technology, Trow designed a pilot test consisting 

of four sub-surface sparge points and conducted controlled injections of ozone and hydrogen peroxide over a two 

month period. 

After a review of the groundwater monitoring and analytical results related to the Pilot Test of the Perozone TM 

injection/sparge point system, it is evident that application of this injection system has the potential to significantly 

lower the concentrations of VOCs in groundwater within a reasonable timeframe. Trow recommended the 

implementation of a full-scale remediation system. 

99 


Tuesday PM – Session P3 – P3-1 


The Bioassay Validation and Real-Time UV Dose Monitoring are Essential 

for Maintaining UV Disinfection Efficacy in Pharmaceutical Manufacturing 

Ismail Gobulukoglu, Ph.D. 

Science and Technology Department, Aquafine Corporation, 29010 Avenue Paine, Valencia, CA 91355, USA. 

Water is commonly used as a raw material and ingredient in the processing, formulation and manufacture of 

pharmaceutical products. Microbial control at various points in the process loop is achieved by UV water 

disinfection systems. It is critical that these UV systems are properly sized for the water process parameters, and 

monitored for ensuring their continuous desired disinfection efficiencies. However, equipment design, reactor 

efficiency and performance vary with each manufacturer’s reactor. Therefore, bioassay validation is a safeguard to 

ensure the disinfection performance achieved by UV systems is equal to, or better than, theoretical predictions of 

their performance and it is a physical verification that UV systems will perform as expected since their 

performance data is generated from real-world testing at a UV dose of 40 mJ/cm2 over a range of flows using 

EPA/DVGW validation protocol. The importance of the use of bioassay validated UV systems along with their real 

time UV dose monitoring in the pharmaceutical applications will be discussed. 


100



Results of a CFD Simulation of the UV/H 2 O 2 Advanced Oxidation Process 

Scott M. Alpert, P.E. 1 and Joel J. Ducoste, Ph.D. 2 

1. HDR Engineering, Inc. of the Carolinas, Charlotte, NC 

2. NC State University, Raleigh, NC 

In order to meet the growing needs of the water treatment community in the treatment of emerging organic 

contaminants, a CFD model was developed to simulate the UV/hydrogen peroxide advanced oxidation process. 

Design and optimization of UV/H2O 2 systems must incorporate both reactor design (i.e., hydrodynamics and lamp 

orientation) and chemical kinetics (reaction mechanisms and kinetic rate constants). In this CFD model, the 

combination of turbulence sub-models, fluence rate sub-models, and kinetic rate equations results in a 

comprehensive and flexible design tool for predicting the effluent chemical composition from a UV-initiated AOP 

reactor. To validate the CFD simulation, the results of the model under various operating conditions were 

compared to pilot reactor trials for the target contaminants of an organic dye (methylene blue) and an antibiotic 

(sulfamethoxazole). The sensitivity of the model to design conditions such as lamp output power and flow rate was 

determined. In addition, the effluent concentration dependence on the turbulence closure model, the fluence rate 

distribution model, and the reaction mechanism kinetics was evaluated. CFD for advanced oxidation process 

analysis is an important numerical tool for engineers in the evaluation of systems designed to degrade organic 

contaminants within water, wastewater, or industrial discharge systems. The optimization of such processes, 

including energy usage and hydrogen peroxide dosage, will be instrumental in allowing utilities to incorporate 

advanced oxidation systems for the removal of emerging contaminants. 

101 




Regenerating Spent Zeolites with UV and UV/H 2 O 2 to 

Enhance Removal of Endocrine Disrupting Compounds 

Safina Singh and Erik Rosenfeldt 

Department of Civil and Environmental Engineering, University of Massachusetts-Amherst 

Endocrine disrupting compounds (EDCs) have become contaminants of emerging concern due to their harmful 

effects on human and ecological heath, even at lower level of concentrations (ppb). EDCs have been detected in 

national surface waters (Kolpin et al., 2002) as they are continually discharged into surface waters by everyday 

agricultural, municipal and industrial activities. One of the methods currently being explored to attenuate EDCs in 

water includes adsorption of hydrophobic EDCs onto solid phase media such as activated carbon (AC) (Snyder et 

al., 2007, Zhang YP et al., 2005; Wintgens et al., 2003). Alternatively, high-silica zeolites provide a hydrophobic 

adsorption surface which may present some advantages over traditional AC sorption. Such sorption processes using 

hydrophobic media play a critical role in the fate and transport of toxic contaminants including EDCs. 

Zeolites are crystalline, porous alumino-silicate with well defined pore structures, and tetrahedral framework. 

The tetrahedral units can be arranged in numerous ways to engineer varying pore size and shapes of channels 

within a zeolite molecule. When the sorption capacity of activated carbon has been exhausted, a complicated, 

energy intensive process is required for regeneration. Conversely, some evidence has been shown that zeolites can 

be regenerated multiple times through relatively inexpensive methods using advanced oxidation process (AOP) 

(Koryabkina et al., 2007) and possibly even ultraviolet (UV) photolysis (Wen et al, 2008). The regeneration 

process not only presents potential for multiple uses of the sorption media, but provides the additional benefit of 

oxidative treatment of back wash water produced from zeolite regeneration. This treatment may result in a 

reduction in hazardous waste production than that associated with traditional sorption methods. 

Bench scale adsorption studies are being performed to collect baseline adsorption data for each of the EDCs in 

Table 1 on three zeolytes (ranging from low to high hydrophobicity) shown in Table 2. Freundlich and Langmuir 

isotherms models are being considered to test the adsorption capacity and strength of each of these zeolites. Results 

obtained have shown that equilibrium was reached within an hour when E2 and EE2 were separately adsorbed onto 

each zeolites- CBV-901 and CBV-780. Although CBV-780 has larger surface area it reduced EE2 by 75% as 

compared to 92% reduction by CBV-901. Despite surface area comparable to other two zeolites, CBV-400 showed 

only about 20% reduction; this may be explained by its lower SiO2/Al2O3 mole ratio and lower hydrophobicity. 

Although CBV-901 initially showed higher adsorption capacity, it did not necessarily show higher regeneration 

capacity when UV/H2O2 AOP was used. Approximately, 24% of its initial adsorption capacity was retrieved after 

one regeneration run, whereas CBV-780 consistently showed retrieval of 33% of its initial adsorption capacity for 

at least two regeneration runs. EE2 solution was used for these regeneration tests. 


102



Mixing Effects on the Chloramination Process 

Khyati Jain 1 and Irvine Wei 2 

1. CDM Inc., Walnut Creek, CA. 

2. Northeastern University, Civil and Environmental Engineering Department, Boston, MA. 

According to a recent study (AwwaRF Report 2760, 2004), more than 90 percent of water treatment plants utilizing 

chloramination for distribution system residuals indicate a certain level of dissatisfaction towards the process 

performance. One factor that may lead to such dissatisfaction is the inadequacy of mixing when ammonia is added 

to chlorinated water. If mixing is not uniform, the actual chlorine to ammonia nitrogen molar ratio will become 

variable at a micro-level, even though the overall ratio at the macro-level is close to the desired 1:1 ratio. Because 

of the non-uniform mixing, certain portions of the mixture might have a molar ratio exceeding the stoichiometric 

ratio of 1:1. In such instances, certain unintended reactions (e.g., breakpoint type of chlorine chemistry) can occur. 

This will lead to the resultant monochloramine concentration being significantly less than the stoichiometric 

concentration, based upon the calculation using the overall molar ratio. Other factors, such as pH variation in 

the micro environment, could also affect the final chemical composition of the chloramination process. 

In this study, the effect of mixing was studied by conducting breakpoint chlorination experiments under different 

levels of mixing, represented by the average velocity gradient, G in s -1 . A rather unique way of plotting breakpoint 

chlorination curve was utilized to analyze the data, which allowed a clear delineation whether the monochloramine 

formation was according to the stoichiometry. A quantitative comparison between experimental data and 

stoichiometry can clearly indicate the impact of non-uniform mixing. The experimental data clearly showed that 

as the G value increased from 35 to 500 s -1 and the monochloramine formation increased from 75 percent to 

87 percent of the stoichiometric value. The location of the breakpoint, correspondingly, increased from a molar 

ratio of 1.25 to 1.75. 

Comparison of 50rpm and 200rpm experimental data was conducted and a breakpoint curve was plotted imposing 

one over the other. It has been observed from previous literature that in ideal conditions, breakpoint occurs 

at chlorine to ammonia nitrogen molar ratio of 1.5:1, and the peak of monochloramine is expected at a molar ratio 

of 1:1. Hence, breakpoint curve was plotted at mixing speed of 50 and 200 rpm, indicating free chlorine, 

monochloramine, dichloramine, trichloramine, and total chlorine concentration at contact time of 45 minutes. 

Few studies were found in literature on mixing effects in chloramination. Data from a previous study (Yamamoto 

et al., Wat. Res.,1990) was re-analyzed and compared with the current study, and a similar trend was observed. 

In another case study, the design G value for a modern water treatment plant in metropolitan Boston was found to 

be 800 s -1 , which was higher than the maximum G value used in this study (500 s -1 ), and is likely to be sufficient. 

In conclusion, when chlorine and ammonia are combined to produce monochloramine, the degree of mixing indeed 

has significant impact on the performance of the chloramination process, and therefore must be a critical 

consideration in its design and operation. This paper will discuss the results of this study and provide practical 

guidance for those utilities currently using chloramination to optimize their disinfection process, and for design 

professionals in designing new chloramination facilities. 

103 



Wednesday Events 

May 6, 2009 

Visit us at the Registration Desk & ask about remaining availability for this BONUS interactive programming! 

Wednesday programming is NOT included in a full conference registration, and are separate events 

intended for those interested in seeing UV and Ozone applications firsthand. Each tour/workshop 

registration includes transportation and a luncheon. 

Ozone Technical Tour 

Tour stops include: 

- Cambridge, MA Water Treatment Plant (24 MGD) 

- MWRA John J. Carroll Water Treatment Plant (405 MGD) 

- Optional drop off (before or by 3pm) at Logan Int’l Airport 


Depart 8:30 AM, Return 3:30 PM 

Onsite Price: $60 

UV Technical Tour 


Tour stops include: 

- Pawtucket, RI Water Treatment Plant (25 MGD DW) 

- Brockton, MA Advanced Waste Water Treatment Plant (60 MGD WW) 

- Optional drop off (before or by 3pm) at Logan Int’l Airport 



Ozone Municipal Operations Workshop 


Intended for water treatment professionals including plant operators, 

instrument and maintenance staff and utility managers who use, or 

may use, ozone for disinfection or other purposes, engineers who 

design ozone systems for water treatment and ozone system 

suppliers and technicians who install and start up ozone equipment. 

Join us as we conduct demonstrations and "hands-on" examples of 

several activities encountered in water treatment plant, including 

Ozone systems operations and maintenance. 

Attendees will be driven by coach bus from the Hyatt Regency Cambridge to the 

Massachusetts Water Resources Authority, John J. Carroll Water Treatment Plant 

in Marlborough, MA for approximately 6 hours, including refreshment breaks and luncheon. 


104


Exhibitors 

Boston - 2009 

Ozone Water Systems, Inc. 

www.ozonewatersystems.com 

Booth #25 

Calgon Carbon Corporation 

www.calgoncarbon-us.com 

Booth #11 

Severn Trent Services 

www.severntrentservices.com 

Booth #15 

Mazzei Injector Company, LLC 

www.mazzei.net 

Booth #24 

ITT Water & Wastewater 

www.us.ittwww.com 

Booths #21-23 

Light Sources, Inc. 

www.light-sources.com 

Booth #1 

AirSep Corporation 

www.airsepcpd.com 

Booth #26 

The Ozone Man, Inc. 

www.theozoneman.com 

Booth #27 

Astro Pak Corporation 

www.astropak.com 

Booth #2 

Oxygen Generating Systems Int'l 

www.ogsi.com 

Booth #16 

Trojan Technologies 

www.trojanuv.com 

Booth #28 

Ozonia North America 

www.ozonia.com 

Booths #29-30 

IN USA Inc. 

www.inusacorp.com 

Booth #20 

Electrolytic Ozone, Inc. 

www.eoi-ozone.com 

Booth #10 

Mitsubishi Power Products, Inc. 

www.meppi.com 

Booths #6-7 

Guardian Manufacturing 

www.guardianmfg.com 

Booth #5 

Aquafine Corporation 

www.aquafineuv.com 

Booth #8 

Aquionics, Inc. 

www.aquionics.com 

Booth #3 

Plasma Technics, Inc. 

www.plasmatechnics.com 

Booth #4 

Teledyne - API 

www.teledyne-api.com 

Booth #9 

Ozone Solutions, Inc. 

www.ozonesupplies.com 

Booth #17 

OSTI, Inc. 

www.osti-inc.com 

Booth #14 

Nedap Light Controls 

www.nedaplightcontrols.com 

Booth #13 

Fuji - Water Treatment Division 

www.fujielectric.com 

Booth #19 

Statiflo Corporation 

www.statiflo.net 

Booth #12 

105 

Kerfoot Technologies, Inc. 

www.kerfoottech.com 

Booth #18 

Pacific Consolidated Industries 

www.pci-intl.com 

Booth #31


Thanks to our Sponsors 

Boston - 2009 

The 2009 Boston Conference Technical Program Committee extends their thanks and 

appreciation to the following sponsors who made this educational event possible!

Abstracts of Oral Presentations Exhibitor & Sponsor Guide Schedule ...

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