United States
Environmental Protection
Agency
Office of
Research and Development
Washington, DC 20460
EPA/600/2-81/156
September 1981
Treatment
Techniques for
Controlling
Trihatomethanes in
Drinking Water

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                                     EPA/600/2-81/156
                                     September 1981
          TREATMENT TECHNIQUES
 FOR CONTROLLING TRIHALOMETHANES
             IN DRINKING WATER
                          by

JAMES M. SYMONS, ALAN A. STEVENS, ROBERT M. CLARK,
      EDWIN E. GELDREICH, O. THOMAS LOVE, JR.,
                 AND JACK DeMARCO
                    Major Contributors

         J.K. Carswell, W.A. Feige, J.C. Hoff, K.L. Kropp,
       M.M. Lilly, G.S. Logsdon, B.W. Lykins, Jr., R.J. Miltner,
                 L.A. Moore, and B.L. Smith
        DRINKING WATER RESEARCH DIVISION
 MUNICIPAL ENVIRONMENTAL RESEARCH LABORATORY
       OFFICE OF RESEARCH AND DEVELOPMENT
      U.S. ENVIRONMENTAL PROTECTION AGENCY
                CINCINNATI, OHIO 45268


                               U& Printed on Recycled Paper

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                                PREFACE

   In this volume, the authors attempt to bring together information developed over
the past 6 years on all aspects of trihalomethanes as they relate to drinking water.
The major sections are:

     I.        Introduction
     II.       Measurement
     III.       Mechanism of Formation
     IV.       Measurement for Treatment Evaluation
     V.       Examples of Treatment Evaluation Techniques
     VI.       Treatment Techniques to Remove Trihalomethanes
     VII.      Treatment Techniques to Remove Trihalomethane Precursors
     VIII.     Use of Alternative Disinfectants
     IX.       Maintaining Bacteriologic Quality
     X.       Treatment Costs
     XI.       Summary of Treatment Considerations
     XII.      References
     XIII.     Appendix

  Section I summarizes with references to the primary literature the discovery of the
trihalomethane problem,  health and regulatory information.  Sections II-V also
summarize the literature regarding key background information necessary for an
understanding of approaches to initiating control measures and evaluation of their
degree of success. Sections VI—XI attempt to be more complete treatments of their
subjects including some previously unpublished in-house USEPA—Drinking Water
Research Division (DWRD) research results, and selected references to the primary
literature, sufficient to describe the state-of-the-art knowledge of trihalomethane
treatment techniques, bacteriologic considerations and  economic impact of
trihalomethane control strategies.  Although the authors and contributors realize
that research is  continuing on  this subject and,  therefore, new  data will be
forthcoming, sufficient new information  is available at this time to  warrant this
update of the "Interim Treatment Guide for the Control of Chloroform and Other
Trihalomethanes" June 1976 (Unpublished).
  The authors and contributors hope  this compilation of research material will
prove  useful to  those  challenged with  the  responsibility  of reducing the
trihalomethane content of our Nation's drinking water.

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                               ABSTRACT

  In   1974,  trihalomethanes  (chloroform,   bromodichloromethane,
dibromochloromethane, and bromoform) were discovered to be formed during the
disinfection  step of drinking water if free chlorine was the disinfectant. Various
surveys have shown that this reaction occurs wherever theabove conditions are met.
This, coupled  with the perceived hazard to the consumer's health, led the U.S.
Environmental Protection Agency to amend the National Interim Primary Drinking
Water  Regulations to include a maximum contaminant level of 0,10 mg/ L for total
trihalomethanes. The Safe Drinking Water Act (Public Law 93-523) requires that
every drinking water regulation contain a statement as to what treatment techniques
water utilities can employ to achieve compliance with the regulation as well as the
maximum  contaminant level.  This report satisfies  the treatment document
requirement for the trihalomethane regulation.
  Following a general discussion of measurement  techniques, mechanisms of
formation, and techniques for evaluating treatment,  the three approaches for
controlling trihalomethanes (removing trihalomethanes, removing trihalomethane
precursors, and the use of disinfectants other than free chlorine) are discussed in
detail.  Finally, a thorough discussion of the impact of  trihalomethane control on
bacteriologic quality of drinking water and the cost of the various unit processes
investigated is contained herein.
  For  trihalomethane  removal,  aeration—either  by  diffused-air  or  with
towers—and adsorption—either  by powdered activated carbon or  granular
activated carbon—is effective. The major  disadvantage of this approach is that
trihalomethane precursors  are not removed by  aeration. For trihalomethane
precursor control, effective processes are: 1) oxidation by ozone or chlorine dioxide;
2) clarification by coagulation, settling and filtration,  precipitative softening, or
direct  filtration; or 3) adsorption by  powdered  activated carbon or granular
activated  carbon.  In  addition,  some  modest  removal  or destruction  of
trihalomethane precursors can  be achieved  by  oxidation  with  potassium
permanganate, lowering the pH, or moving the point of chlorination to the clarified
water.  Further, the utility's source should be examined to  determine whether or not it
can  be  improved to  contain  less  trihalomethane  precursor.  Lowering  of
trihalomethane precursor concentrations has the additional advantage of reducing
overall disinfectant demand, thereby reducing the possibility of the formation of all
disinfection byproducts.
  Neither chlorine dioxide, nor ozone, nor chloramines produce trihalomethanes at
significant concentrations when used alone as disinfectants. Furthermore, the cost of
any of these unit processes is very low. The major disadvantage of using alternate
disinfectants for trihalomethane control relates to the lack of any precursor removal.
Although no trihalomethanes will be produced as disinfection byproducts, other
byproducts  will still be produced as the oxidants (disinfectants) react with organic
matter in the water.  Further, some of these byproducts will be halogenated if
chlorine  dioxide  or  chloramines  are used  as the disinfectant  alternative.
Additionally,  each of the disinfectants itself has  inherent  disadvantages; for
example, ozone does not produce a residual for the distribution systgm; chloramine
is a weaker  disinfectant than free chlorine and may itself have unique toxicologic
properties, and chlorine dioxide produces  chlorite and chlorate as inorganic by-
products, anionic species whose health effect is currently unknown.

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  Each of these approaches has advantages and disadvantages as well as different
degrees of effectiveness and unit costs, and these are detailed herein to help water
utility managers, consulting engineers, Primacy Agencies, and others to choose the
best approach  to solve a given problem. Studies have shown that  any of these
techniques,  if  used  properly  and if final disinfection is applied diligently and
monitored closely, can be used for trihalomethane control without any deterioration
in bacteriologic quality at the consumer's tap.
vlii

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                             CONTENTS

Foreword	    iii
Abstract	,	,	,	    vii
Acknowledgments	    xi
   I.   Introduction	     1
   II.   Measurement	     6
  111.   Mechanism of Formation	    10
  IV.   Measurement for Treatment Evaluation	    23
   V.   Examples of Treatment Evaluation Techniques	    29
  VI.   Treatment Techniques to Remove Trihalomethanes (InstTHM)...    36
 VII.   Treatment Techniques to Remove Trihalomethane Precursors
        (THMFP)	    87
VIII.   Use of Alternative Disinfectants	   160
  IX.   Maintaining Bacteriologic Quality 	   194
   X.   Treatment Costs			   228
  XI.   Summary of Treatment Considerations	,	   256
 XII.   References	   26?
XIII.   Appendix	   282
Index	   286

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                       ACKNOWLEDGMENTS
  No project this  large could  be  accomplished alone,  and the authors and
contributors acknowledge the participation of their associates. First, we wish to
thank Gordon G. Robeck,  Director, Drinking Water Research Division, without
whose leadership and management skills the USEPA research reported herein could
not have been conducted. Second, we would like to thank those"other DWRD staff
members who contributed  considerable time  and effort to this work; Diane
Hinderberger, Paul Keller,  Steven Canter, Raymond  Taylor, Martin  J. Allen,
Elizabeth Creamer, Virginia Maphet,  Patricia Pierson, William Winters, Paul
Dorsey, Walter  Elbert, Ronald Dressman, Dennis Seeger, and Clois Slocum.
Thanks is given to Dr. Irwin J. Kugelman of the  Wastewater Research  Division,
Municipal Environmental Research Laboratory, USEPA, who generously gave of
his time to help with the Aeration part of Section VI.
  We wish to acknowledge the contributions of the principal investigators on the
DWRD-sponsored  extramural  projects from  which  much of  the  research
information was collected:
  Mr.  Noel V. Brodtman, Jefferson Parish Water Works, Jefferson  Parish, LA
  Mr.  Patrick R. Cairo, Philadelphia  Water Department, Philadelphia, PA
  Dr. Russell F. Christman, University of North  Carolina, Chapel Hill, NC
  Dr. James K, Edzwald, Clarkson College, Potsdam,  NY
  Dr. Richard S. Engelbrecht, University of Illinois, Urbana-Champaign, IL
  Dr. William H. Glaze, North Texas State University, Demon,  TX
  Dr. Leland L, Harms and Dr, Robert Looyenga, South Dakota School of
     Mines and  Technology, Rapid City, SD
  Mr.  Wendell  R. Inhoffer and Mr.  Richard E.  Roby, Passaic Valley Water
     Commission, Little Falls, NJ
  Dr. Riley Kinman, University of Cincinnati, Cincinnati, OH
  Mr.  David Kittredge, Manchester Waterworks, Manchester, NH
  Mr.  Donald B. Mills, City of Evansville, IN
  Mr.  Richard J.  Miltner, Ohio River Valley  Water Sanitation Commission,
     Cincinnati, OH
  Dr. John.T, O'Conner, University of Missouri, Columbia, MO
  Dr. Charles Oulman, Iowa State University, Ames, IA
  Dr. Aaron  A. Rosen (deceased) and  Mr.  David Hartman, Cincinnati
     Water Works, Cincinnati, OH
  Mr.  Dominick D. Ruggiero, NKRE, P.C., New York, NY
  Dr. Pasquale V. Scarpino, University of Cincinnati, Cincinnati, OH
  Dr. Michael J. Semmens, University of Minnesota, Minneapolis, MN
  Dr. Gordon Sharp, University of North Carolina, Chapel Hill, NC
  Dr. Vernon L, Snoeyink, University of Illinois, Urbana-Champaign, IL
  Dr. Charles A. Sorber, University of Texas, San Antonio, TX
  Dr. Otis Sproul, Ohio State University, Columbus, OH
  Mr.  G. Joseph Sullivan,  Sewage and Water Board of New Orleans,
     New Orleans, LA
  Mr.  Albert Sylvia, Lawrence Experiment Station, Lawrence, MA
  Mr.  Michael Taras,  AWWA Research Foundation, Denver, CO
  Mr.  Paul R. Wood, Florida International University, Miami, FL
  We wish to thank Edward Kispert and  George Hicks of the Cincinnati Water
Works for their assistance and cooperation in supplying water for the in-house

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USEP A-D WR D studies, and we wish to thank those whose time and talent made the
final  publication  of this  volume  possible, particularly,  Marion  Curry,  Ann
Hamilton, and WAPORA, Inc., who handled the final production.
  Finally, we wish  to  thank those who  provided  us with review and helpful
comments: Joseph Cotruvo, Chieh Wu, Craig Vogt, and Stig Regli of the Office of
Drinking Water, USEPA,  Washington, D.C.; Mac Weaver, USEPA Region VI,
Dallas, TX; and David Kittredgeofthe Manchester Water Works, Manchester, NH.
Special thanks are given to our designated peer-reviewers: Dr. Michael J. McGuire
of the Metropolitan  Water District of Southern California, LaVerne, CA,  Dr.
Michael C. Kavanaugh of James M. Montgomery Consulting  Engineers,  Inc.,
Pasadena, CA; and the many staff members of their respective organizations. The
time spent and the depth of their  two reviews, particularly because they involved
their colleagues, were extraordinary and contributed greatly to the accuracy and
final quality of this document.
xi!

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                               SECTION I
                            INTRODUCTION

  Since the 1974 discovery of trihalomethane formation in drinking water as a result
of chlorinatiori,1'2* much research has been conducted to determine:

  1.  whether trihalomethanes affect the health of consumers;
  1.  how trihalomethanes should be measured;
  3.  how water quality conditions influence trihalomethane formation;
  4.  treatment techniques) a drinking water utility could use to reduce tri-
      halomethane concentrations in distributed water;
  5.  what effect altering treatment procedures to control trihalomethanes will
      have on the bacteriologic quality of distributed water; and
  6.  the cost of the various treatment possibilities.

  The results of these studies "were the basis for the U.S. Environmental Protection
Agency's (USEPA) amendment to the National Interim Primary Drinking Water
Regulations issued November 29, 1979—an amendment establishing a maximum
contaminant level (MCL) of 0.10 mg/L total trihalomethanes (TTHM) in drinking
water.3
  Section 1401 (1)(D) of the Safe Drinking Water Act, Public Law 93-523, states
that "the term 'primary drinking water  regulation'  means a  regulation which
contains criteria  and procedures  to  assure a  supply of drinking  water which
dependably complies with such maximum contaminant levels.. ."and Section 1412
(a)(2) states that "National interim primary drinking water regulations promulgated
under paragraph (a)(l) shall protect health to the extent feasible, using technology,
treatment techniques, and other means, which the Administrator determines are
generally available (taking costs into consideration). . ." Thus, for any regulated
contaminant,  a  "Treatment  Techniques"  document  must  accompany  the
establishment of a "Maximum Contaminant LeveP'(MCL) to provide compliance
guidance. This research reportt satisfies the treatment document requirement for the
Trihalomethane Regulation and is a companion to the "Manual of Treatment
Techniques for Meeting the Interim Primary Drinking Water Regulations," EPA-
600/8-77-005 (April,  1978).4 For further information on the Regulation,3 the reader
is referred to a document entitled "Trihalomethane Implementation Guidance"5 that
is available from the Office of Drinking Water, USEPA,  Washington, D.C.
  The purpose of this research report is to review the discovery of the problem; to
summarize the  results  of research  areas 1,  2, 3, 5, and 6  (above) and the
Trihalomethane Regulation3; and to detail the results of the treatment studies, i.e.,
research area 4 (above).
  The first five Sections of this report provide background information needed to
understand and interpret the treatment research  presented in Sections VI through
VIII, In Section IX are summarized the findings concerning the impact of changing
treatment to control trihalomethane concentrations on the bacteriologic quality in
distributed water. This information will aid in understanding the interrelationship
•Key papers are cited as references; the reader is referred to the literature citations in each of these papers for a more complete
 reading list.
fThis work has been synopsized in "* Removing Trihaiornethanes from Drinking Water—An Overview of Treatment Tech-
 niques," J.M. Symonj. A, A. Stevens, R.M. Clark, E.E. Geldreich, O.T. Love, Jr., and J. DeMarco. Water Engrg,& Mgmt,,
 128 <7j: 50-53, 56, 61-64, July I9gi.


                                                     Section I. Introduction   1

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 between disinfection  practices,  trihalomethane concentrations,  and  resulting
 bactcriologic quality. Section X on "Costs" will help the reader choose the most cost-
 effective treatment technique by combining the information in Sections VI through
 VIII on treatment effectiveness with the cost data in Section X. Section XI is a
 summary of treatment approaches with discussions of cost/effectiveness  tradeoffs
 and examples of hypothetical situations that demonstrate how to select cost-effective
 treatment strategies  for THM  control.

 Discovery

  Although  sporadic  reports  of  the presence  of  chloroform  and   other
 trihalomethanes in finished drinking water occurred before 1974,* the reports that
 year by  Rook1 in The  Netherlands and by Bellar,  Lichtenberg, and  Kroner2 of
 USEPA clearly demonstrated that these contaminants were formed during the water
 treatment process as a result of chlorination. This finding prompted a survey in early
 1975 of 80 water utilities in the United States,  79 of which practiced free residual
 chlorination or combined residual chlorination. This survey, the National Organics
 Reconnaissance Survey (NORS), showed that all of the water utilities that  used free
 chlorine (sometimes  called  chlorine)  in their treatment practice had varying
 concentrations of at least four trihalomethanes in their finished drinking water and
 that they were formed  during treatment.7 Follow-up studies* in 1975 and  1976,
 including the National Organics  Monitoring Survey (NOMS), unpublished  at this
 writing, confirmed this finding with samples collected at 113 locations during three
 different seasons.
  These surveys, combined with like results from all over the world, showed that the
 reaction of chlorine to produce trihalomethanes was widespread and surely  had been
 occurring for  as long as chlorine  had  been  in  use in  water  treatment.
 Trihalomethanes in drinking water had usually escaped detection until 1974 because,
 before that time, the analytic  techniques used to measure the organic content of
 water did not detect them. Once discovered, however, extensive research was begun
 to determine if their presence in drinking water was a health hazard for consumers.
 The results of the health effects studies that led up to the promulgation of the Tri-
 halomethane Regulation' are summarized below.

Health Effects

  People are exposed to chloroform in the air they breathe and the food they eat.
Analysis of the relative contribution of chloroform in drinking water, air, and food
assumes various levels of exposure based on monitoring studies. Drinking water may
contribute from zero to more than 90 percent of the total daily body intake.
  Chloroform has been shown to be rapidly absorbed on oral and intraperitoneal
administration and to be subsequently metabolized to carbon dioxide, chloride ion,
phosgene, and other unidentified metabolites. The metabolic profile of chloroform
in animal species such as mice, rats, and  monkeys is qualitatively similar to that in
humans.
  Mammalian responses to chloroform  exposure include: central nervous system
depression, hepatoxicity, nephrotoxicity, teratogenicity, and carcinogenicity. These
responses are discernible in mammals after oral and inhalation exposures to high
levels of chloroform ranging from 30 to 350 mg/kg of body weight, the intensity of
 response being dependent upon  the dose. Although less toxicologic information
is available for the bromine-containing trihalomethanes, mutagenicjty and carcin-
 ogenicity have been detected in some test systems. Physiological activity is thought
to  be  greater for the bromine-containing trihalomethanes  than  for chloro-
form.
  Although short-term toxic responses to trihalomethanes in drinking water are not
documented, the potential effects of chronic exposures to trihalomethanes should be
a matter of concern. Prolonged administration of chloroform at relatively high dose

 2  Treatment Techniques for Controlling  Trihalomethanes in Drinking Water

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levels,, 1QO to 133 ing/kg,.to rats and mice manifested oncogenic effects, Oncogenic
effects were not observed at the lowest dose levels, 17 mg/kg, in three experiments.
Because  methods do not now  exist to  establish a  "threshold no effect" level of
exposure to carcinogens, the preceding data do not imply that a "safe" level of
exposure can be established for humans.
   Human epidemiologic evidence is inconclusive, although several studies have
found positive associations with some cancer sites. Eighteen retrospective studies,
discussed in detail  in  Attachment 7 of the Trihalomethane Regulation,3 have
investigated some aspect of a relationship between cancer mortality or morbidity
and drinking water variables. Because of various limitations in the epidemiologic
methods, difficulties with the water quality data, and problems with the individual
studies, the present evidence does  not lead to a firm conclusion that an association
exists between contaminants in drinking water and cancer mortality or morbidity;
causal relationships  cannot be  proven on the basis of results from epidemiologic
studies.  When  viewed collectively, however, the epidemiologic studies provide
sufficient evidence for maintaining the hypothesis that a health risk may be occurring
and that the positive relationships may be reflecting a causal association between
constituents of drinking water and cancer mortality.
   Using  different models, the Science Advisory Board, the National Academy of
Sciences, and  USEPA's  Carcinogen   Assessment Group  have  estimated the
incremental risks associated with the'exposure from chloroform in drinking water.
The  exposure, to chloroform from air and food  has  not been included ia these
computations. The risk estimates associated  with theTTHM MCLofO.10 mg/ Lare
essentially the same from the National Academy of Sciences and the Carcinogen
Assessment  Group  computations, i.e., they would predict an  incremental risk of
three to four per 10,000 population consuming 2 liters of water containing 0.10 mg/ L
chloroform  daily for 70 years.
   In summary,"on the basis of the available toxicologic data, chloroform has been
shown to be a carcinogen in mice and rats at high dose levels.  Because its metabolic
pattern in animals is qualitatively  similar to that in humans, chloroform should be
suspected of being a human carcinogen. Epidemiologic studies also suggest a human
risk.  Although documentation of  other trihalomethane  toxicity is  not so well
established, they should be suspected of posing similar risk. Because of  these
suspected health effects, the  Trihalomethane  Regulation was  promulgated  on
November 29, 1979,! The Trihalomethane Regulation is summarized below.

Regulation

History—
   Four statements in the Federal Register**'-*' trace the regulatory history of the
control  of organic contaminants  in drinking water. The first statement was  an
Advance Notice for  Proposed Rulemaking published July 14, 1976, in which the
USEPA  .proposed  several  options for the control of trihalomethanes  and other
organic contaminants in  drinking water and requested comments from the  public.
   As a  result of this statement and the public comments,  USEPA proposed a
two-part Regulation for organic contaminant control in drinking water on February
9, 1978.'° This document specified an MCL for the control of trihalomethanes and
specified that a treatment technique, granular activated carbon, be installed-at water
utilities where source waters were significantly contaminated for thecontrol of other
synthetic organic contaminants.*
   On July 6, 1978, the USEPA published supplemental technical information  on
this subject and extended the public comment period.11 The final Regulation for the
control of trihalomethanes only was published in the Federal Register on November
•Nole, although the February 9.1978, proposed Trihalomethane Regulation10 is often misunderstood 10 say that the USEPA
 was-proposing to r*?i/irplhe use of granular activated carbon adsorption for the control of trihalomethane concentrations.
 this was not the case.   .


                                                     Section I. Introduction  3

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 29, I979.3 In this same document, the proposed regulation of other synthetic organic
 contaminants by using granular activated carbon treatment was deferred, and may
 be re-proposed at a later time.
   On January 11, 1980, the American Water Works Association, together with the
 City  of Englewood, Colorado, and the Capital City Water Company, a Missouri
 corporation, filed a Petition for Review with the U.S. Court of Appeals for the
 District of Columbia Circuit, asking the court for "a review of a final rule" as allowed
 by Section 1448 (a)(l) of the Safe Drinking Water Act (Public Law 93-523). At this
 writing no action has been taken on this Petition.

 Summary of Trlhalomethane Regulation (promulgated November 29,1979)3—
 Maximum Contaminant Level (MCL):
           0.10 mg/L total trihalornethanes (TTHM) (Sum of concentrations of
           compounds 1, 2, 3, and 4,  Table 1).

 Applicability.
           Community water systems that add disinfectant to the treatment process
           (ground and surface).
       Effective:
           Systems >75,OOQ:    2 years after promulgation
           Systems 10-75,000:  4 years after promulgation
           Systems < 10,000:   Discretion of Primacy Agency (State, or USEP A
                                  if  the State does not have primacy)

 Monitoring Requirements:
           Twelve-month-running average of  a minimum of 4 samples per quarter
           per treatment plant taken on the same day. Systems using multiple wells
           drawing raw water from a single  aquifer may, with  Primacy Agency
           approval, be considered to have one treatment plant for determining the
           required number of samples.
       Effective:
           Systems > 75,000:   1 year after  promulgation
           Systems 10-75,000:  3 years after promulgation
           Systems < 10,000:   Primacy Agency discretion
       Sample Locations:
           25 percent at extremity of the distribution system; 75 percent at locations
           representative of the population distribution.

 Adjustment of Sampling Frequency,
           For groundwater systems, reduced monitoring may be appropriate for
           certain systems. The Primacy Agency may reduce the requirements
           through consideration of appropriate data including demonstration by
           the system that the maximum total trihalomethanepotential* (MTP) is
           less than 0.10 mg/ L. The minimum frequency would be one sample'per
           year for MTP taken at the extremity of the distribution system. For
           groundwater systems not meeting the above MTP limit and for surface
           water systems, the Primacy Agency may reduce the monitoring require-
           ments if, after 1 year of data collection, TTHM concentrations are
           consistently below 0.10 mg/L. The minimum frequency  would be one
           sample per quarter per treatment plant for total trihalornethanes taken
          at the extremity of the distribution system. The original frequency would
          be reinstated if the TTHM  concentrations exceed 0.10 mg/L or if the
          treatment or source is modified.
•The maximum total irihalomethane potential is defined as the total trihEtlomethane concentration in a sample after storage
 for ?dt?*at 25*C(?7*F) of above in the presence of a t/istttfeciam residual or after the use of USEPA method 501.1 if no
 diiinfeuarit residual is present after initial storage.


 4  Treatment Techniques for Controlling Trihalornethanes in Drinking Water

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Reporting Requirements:
      To Primacy State:
          Average of each quarterly analysis, within 30 days. Until Primacy States
          have  adopted the regulations,  reporting will  be to USEPA unless
          Primacy State requests receipt of data.
      To Public and Primacy State:             '
          Running-12-month average of each quarterly sample if total trihalo-
          methane concentration  exceeds MCL, as prescribed by the public
          notification  provisions.

Other Requirements:
      To Ensure Microbiologic Quality:    '       '
          Primacy Agency approval of significant modifications in the treatment
          process for the purpose of meeting the TTHM  MCL.
      Analytic Requirements:
          In accordance with specified methods  (purge and trap or liquid-liquid
          extraction) conducted by certified laboratories (see Section II, Measure-
          ment).

  As a further aid to understanding the Regulation3 the reader is referred to the
document "Trihalomethane  Implementation Guidance"* that is available from
Office of Drinking Water, USEPA, Washington, D.C, The Appendix contains the
entire Trihalomethane Regulation from the Federal Register,
                                                    Section I. Introduction  5

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                              SECTION II
                           MEASUREMENT

  Appendix C of the Trihalomethane Regulation3 contains a detailed description of
the USEPA approved methods for sampling and analyzing drinking water for
trihalomethane concentrations. These techniques are summarized here so that the
reader will understand the general approach.

Sample of Collection and Handling

   1. The sample containers should have a total volume of at least 25 mL. Narrow-
mouth screw cap bottles with poiytetrafluoroethylene (PTFE) faced silicon septa cap
liners are strongly recommended.
  2. If the trihalomethane concentration at the time of sampling is desired, a
chemical reducing agent, sodium thiosulfate or sodium sulfite, must be added to the
sample to arrest the  formation of trihalomethanes after sample collection.  If
chemical stabilization is employed, the reagent must be also added to the blanks,
  3. The sample bottles are filled in such a manner that no air bubbles pass through
the sample as the  bottle is filled. The  sample is then inverted; the absence of
entrapped air indicates a successful seal.
  4. If a chemical reducing agent has been added to the sample bottle, the bottle is
shaken vigorously for  1 minute after sealing the bottle.
  5. Blanks are prepared in duplicate at the laboratory by filling and sealing sample
bottles with waters containing a low concentration of organics just before shipping
the sample bottles to the sampling site.  The blanks  are shipped to and from the
sampling site along with the sample bottles. The blanks and the samples collected at a
given site are stored together.
  6. The procedure recommends that all samples be analyzed within  14 days of
collection.

Measurement Techniques

  Although other techniques were investigated,12 the USEPA has approved two gas
chromatographic (GC) techniques for the measurement of trihalomethanes. These
are generally called the "Purge  and  Trap" and  "Liquid-Liquid  Extraction"
techniques. Although  both methods have advantages and disadvantages, when
performed properly, they  have been shown to produce equivalent  results for
trihalomethane analysis.  The two appoved  methods are summarized below:

Purge and Trap Summary—
   1. Trihalomethanes are purged by an inert gas that is bubbled through the aqueous
sample. The trihalomethanes, along with other organic constituents that exhibit low
water solubility and a vapor pressure significantly greater than water, are efficiently
transferred from the aqueous phase to the gaseous phase. These compounds are
swept from the purging device and are trapped-in a short column containing a
suitable sorbent. After a predetermined time, the trapped components are thermally
desorbed and  back flushed onto a gas chromatographic column and separated under
temperature programmed conditions. Measurement is accomplished with a halide
specific detector such as electrolytic conductivity or microcoulometric titration.

6  Treatment  Techniques for Controlling Trihalomathanes in Drinking Water

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   2. Confirmations of identity may be obtained using dissimilar columns, or by mass
 spectrometry (MS).
   3, Aqueous standards, blanks, and unknowns are purged and analyzed under
 identical conditions to compensate for varying purging recoveries.
   4. The total analysis time, assuming  the absence  of other organohalides,  is
 approximately 35 minutes per sample.
 Liquid-Liquid Extraction Summary—
   1. Ten mL of sample are extracted at one time with 2 mL of solvent (pentane,
 hexane, or methylcyclohexane). Three /jL of the extract are then injected into a gas
 chromatograph equipped with a linearized electron capture detector for separation
 and analysis. The absence of trihalomethane peaks in the raw water is generally
 ample evidence of an interference-free finished water analysis.
   2. When needed, confirmatory evidence may be obtained using dissimilar columns
 and temperature programming. When  component concentrations are sufficiently
 high (>50 ^g/ L), halide specific detectors may be employed for improved specificity.
 Unequivocal confirmations of identity  at high concentrations (>50 pg/L) can be
 obtained using MS in place of the electron capture detector. At concentrations below
 50 figi L, unequivocal confirmation of identifications can only be performed by the
 purge and  trap technique  outlined above.
   3. Standards are dosed into water with a low concentration of organics, and the
 standards  are extracted and analyzed  in a manner identical to the samples to
 compensate for possible extraction losses.
   4. The extraction and analysis time  is  10 to 50 minutes per sample depending upon
 the chromatographic conditions chosen.


 Units of Concentration—
   Because the gas chromatographic techniques used to measure trihalomethanes are
 based  on  gravimetric (weighed) standards,  and  because  the Trihalomethane
 Regulation  is based on total trihalomethanes summed on a weight basis, ^tg/L,
 trihalomethane concentrations are most  often seen in the literature expressed in this
 manner.  Frequently, however, expressing the concentration in terms of chemical
 equivalents (mieromoles/ L)  is  more  desirable.  Chemical  equivalents  .are an
 expression  of the number  of molecules present (6.02 X I0"//umol), and are, there-
 fore, a better unit of expression when concentrations of reactive sites(precursors) or
 active sites (adsorption) are being discussed because the interpretation of research
 results  will  not  be  influenced  by the differing  molecular  weights  of the
 trihalomethanes present in various  mixtures.  Throughout  this document, both
 systems of  units are used. In detailed interpretation of research results, the units of
 /amol/ L are the most appropriate; however, to aid the reader in judging the success of
 a water utility to meet the Trihalomethane Regulation,3 the data are more often
 reported in terms of weight concentration (fig/ L) rather than, or in addition to, the
 more chemically meaningful molecular  concentration
Quality Assurance

  The USEPA has set a requirement that, to be approved, a laboratory must be able
to measure the concentration of the individual trihalomethanes as well as the TTHM
concentration in a quality control sample supplied by USEPA to within ±20 percent
of the "true" value. This determination  must  be made annually., If, after an
investigation of its  procedures,  a  laboratory cannot meet this requirement, it is
allowed to demonstrate its effectiveness on repeat quality  control samples.

                                                  Section II. Measurement  7

-------
 Surrogate Measurements

   Because the analysis for the presence of trihalomethanes  is a GC procedure
 requiring skilled operators and some time to complete, a simple rapid surrogate
 measurement that would predict trihalomethane concentrations seemed desirable.
 Because chlorine reacts with precursors to form trihalomethanes, a test that would
 measure the  precursor concentrations in water was thought to  be useful  for
 predicting trihalomethane concentrations.
   No direct test for trihalomethane precursors exists,* so a test for general organic
 content was considered as an alternative. The difficulty with using a general organics
 test as a measure of trihalomethane precursors is that precursor concentrations are
 not a constant percentage of the general organic content. Nevertheless, in the report
 of the National Organics Reconnaissance Survey,7 nonpurgeable organic carbonf
 (NPOC)  was  proposed as  a  surrogate analytic  test for  the trihalomethane
 measurement. The report' suggested that raw water NPOC concentrations could be
 used to predict TTHM concentrations in micromoles per liter  in finished water (1
 /imol/L is approximately 120 fig/L as CHClj).
   For the analysis of the data in Reference 7, the NPOC data were grouped in
 concentration ranges and the mean TTHM concentration for all data in a given
 NPOC range was plotted against the mid-point of the given NPOC range. These data
 were very linear when plotted arithmetically. Subsequent research (see Section  III,
 Mechanism of Formation) showed, however, that several water quality conditions
 such as precursor type, temperature, pH, bromide concentration, and  disinfectant
 type, as well as time of exposure to free chlorine before measurement influenced the
 resulting TTHM concentration in a given location. Therefore, the suggestion noted
 above was reviewed.
   Figure 1, in which all the data from the NORS7 are plotted, shows the scatter
 around the line of best fit by least squares. The correlation coefficient, 0.77, is highly
 statistically significant,  showing  that, in general,  waters with higher NPOC
 concentrations will produce more trihalomethanes than waters with lower NPOC
 concentrations. The  scatter,  however, is great, as demonstrated by  the high
 calculated 95  percent confidence limit, ±0.5 fimol TTHM per liter (approximately
 ±60 A
-------
4.0  r
    0             5             10            15

                SOURCE WATER NPOC CONG, mg/L

 Figure 1. Raw water nonpurgeable organic carbon vs. finished
         water total trihalomethanes. (Data obtained from the
         National Organics Reconnaissance Survey.')
                                        Section If. Measurement  9

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                              SECTION III
                   MECHANISM OF FORMATION
Nomenclature
   For those readers unfamiliar with organic nomenclature, the following discussion
 defines some of the terms. Although methane gas does not seem to be involved, the
 reaction  of chlorine in water with certain organic compounds,  under certain
 conditions,  produces a group of halogen-substituted single carbon compounds.
 These compounds  are named as derivatives of methane (CH,i) (Table )).
   Under typical circumstances, the trihalomethanes produced in drinking water are
 dominated by compounds 1 and 2, but compounds 3 and 4 are frequently found and
 compounds 5 and 6 have been detected (Table 1).  Note, the arithmetic sum of the
 concentrations of compounds 1,2, 3, and 4 has been defined in the Trihalomethane
 Regulation3 as "Total Trihalomethanes" (TTHM).

 General Mechanism

  The formation of trihalomethanes during free chlorination of drinking water
 results from a complicated mechanism of attack by aqueous halogen species on
 natural aquatic humic substances, i.e., humic and fulvic acids, rather than organic
 compounds whose source is industrial water pollution. Thus, trihalomethanes result
 from the generalized reaction:

   FRF.F           PRECURSORS
 rwrnRIMP + (HUMIC SUBSTANCES) -  TRIHALOMETHANES +
 CHLUKIMt      AND BROMIDE

Several factors influencing this reaction15"" are summarized below. Design of the
 most effective treatment strategy depends  on a knowledge  of the trihalomethane
formation reaction  and the factors  controlling it.

 Effect of Time

  The formation of trihalomethanes under natural conditions is not instantaneous.
 Although, under some reaction conditions the formation of trihalomethanes may be
 completed in less than an hour, in other circumstances, several days may be required
 before the maximum yield of trihalomethanes occurs.
  Varying apparent "yields" of trihalomethanes reported throughout the literature
 under varying reaction conditions may be influenced by the reaction rate. Thus, a
 lower reported "yield" may be the result  of the  reaction  proceeding  toward
 "completion" at a slower rate. Reaction conditions may also, however, influence the
 yield of trihalomethanes obtained at a time when no further reaction appears to be
 occurring.
  The precise effect on the kinetics (rate) of  trihalomethane formation of various
 parameters influencing it or yield  at "completion" of the  reaction is difficult to
 predict because of the complexity of the reactions between aqueous free chlorine and
 the mixture of precursors  of largely unknown structure. Thus, from a practical
 standpoint, when yield of trihalomethanes is discussed, the time allowed for the
 reaction and other  conditions discussed below must  be defined.

 10  Treatment Techniques for Controlling Trihalomothanes in Drinking Water

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         TABLE 1, STRUCTURAL FORMULAS AND NAMES
                   OF THE TRIHALOMETHANES
   Formula
                  Name
                                      Formula
                                                     Name
        Cl
         I
1,  H — C — CI
        Cl    Trichloromethane
               (Chloroform)
                  CHCIj
                                           I
                                           I
                                   6.  H - C - Cl
                                           i
                                           Br    Bromochloro-
                                                iodomethane
                                                  CHCIBrl
        Br
         I
2. H — C •
         I
        Cl
             Cl

             Bromodichloromethane
                   CHBrCI,
         I
         I
7. H  - C
         I
        Cl
Chlorodiiodomethane
      CHCII,
        Br
         I  '
3. H — C — Cl
        Br   Dibromochloromethane
                   CHBrjCI
                                            I
                                            I
                                   8. H - C - Br
                                            I
                                           Br
                                                Dibromoiodo methane
                                                      CHBr,I
        Br
         i
4, H  — C  — Br
        Br   Tribromomethane
               (Bromoform)
                  CHBr,
                                   9. H - C — Br
                                            I    Bromodiiodomethane
                                                      CHBrl,
         I
         I
6, H — C  — Cl
         I
        Cl
                                            I
                                  10. H  - C  —  I
             Dichloroiodomethane
                   CHCI,I
         I    Triiodomethane
               (lodoform)
                  CHIa
                                    Section III. Mechanism of Formation  11

-------
Effect of Temperature
  When Ohio  River water was chlorinated in the laboratory, increasing the
temperature had  a positive effect on trihalomethane formation15 (Figure 2).  A
corresponding seasonal variation, noticed at a water utility using the same source,
has been shown to be largely a temperature  effect. Thus, trihalomethane control
problems  become more acute  during hot weather when water temperatures are
higher during treatment and distribution.
  Data collected  by the  Ohio  River  Valley Water  Sanitation  Commission
(ORSANCO)1* showed  that at several water utilities the finished water TTHM
concentrations  varied  seasonally  and were lower in  the winter when water
temperatures were lower, although data were  not controlled for possible variations
in precursors and other treatment condition variables (Figure 3).
          250
          200 - -
          150 --
      X
      O)
      3.
      O
      z
      O
      O
       n
      O

      O
         100 --
          50 -
                                  40°C
                      20
                                                         100
                                                                 120
                               40       60       80

                                REACTION TIME, hr

            Figure 2. Effect of temperature on chloroform formation.18

12  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
      o
      z
      o
      o
         180
         160-
         140
         120
         100
          80
          60
          40-
          20 --
                                                    I    I    I    I
                                                  *  Wheeling, WV
                                                  O  Louisville, KY
                                                  •  Huntington, WV
                                                  O  Cincinnati. OH
                                                  A  Evansvilie, IN
                 JUL
                 1977
_H	1	1	1	1—|	(_
 SEP     NOV     JAN     MAR

        DATE OF SAMPLING
MAY
        JUL
       1978
         Figure 3. Seasonal variation in finished  water TTHM concen-
                  tration for treated surface waters.1"
Effect of Bromide and Iodide Concentration

  Bromide and iodide ions are oxidized by aqueous chlorine to species capable of
participating in organic substitution reactions resulting in the formation of pure- and
mixed-halogen trihalomethanes.  When Bunn et al.  chlorinated Missouri  River
water in the presence of added fluoride, broniide, and iodide, they first confirmed
one of Rook's suspicions that this could occur in aqueous systems. They observed the
formation of all ten possible chlorine-, bromine- and iodine-containing pure- and
mixed-halogen trihalomethanes shown in Table 1, On a theoretical basis, oxidation
of fluoride by  aqueous chlorine to active fluorine species followed by substitution
was not expected and was not observed.
  Figures 4A and 4B illustrate the effect that adding bromide has on the ratio of
trihalomethanes produced during the reaction of aqueous chlorine with humie acids.
Note that bromine substitution is favored over chlorine, even though chlorine is
present in large excess compared with the initial bromide.
                                      Section III. Mechanism of Formation  13

-------
        1,2
                                                                 313
        1-2 --  B
       1.0
    o
    E
    a.
    o
    z
    o
    o
    5

    I
0.8 --
0.6 --
0.4 --
       0.2--
                                             12
                                                       62
                                                          1
                                                                 313
                             BROMIDE ADDED,
          Figure 4.   Trihalomethanes formed by reaction of humic acid
                     with aqueous chlorine in the presence of varying bro-
                     mide ion concentrations using a chlorine dose of 282
                     microequivalents per liter.
14  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
  For example,"in the experiment where  12 nmol bromide/L were added to the
solution containing the humic acid and 282 ^equivalents chlorine/ L, the oxidant
ratio, Ch/ Brz was 23, but the reacted Cl/ Br ratio in the trihalomethanes formed was
only 0.42 (Figure 4A), Thus, bromine competes more effectively than chlorine for
active sites on the humic acid precursor molecule, perhaps mechanistically by way of
a faster substitution reaction rate. A probable example of this effect occurred in a
coastal city,  Brownsville, TX,  that  had  a finished water  with  the  following
concentrations of trihalomethanes: chloroform, 12 Mg/L; bromodichloromethane,
37 jug/L; dibromochloromethane, 100 /ig/L; and bromoform, 92 (ig/L.J
  Additionally, the total molar yield of trihalomethanes appears to increase with
increasing bromine substitution. Without any added bromide, 0.8 fj.mol TTHM/L
was formed, but when 313 pmol of bromide/ L was added to the solution, the TTH M
yield  was 1.25 /itnol/L,  Figure  4B.  This  was  also observed when  pure aqueous
bromide was  reacted with the humic acid under the same conditions as aqueous
chlorine.  Reactions in these experiments were allowed to proceed over a period of
many days  until detectable changes in trihalomethane concentrations were small.
Nevertheless, the apparent higher "yields" obtained with, bromination may be only a
kinetic effect of faster formation of brominated species. This, interpretation is
supported by a qualitative observation that the favored bromine-containing species
formation was  more pronounced in the early  stages  of reaction. Although few
utilities may experience this kind of problem, either cause of high trihalomethane
concentrations will create a larger TTHM  problem for utilities that experience the
presence of bromide. For example, increases in TTHM concentrations during the
time of treatment have been reported at a water treatment plant in Contra Costa,
CA, where sea water intrusion was temporarily responsible for increases in bromide
(Figure S).20
Effect of pH

  Numerous workers have shown that increasing the pH of the water being treated
dramatically  influences rates  of formation  of  trihalomethanes  during water
treatment. Figure 6 presents one example. Given sufficient time, however, the yields
for the two pH systems may be similar. Note that the two lines in Figure 6 are still
approaching each other after 70 hours. The increase of trihalomethane formation
rate with pH was expected, because the classic haloform reaction is base catalyzed;
however, this explanation is likely to be an oversimplification where rather complex
humic acid structures are involved. Simple methyl ketones, models for the haloform
reaction, have been shown to react too slowly  to account for trihalomethane
formation under most drinking water treatment conditions.
  Figure 7 shows the results of attempts to react chlorine at pH 7 with simple acetyl
compounds (acetone, acetaldehyde, and acetophenone) when these'compounds were
spiked at 5 fimol/ L into raw and granular activated carbon (GAC) treated water.
Under these circumstances, trihalomethanes were not produced at rates significantly
higher than those for the blank samples. Figure 8, however, shows that at higher pH
values, the simplest methyl ketone, acetone, reacts at a much higher rate, and this
class of compounds could become a significant source of precursor in  those pH
ranges. The complex humic structure, therefore, must have more active groups than
the simple methyl ketones for chlorine substitution to account for reactivity at pH 7,
with the possibility of less active acetyl groups becoming more significant at higher
pH, increasing reaction rate and possibly yield.
  An alternative explanation for the effect of pH on rate and yield with humic acid
precursor has been suggested by Christman, however (R.F. Christman, Univ. North
Carolina, Chapel Hill,  1977, personal communication). The macromolecule may
simply be "opening up " by mutual repulsion of the negative charges at high pH, thus
increasing the availability of additional reactive sites on the molecule.

                                      Section III. Mechanism of Formation  15

-------
        200
        180
         160
        140
         120
      o>
      o
      o
      o
      5
      I
100
             * TTHM
             O CHCI,
             A CHCIBr,
             D CHCI,Br
             • CHBr,
         40
         20
                       50        100       150        200        250

                     SOURCE WATER CHLORIDE CONG, mg/L

         Figure 5. Effect of salt water intrusion on THM formation poten-
                  tial.20 (Adapted from JOURNAL American Water Works
                  Association, Volume 70, No. 11 [November 1978] by
                  permission. Copyright  1978, the American Water
                  Works Association.)
Effect of Characteristics and Concentration of Precursors

  Increasing the concentration of humic acid precursor in the presence of excess
chlorine with otherwise constant reaction conditions caused trihalomethane yields
to increase in direct proportion to the humic acid dose (Figure 9), At similar NPOC
concentrations, humic acids and natural water have been shown to result in similar
trihalomethane yields (Figure  10,  page 19). When different source waters are com-
pared, however (see Section II, Surrogate Measurements) only crude relationships
have been found between organic carbon concentrations and trihalomethane yields.
16  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
120
           10
                   20     30     40      50

                         REACTION TIME, hr
                                                        70
                                           80
   Figure 6.   Effect of pH on chloroform production, settled water,
              25°C (77°F), 10 mg/L chlorine dose.16
         200
         180 - -


         160 --


      _, 140 - -
      x
      O!
      a. 120 - -
• Acetone
O Acciaiaehydo
• Aeetophenone
O Blank
                                       50   60    70   80
                          REACTION TIME, hr

   Figure 7,   Raw and GAC filtered water spiked at 5 /imol/Lwith
              low molecular weight acetyl compounds. pH 7.0; 10
              mg/L chlorine dose.15
                                 Section Hf. Mechanism of Formation  17

-------
       08--
                 10    20
                             30   40    50   60    70

                               REACTION TIME, hr
                                                              90    100
         Figure 8.  Effect of pH on trihatomethane production from ace-
                   tone. 1 mg/L; 25°C (77°F); 10 mg/L chlorine dose.18
       0.3  - -
         0 C
                 10    20    30   40    50    60   70    80    90  100

                               REACTION TIME, hr
         Figure 9.  Effect of humic acid concentration on trihalomethane
                   production. pH 6.7; 25°C (77°F); 10  mg/L chlorine
                   dose.16

18  Treatment Techniques for Controlling Trihatometbanes in Drinking Water

-------
               180

               160 --


               140 --
            X 120 -h
            O 100 - -
I      1     I     1      r
                            Humic Aetd B mg/L,
                      NPQC Appro*. 3 mg/L, [
                                   rce Water NPOC 3 mg/L, pH 6,8-6,9
                    0   10   20    30   40   50   60    70   80
                                REACTION TIME, hr

         Figure 1O.   Comparison of humic acid, source water reaction
                     rates  at similar  NPOC concentrations. 10 mg/L
                     chlorine dose,18
  Further, rate curves take on distinctly different shapes depending on the source of
precursor substances. The work of Rook21 shows the reaction of-fulvic acid solutions
to be characteristic of m-dihydroxyphenyl moieties, e.g., resorcinol, as that reaction
is nearly complete at near neutral pH in less than 2 hours (Figure 11). Quite a
different characteristic curve is observed with Ohio River water precursor and a
different source of humic acid (Figure 10), however, where the reaction takes place
relatively slowly over a period of many days.
     o
     X
     o
     |20tr>4-
     gl5Q-t
     CC

     " 100
     o
yy
I 1 1 1 1 '' 1 \
~ Resorcinol ~
. 	 	 	 	 J* 	 »
- /^ • J
o
E
'o
-40 |
• z"
— 30 'aj
cc
                  10     20   30     40     50    110   120   130
                            REACTION TIME, hr
        Figure 11. Reaction  of  model   precursors  with  aqueous
                   chlorine.1*
                                       Section HI. Mechanism of Formation   IS

-------
  The probable differences in precursors at different locations have been further
demonstrated. As  expected  on a theoretical  basis,  treatment of resorcinol and
m-dihydroxybenzoic acid solutions with potassium permanganate at low dosages
was nearly 100 percent effective in preventing the formation of trihalomethanes
upon  chlorination of these  substances, yet potassium permanganate was only
marginally (10% to 20%) effective in reducing the ability of Ohio River precursors to
form trihalomethanes upon subsequent chlorination. (This work is discussed more
completely on pages 129 to 135.)
  Research by Christman and his team22 is attempting to understand the structure of
aquatic humic and fulvic acids and their roles in the trihalomethane reaction. To
date,  scores of substructure moieties have been identified through  the use  of
controlled oxidative and hydrolytic degradation procedures coupled with sophisti-
cated GC/ MS identification techniques. Representative models selected from these
have been reacted with aqueous free chlorine to show that trihalomethanes, as well as
other chlorinated byproducts, may be formed by a number of different pathways and
at vastly different rates.
  The above serves to indicate that although precursor materials from various water
sources may be of largely natural origin, the composition of that material is likely to
be different depending on the type of source water involved and the  origin of
precursors  in  the watershed. Considerably more work is needed, therefore,  to
understand precisely the complex mechanisms of trihalomethane formation during
drinking water chlorination.

Effect of Chlorine  Dose and Type

  Where precursor is kept constant, only a slight influence on trihalomethane for-
mation  rate or yield occurs  when the free chlorine dose is increased  beyond the
demand (Figure  12). Additionally, work by Kajinoand Yagi (Figure 13) showed that
once chlorine demand was satisfied, increasing chlorine residual concentrations had
little influence on chloroform yield in the 8-hr reaction time.23 Both similar20'24'25 and
contrary"127 results have been reported while conducting tests with different sources
of precursor. Combined chlorine (chloramines) does not  cause the formation of
trihalomethanes  (Figure 14).
                 10
                      20
80   90   100
                           30   40   50   60    70
                             REACTION TIME,  hr
          Figure 12.   Effectof chlorinedoseon trihalomethaneformation.
                      pH 7.0; 25°C (77°F).1S

20  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                450
     en
         4 - -
         3 ~ ™
     DC
     3

     §   a
     <
     9
     ui
     cc
                                 CHLORINE DOSE, mg/L

         Figure 13.  Chloroform   formation  compared  with  chlorine
                    residual.23

  Because of the possible significance of free chlorine concentration under some
circumstances and the importance of precursor concentration discussed above, the
manner in which the chlorine is added to the water (initial mixing and reactor design)
is likely to impact the rate of formation  of trihalomethanes and therefore their
concentrations after treatment.
  All of the factors discussed here influence the concentration of trihalomethanes
each consumer in a given utility's distribution system will receive. As  mentioned
above, all must be understood if the success of a proposed treatment change at a
given utility is to be properly evaluated. Section IV will show how these factors are
applied during any treatment evaluation.
                                       Sect/on III. Mechanism of Formation 21

-------
            10 --
               0     10    20    30    40    50    60   70
                              REACTION TIME, hr


        Figure 14.   Chloroform formationbyfreeandcombinedchlorine
                    residual,16
22  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                                SECTION IV
         MEASUREMENT FOR TREATMENT EVALUATION

Definitions

  To understand the measurements  that  must be  made  to  evaluate  treatment
success,  four definitions are important,
  I. Instantaneous trihalomethane (InstTHM) concentration — The concentration
of trihalomethanes in the water at the moment of sampling. This may be expressed in
terms of the individual species or their sum as total trihalomethanes (TTH M). This is
the parameter measured in the distribution system to provide the data  needed to
judge compliance with the Trihalomethane Regulation.*
  2, Terminal trihalomethane (TermTHM) concentration* — The concentration of
trihalomethanes that occurs at the  termination of the measurement of this para-
meter. To  measure  TermTHM  concentration, the chlorine-precursor reaction
conditions are selected according to the treatment practiced at  the particular water
plant being evaluated.  In  general, a sample of water is chlorinated under these
conditions, and chloroform and the other trihalomethane species are measured after
a specified time period, as explained below.
  TermTHM concentration is equally important  as a  parameter for evaluating
consumer risk as is the InstTHM concentration. Because this parameter is a measure
of the sum of the amounts of trihalomethanes already present (instantaneous) and
those formed during the reaction time, a third parameter, useful for evaluating unit
process  performance for  removal  of unreacted  precursor, must be defined
(Definition 3, below).
  3. Trihalomethane formation potential (THMFP) — Calculated as the increase in
trihalomethane concentration that occurs during the storage period in  the deter-
mination of the TermTHM concentration. The THMFP is obtained by subtracting
the InstTHM concentration from the TermTHM concentration, either when total
trihalomethanes or when the individual species data are used. THM FP is a measure
of the portion of the total precursor material (see Definition 4 below) that is in the
water at  a given point in the treatment train and, therefore, is of most concern to the
water utility operator. This parameter, when computed on unit process influent and
effluent samples, can be used to determine the efficiency of the process being used to
remove the pertinent fraction of precursor  material.
  4. Total precursor — The concentration of all trihalomethane precursor materials
present in  the water  that could react  with  halogen species under conditions that
maximize the yield of trihalomethanes.  A distinction between THMFP and total
precursor is important.  No standardized procedure for measuring this  parameter
exists, however, and considerable  research would  be  required to  establish  the
optimum conditions to ensure the complete reaction of all precursors to yield the
theoretical maximum trihalomethane concentrations.
  Because  the  chlorination conditions   for  the  TermTHM   concentration
measurement are somewhat less than  optimum  for trihalomethane formation, the
 "TerrflTHM is not to be confused with the Maximum Total Trihaiomethane Potential (MTP) mentioned in the Trihalo-
 methane Regulation' and in Section I. Summary of Regulation. They are different parameters. The goal of MTP is
 to define the upper limit of the possible total trihalomethane concentration in certain water utilities treating groundwater.
 MTP is not a quantitative index of trihalomethane precursor concentrations as is the TermTHM parameter. Also.
 TermTHM should not be confused with other proposed techniques designed to hasten the reaction between chlorine and
 precursor by heating and pH elevation or with "Total Potential Haioforms," measured by a direct aqueous sample injection
 technique,  that are likely to give unrealistic estimates of pertinent precursor concentrations.'2


                           Section IV. Measurement for Treatment Evaluation  23

-------
TermTHM concentration obtained in any test will be somewhat less than the theo-
retical maximum trihalomethane  concentration. Thus, the value obtained for'
THMFP under these conditions will  be smaller than the theoretical "total pre-
cursor" parameter. Although the value obtained, THMFP, is not the "total pre-
cursor" concentration, as noted above, it is an index  of the concentration of
materials of most concern relative to trihalomethane formation at a particular water
treatment plant and in that distribution system. To compare treatment results from
utility to utility nationwide or within a utility where reaction conditions caused by
differing treatment conditions  exist,  selection  of  a  single set of standard  test
conditions may seem desirable. This potential comparability, however, is  less
desirable than the direct evaluation of precursor removal within the utility under
study where that utility is evaluating its own capabilities to meet the trihalomethane
MCL. The TermTHM and THMFP test conditions are  intentionally left flexible
here to encourage the individual utility to select conditions for the test to reflect their
individually most promising treatment options. Although this test approach makes
inter-utility comparisons of treatments very difficult, the approach makes treatment
evaluation measurements better predictors of eventual success at that utility. The
option exists, of course, in any collection of research efforts to conduct the precursor
test under any one or a multiple of several sets of conditions to allow for direct
comparisons  of precursor removal results  within one or between any number of
utilities conducting similar treatment experiments. Figure 15  graphically presents
the parameters discussed.






o
z
o
o
5
X






\f$$K\ Remainder ,
^*^^3 of Total
^ — Precursor— »*

















Appro, it) •
motion of
Cone, in
Distribution
System
at a Given
Point
Cone,
at Time
of
Sampling
"•**-






%M%>.
^m,








%


'''tyfyl
(Lilllo
Consequence) <








Insi.
THM
Cone,



1












THM
Formation
Potential
(B-A)
Omporlaot
Portion of
TotaJ
Precursoff

i





Total
Precursor






Terminal
THM conc.
ISample
Stored Appropriately
with Freo
Chlonne
Roaidual)










Theoretical
Maximum
THM
Cone.






                               A  B

              Figure 1B.   Trihalomethane measurement parameters.
Measurement of Instantaneous THM Concentrations

  For an InstTHM concentration  measurement, the reaction  of chlorine with
precursor materials must be halted at the time of sampling with the goal being to
measure only  trihalomethanes present at that time.  A small amount of reducing
agent, sodium sulfite or sodium thiosulfate, is added to the sample to react with the
 24  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
chlorine and, thus, render the chlorine unavailable for oxidation or substitution
reactions. This technique is used in the samples required for compliance with the Tri-
halomethane Regulation.3
  A small increase in trihalomethane concentrations upon storage after addition of
the reducing agent usually is observed, even when the mixing of the reducing agent
is  nearly instantaneous. This is probably caused by a  slow hydrolysis  of certain
trihalo-intermediates; the hydrolysis step does not require the presence of chlorine.
The distinction  should be made  between  this  minor effect on the  InstTHM
concentration and the continued  trihalomethane formation  reaction when no
reducing agent  is added  (discussed  below).  The  increase  in  trihalomethane
concentration during storage after a reducing agent has been added  is only a few
percent of the total value.

Measurement of Terminal THM Concentration and Calculation
of THM Formation Potential

  These  two parameters  are  discussed  together because  the measurement  of
InstTHM concentration is subtracted from the TermTHM concentration to yield
the THMFP. To determine the TermTHM concentration, chlorine is reacted  with
trihalomethane precursors in a given sample in the dark  under certain  controlled
conditions that affect yield and rate of formation of the  trihalomethanes (discussed
in Section III); the concentrations of the trihalomethane species produced are then
measured. The conditions for this measurement are based on the conditions at the
treatment plant  under  study and must be reproducible  from sample to sample.
"Precursor" is a  mixture of organic chemicals, and the  conditions chosen for  their
measurement will influence which fraction of the mixture is measured. Therefore, if
any comparisons between samples are to be made, the measurement conditions must
be the same,  or a second variable,  measuring a changing fraction of the precursor
mixture, will be introduced into the experiment. Critical factors to be considered are:
time of reaction; maintenance of a free chlorine residual; temperature;  and pH. Each
will be discussed as it relates to the evaluation of a given treatment process at a given
water utility.

Effect of Time—
   Although a single measurement of trihalomethane concentrations aftef a storage
period of several days  in a bottle under appropriate conditions can give a useful
determination of the TermTH M concentration for that specified time, much more
information can be gained  from  the reaction curves obtained  by plotting trihalo-
methane concentration vs. time, i.e., the "rate curve." The rate curves obtained by
periodic measurement of trihalomethane concentrations  in properly stored water
can be used to predict the  trihalomethane concentrations at any given time  after
sampling.
   In any system, the generation of the rate curve is recommended, at least initially, so
that the nature of the reaction that occurs at a given location  can be determined.
Furthermore, if possible, periodic  development of the rate curve is suggested to
determine whether or not changes in precursor type are occurring. Figure 16 shows
two hypothetical curves describing  the rate of chloroform formation  that might be
expected for finished waters of distinctly different qualities after leaving  typical
water treatment  plants.
   Curves "A" and "B" in Figure 16 represent  two extreme situations that might
occur. Although at time "T" the  chloroform concentrations are the  same for two
waters from the  two treatment plants, the short-term chloroform concentration is
greater in "Water A,"  and the long-term chloroform  concentration is greater in
"Water B." A "Water A" type curve would be expected where chloroform formation
'potential is relatively low, but the precursor present is of the type that  reacts quickly
under  the given  conditions, i.e.,  the final concentration of chloroform  is reached

                          Section IV. Measurement for Treatment Evaluation 25

-------
      o
      z
      o
      o
      *•*
      G
                                                          2T
                             REACTION TIME, day
         Figure 16.
Formation of chloroform under widely different treat-
ment plant conditions.
early. A "Water B" type curve would be expected where chloroform formation
potential is high, but the reaction with chlorine is slow because of the nature of
precursor or reaction conditions. Thus, these rate curves are more informative than a
single chloroform determination performed at time "T," and a single measurement
from each plant easily could be misinterpreted to mean that both situations were the
same.
  Good approximations of both curves can be obtained by selecting three or four
points beyond time "0" (instantaneous  value)  such as  "1/2T," "T," "2T" (as
shown) where "2T* is equal to or slightly longer than the maximum distribution
system residence time. With these added analyses, generating rate curves could be
time consuming, especially if conditions are such that reactions are slow and the
distribution system residence time is long. If developing a rate curve is beyond the
capability of  a utility, the time  for storage during the determination of the
TermTHM concentration should be the longest residence time  in the distribution
system, as this represents the most stringent  condition for that  utility.

Maintenance of Free Chlorine Residual—
  In conventional water treatment practice in the United States, maintaining a free
chlorine residual through the distribution system often is recommended or required.
The continued reaction of precursor with chlorine to yield trihalomethanes depends
on the maintenance of a free chlorine residual. Again, with  chloroform as an
example, the raw water curve presented in Figure 17 shows the abrupt cessation of
chloroform production as the free chlorine residual became depleted.  If a water
utility maintained a free chlorine residual throughout the distribution system, the 24-
hr and later chloroform concentrations from this test could be misleading. Thus, to
avoid obtaining misleading results when evaluating systems where free chlorination
is practiced, a  chlorine residual measurement always must be performed at the time
 26  Treatment Techniques lor Controlling Trihalomethanes in Drinking Water

-------
        200
        175
                                   CI, exhausted
                                             Settled Water
                                         60           90            120
                                 REACTION TIME, hr

         Figure 17,   Effect of different treatment on chloroform forma-
                     tion, pH 7,0; 25°C (77°F); 8 mg/L chlorine dose.18

of the TermTHM analysis to ensure that a free chlorine residual is present. If insuffi-
cient free chlorine is in the water at the time of sampling to last through the test,
chlorine must be added before sample storage.
  Work at the  USEPA-DWRD laboratory indicates that TermTHM  concentra-
tions are not influenced significantly by the amount of free chlorine present (Figure
12)  as long as the concentration is above about 0.5 mg/L. This, which was not
demonstrated  with lower free  chlorine  residuals, may  only  be  because the
tri halo methane concentrations usually are limited by the amounts of  precursors
present. Because some uncertainty exists about the effect of chlorine concentrations
on the reaction rate, however,20'23"27 the starting free chlorine concentration used in
the  TermTHM determination should be nearly the same as the chlorine dose added
at the treatment plant and possibly in the distribution system, if that dose is adequate
to supply the required residual for the duration of the test.

Effect of Temperature—
  Because  temperature has a dramatic effect on rate of formation  of trihalo-
methanes (Figures 2 and 3) and therefore on the yield at any given time, a need exists
for  close  temperature control  during the  determination  of  the TermTHM
concentration. At a waterworks,  because  temperature  cannot  be controlled but
varies seasonally, selection of a sample storage temperature will depend on the
experimental objective.  For  example, if the objective is  to estimate consumer
exposure to trihalomethanes  throughout a year, a logical choice is the estimated
average distribution system temperature, and this will vary depending on the time of
                         Section IV. Measurement for Treatment Evaluation  27

-------
the year the sample is collected. When the objective is to evaluate precursor removal
efficiencies of a unit process, the same fraction of the precursor mixture must be
measured during each test; therefore, the temperature must be maintained at a single
value for all of the tests, regardless of the time of the year.

Effect of pH—
  Selecting  the pH  for the controlled reaction during determination of  the
TermTHM concentration is less straightforward  than  that for reaction time and
temperature. The variation of pH through an operating water treatment plant can be
quite wide, and the variation is controlled operationally.
  If the determination of only the TermTHM concentration and the THMFP for the
finished water is desired, pH selection is not a problem; the samples should be stored
at the finished water pH. Selecting pH is more difficult if a comparison is needed
between the TH M FP of the finished water with that of the raw water (or with water
at any stage of treatment) to evaluate the success of a unit process in removing
THMFP.
  The analyst must be sure that the same fraction of the total precursor concentra-
tion,  pH dependent (Figures  6 and 8), is reacting at each point of treatment
evaluation  and  that the  reaction  rate of chlorine with the material, also  pH
dependent (Figure 8), is the same at each point. Thus, all of the samples from each of
the various sampling points must be chlorinated and buffered at a single selected pH
value before storage. Therefore, because the TH MFP test is designed to measure the
portion of the total precursor that is significant in a given water as it leaves a given
treatment plant, the logical single reaction pH value is usually that of the finished
water entering the distribution system, as it  was with the choice of temperature.
Recall that, as with temperature, when the objective is to evaluatep«rursor removal
efficiencies of a unit process, the pH must be maintained at a single value in all tests.
Therefore, the pH naturally occurring  at the point in the treatment train where the
sample was taken should be adjusted and buffered to the selected pH.

Summary of Procedures for InstTHM, TermTHM and THMFP

  Procedures for measurement of these parameters have been discussed in terms of
general concepts. Considerably more detail is given by Stevens and Symons29 and
analytical procedures are similar to those presented in the USEPA method 510.1 for
Maximum  Trihalomethane Potential (MTP). In summary,  InstTHM  is  the
measured trihalomethane concentration when the chlorine-precursor reaction was
stopped  by the addition of a  chemical reducing  agent at the time of sampling.
TermTH M is the measured trihalomethane concentration afterthe reaction between
precursors and free chlorine has been allowed to continue in a sealed container under
specified conditions for a given time period.* THMFP is the arithmetic difference
between TermTHM and InstTH M concentrations and represents the concentration
of precursor that is unreacted, is present in the water at the time of the original
sampling, and is of concern  in a given situation.
  Generation of the trihalomethane formation rate curve,  although  not always
necessary,  provides useful background information for plant  and unit process
evaluations. The rate of formation curve, when generated for finished water samples,
provides a  useful estimate of the trihalomethane concentration for any given time
after the water leaves the treatment plant, an important factor. Section V discusses
how these three parameters are specifically used to evaluate some example treatment
plants.
 *Na*e, if *ny chemicals are added to the sample al the itart of this determination, they must be free of bromide.

 28  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                              SECTION V
   EXAMPLES OF TREATMENT EVALUATION TECHNIQUES

  Two hypothetical examples will help to demonstrate the use of the InstTHM and
TermTHM determinations and the calculated THMFP to estimate both consumer
exposure to trihalomethanes resulting from the chlorination process and the efficien-
cies of various unit processes within the plant for removing precursor compounds
during treatment. The efficiency of unit processes for removing chloroform or other
trihalomethanes  themselves can also be estimated.
  These hypothetical examples should not  be considered to be predictions of the
success or failure of certain unit processes  in a treatment train. The examples do
serve to indicate  the type of results that might be  obtained when a plant is sampled
for the measurement of InstTHM  and TermTHM concentrations and THMFP
concentrations calculated, and should help in understanding how this information is
used for unit processes or whole plant evaluations as detailed in the treatment effec-
tiveness research presented in Sections VI—VIII. For further information the reader
is  directed to Reference 29,  where many other  examples  are given and their
interpretations discussed more  fully.


Simple Chlorination

  The first example represents the simplest case, a water treatment plant with chlo-
rination only. Figure 18 depicts the relative  values for  the parameters that might be
obtained if analyses were conducted for the InstTHM concentration and TermTHM
concentration at  the source, "A," the plant clearwell, "B,"and a theoretical point at
the maximum residence time in  the distribution system, "C." For simplification, the
trihalomethanes  are being discussed here as a group. Each bar could  represent the
single group index total trihalomethanes or any one of the individual species; or it
could be subdivided horizontally into four bars of different heights to represent all
commonly found trihalomethanes.
  According to this bar graph, trihalomethanes were absent in the untreated source
water, i.e., InstTHM was not found upon analysis of the source water, but the full
THMFP  was present and equal to the TermTHM concentration obtained
experimentally. At the clearwell, some of the precursor measured as  THMFP has
reacted to form trihalomethanes (measured  as InstTHM in the finished water) and
has left a smaller remaining THMFP. The remaining  THMFP, plus the InstTHM
concentration, equals the TermTHM concentration determined originally on the
source water. At point "C," the entire source water  THMFP has reacted to give an
InstTHM concentration identical to the TermTHM concentration.
  No unit process at this plant effectively lowered  either TermTHM or InstTHM
concentrations. The practice of chlorination itself converted THMFP to InstTHM,
thereby causing a decline in the THMFP concentration. In assessing the THMFP
removal by any unit process, care must be taken to  treat separately the removal of
THMFP by  conversion  to  InstTHM during chlorination and  the removal of
THMFP by the unit process itself. Only at a  point closer to the treatment plant than
the maximum length  of  the  distribution  system is the consumer exposed to
trihalomethane concentrations (InstTHM) that  are  lower than the TermTHM
concentration shown at point "C" in Figure  18. These two concepts will be discussed
further in the more complex example presented below.

                    Section V. Examples of Treatment Evaluation Techniques  29

-------
     u
     z
     o
     o
     S
                                            InstTHM Concantration

                                      |   i TMM Formation Potential

                                I    1+PH! TwcnTHM Concentration
              Li
          1 SOURCE

4 *
CLEAR-
WELL


END OF DISTRIBUTION
SYSTEM
          Figure 18.   Trihalomethanes formed during water treatment by
                      chlorination only.

Conventional Treatment

Finished Water TermTHM Concentration Reduction—
   During conventional treatment with raw water chiorination (Figure  19) some
trihalomethanes are formed during rapid mixing and throughout the following treat-
ment stages in the presence of free chlorine. Thus, the InstTHM concentration
increases as the  water passes through  rapid mixing, settling, and filtration, i.e.,
points "B," "C," and "D."  Coagulation and settling do remove  THMFP, i.e.,
precursor removal, so that  parameter, as well as the TermTHM concentration
declines from point "B"to "C." Filtration removes more precursor material that is
associated with the carryover floe; therefore, the THMFP concentration declines
slightly again from point "C" to "D," as does the TermTH M concentration. Recall
that some of this TH M FP concentration decline from point "B" to "C" to "D" results
from conversion to InstTHM. (This is discussed more fully in the next subsection.)
The remaining THMFP is converted by the free chlorine to trihalomethanes from
point "D" to "E," and therefore, the InstTHM  concentration determined for a
sample taken at point "E" in distribution system equals the TermTHM concentra-
tion of the sample collected at point "D." Therefore, if the consumer farthest from
the treatment plant is to receive water containing less trihalomethanes, the finished
water TermTHM concentration must be lowered.
   A concept that is important when attempting to evaluate the performance of unit
processes and  treatment schemes using the laboratory test technique relates to the
difference in the behavior of trihalomethane formation in a test bottle as opposed to
behavior in a treatment plant and distribution system. For example, source water
and filtered water may be  stored in test bottles and the TermTHM concentration
determined on each sample, according to the method described earlier in Section IV,
The difference in these two concentrations of TermTHM indicates the removal of
trihalomethane precursors  during treatment. Moving the point of chlorination from
the source water to the filtered  water in the treatment plant will not necessarily,
however, cause the fully equivalent decline in the TermTHM concentration in the
finished water after the change in chlorination  practice at the plant although some
lowering of the TermTH M concentration usually will occur because of precursor
 30  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
    o
    o
                                            InstTHM Concentration

                                      |    | THM Formation Potential
        CHLORINE
      COAGULANT
         Figure 19.   Trihalomethanes formed during conventional treat-
                     ment with source water chlorination.
removal  during  treatment. The  full source  water TermTHM concentration, as
measured in the test bottle, will not be realized in the distribution system, even when
the source water is chlorinated in the treatment plant; compare points "A"and "E"in
Figure 19. This is because the test bottle is a closed system with intimate mixing of
precursor and free chlorine for the duration of the test, and the treatment plant is not.
That is, some precursor is removed "across" the unit process in the treatment plant
before it is able to react with the free chlorine, even when source water chlorination is
practiced. Therefore,  as noted above, InstTHM  and TermTHM measurements
"across"  unit processes give  accurate information about process effectiveness for
trihalomethane and precursor removal, but in  themselves, they do not reflect the
exact degree of trihalomethane control to be expected by movement of the point of
chlorination from one place  to another in the treatment plant.
  Actually moving the point  of chlorination in a treatment plant and measuring the
influence on the TermTH M concentration in the finished water is the best method of
establishing what effect precursor removal before chlorination will have at that site.
Some approximation may still be obtained, however, by conducting some "bottle"
experiments at the plant and interpreting the data according to the example in Figure
20.
  In  this hypothetical case  with chlorination at the rapid  mix during routine
operation (Figure 20), "Amount B"of the source water precursor is removed by sedi-
mentation, "Amount C" is converted to InstTHM during flocculation and settling,
and "Amount A" remains as THMFP after settling. Moving the chlorination point
to the settling basin effluent would allow some portion of "Amount C" precursor to
be settled out ("Amount X" in Figure 20) before it is chlorinated, because, after the
point of chlorination is moved, the reaction of chlorine with this precursor would not
be "competing" with settling for "Amount C." Further, moving the point  of
chlorination is not likely to influence the fraction [B/(A+B)] of unreactedprecursor
(A+B) that was removed, because that fraction  is already being successfully settled
out without reacting with the chlorine that was present during routine operation.
Therefore, the TermTH M concentration would decline only by whatever "Amount
X" of "Amount C" would  be in a given situation.

                    Section V; Examples of Treatment Evaluation Techniques  31

-------
      O

      §
      O
RAPID
MIX


PLOCCU-
LATION
                  CIMCOAOULANT
           Figure 20.
Example of using "bottle" data for predicting per-
formance of settling on precursor removal.
  The decline  in  finished  water TermTHM  concentration cannot  be exactly
predicted  from  the  data collected in the bottles  because the rate at which
trihalomethanes are being formed, the rate at which precursors are being settled, and
the mix of precursors being influenced by each reaction would not be known.
Clearly, the decline will not equal "Amount B" (Figure 20). Some approximations
can be made from bottle experiments, however, because the "fraction" of precursor
converted  to trihalomethanes during passage through the unit process understudy
during routine conditions [C/(C + A) in Figure 20] can be evaluated in laboratory
experiments,  and the magnitude of this  "fraction"  influences  the  potential  for
success.
  For example, the lower this "fraction," the less the chance of success will be for
lowering the finished  water TermTH M concentration by chlorination after the pre-
cursor removal unit process. In that case, free chlorine and precursor are reacting
slowly, so the precursor that is settling is not involved significantly in the trihalo-
methane formation reaction, causing the point of chlorination to be  of little
importance. Of course, the opposite is also true. In situations where a high "fraction"
of precursor is converted to InstTHM during passage through a unit process when
free chlorine is present, the chance of success for improving precursor removal by
delaying chlorination until later in the treatment train is higher, as more precursor
material could be precipitated if the rapid conversion to InstTHM were prevented
from "competing" with the settling process.
  Another factor that must be considered in judging the potential for success of any
plan to lower finished water TermTHM concentrations (by enhancing precursor
removal through moving the point of chlorination) is the degree of precursor
removal in the unit process  under study. If in  the example  shown  in Figure  20,
"Amount B" were a small percentage of the unit process influent, "Amount A + B +
C," then the chance for success in lowering the finished water TermTH M by moving
the chlorine point downstream would be small, no.matter what the magnitude of the
C/(Of A) fraction.
  The same concepts may be applied even when some InstTHM is present in  the
influent to the unit process under study. In this case, "Amount C" would be  the
 32  Treatment Techniques for Controlling Trihalomethanas in Drinking Water

-------
increase in InstTHM concentration "across" the  unit process under study. The
remainder of the analysis would be carried out as outlined above.
  As mentioned previously, the concentration of THMFP can be lowered in two
ways: either TermTH M concentrations can be lowered because of precursor removal
or precursor can be converted to  InstTHM. Hypothetically, in Figure 21 for
example, when the  chlorination point  was moved from the source water to the
settling basin effluent, more THMFP was present in the clearwell after the move
than before, even though the TermTH M concentration declined a little. This results
from the decline in InstTHM concentration that occurs because of the shorter tri-
halomethane formation reaction time before the clearwell—a shorter time caused by
the change in chlorination practice. Further, under routine operation (source water
chlorination), a large decline in THMFP concentration occurred from the settling
basin effluent to the  clearwell because of the increase in InstTHM concentration,
even though  the TermTH M concentration only declined  slightly. Care  must be
taken,  therefore, when interpreting THMFP concentration data.
      u
      §
      u
                        $%% InstTHM

                        |   [ THMFP

                       +i^l T«">iTHM
RAPID
MIX

'
FLOCCU-
IATION
    Routine

    Modified
   t
CHLORINE
         Figure 21;  Deelinfe of InstTHM and TermTHM concentrations
                     with change of pojnt of chlorination.
Finished Water InstTHM Concentration Reduction—
  The previous subsection 'detailed  methods of  anticipating finished  water
TermTHM concentration declines during treatment alternatives because this will
reduce InstTH M concentrations at the extremities of the distribution system. Some
success may, however, accrue from  a treatment modification even if the finished
water TermTHM concentration does not decline much.
  In the example in Figure 21, the finished water TermTHM concentration did not
decline much after the point of chlorination was moved, but, because of the delay in
chlorination, the finished'water InstTHM concentration was reduced by "Amount
E" (Figure 21), Therefore, although  the total trihalomethane concentration at the
end of the distribution system was not lowered significantly, many consumers nearer
                     Section V. Examples of Treatment Evaluation Techniques  33

-------
the treatment plant might receive substantially lower total trihalomethane concen-
trations in their drinking water because of the change in treatment practice. This
benefit should not be overlooked.
  The development of a trihalomethane formation rate curve will help quantify
these benefits. Recall that, according to the Trihalomethane Regulation,3 as much as
75 percent of the compliance samples are to be collected from the central part of the
distribution system where this benefit would occur.

Other Considerations

  During such evaluations, the TermTHM concentration of the source watershould
be monitored as a control to ensure  that any change in finished water TermTHM
concentration is not caused by a  change in the characteristics of the source water.
Table 2 shows how the trihalomethane precursor concentrations changed during a
12-month period  in the Ohio  River at Cincinnati. The change in the bromine-
containing trihalomethane species concentrations indicated a change in the bromide
content of the river, as well as  the change in total trihalomethane concentrations.
Note, although the samples were not buffered, the changes in  pH over the study
period were not great and therefore did not influence the data  excessively.
     TABLE 2. INFLUENCE OF SEASON ON TRIHALOMETHANE
     FORMATION POTENTIAL* IN THE OHIO RIVER. 1977-1978
Month
July
August
September
October
Novamber
December
January
February
March
April
May
June
July
Max.
Min.
Spread
Number
of samples
2
4
4
5
3
3
2
3
4
5
4
4
4



Geometric mean (Gm)
Trihalomethanes, jtg/L
CHCI,
153
120
108
120
106
144
103
89
147
115
109
92
109
153
89
64
CHBrCI,
41
43
44
33
30
29
23
27
17
21
32
35
47
47
17
30
CHBr2CI
6.5
8.3
9.3
5.5
7.3
5.6
8.0
8.8
1.6
2.3
5.2
5.0
13
13
1.6
11.4
CHBr,
NFf
<0.1
0.1
<0.1
<0.1
NF
0.2
0.1
NF
NF
NF
0.1
1.1
1.1
NF
1.1
Gm
TTHM.
M9/L
200
171
161
158
143
179
134
125
166
138
147
132
171
200
125
75
•3 d«v« itor*gi; Z5°C J77°F); timptei not buffered. pH range 6.9 to 7.0.
f Nona found.
  Further, the possibility exists that precursor concentration may change in the dis-
tribution system because debris on the pipe walls might act as precursor.  If this is
occurring, the TermTHM concentration measured in the finished water would be
lower than the InstTHM concentration measured at the corresponding point in the
distribution system. In the five places where this has been investigated, however,
good agreement was obtained between these two parameters (References 30 and 31
and the unpublished  1976 National Organics Monitoring Survey).

34  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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  Finally, investigators planning to conduct the type of studies outlined above must
be aware of the need to repeat sampling frequently enough to overcome the inherent
problems of variability in the trihalomethane analytic results. To be able to assess
accurately changes in treatment performance, multiple samples may be needed to
provide a data base large enough to make the observed concentrations statistically
significant. Variability also occurs from trial to trial, necessitating several repeals of
the experiment to ensure confidence in the findings.
                     Section V. Examples of Treatment Evaluation Techniques  35

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                              SECTION VI
TREATMENT TECHNIQUES TO REMOVE TRIHALOMETHANES
                               (InstTHM)

Background

   The proposed10  and the promulgated Tnhalomethane Regulation3 contain a
 Maximum Contaminant .Level (MCL) for the total trihalomethane concentration;
 the decision as to what treatment strategy is best to meet the MCL in a given location
 is left up to the individual utility, with approval of the Primacy Agency,
   Because the general reaction of free chlorine with precursors to form trihalometh-
 anes is:

   PRFF          PRECURSORS                                  OTHFR
rui HRINP + (HUMIC SUBSTANCES) - TRIHALOMETHANES + BvpnnniirT<;
CHLORINE      AND BROMiDE                               BYPRODUCTS

 three treatment approaches are possible. These are:

   1)  treatment to remove trihalomethanes (InstTHM) after formation
   2)  treatment to remove trihalomethane precursors (THMFP), and
   3)  the use of disinfectants other than free chlorine.

 Each of these techniques has been discussed in the literature;""3* in Sections VI, VII,
 and VIII, the research information for each of these approaches will be updated with:

   •  controlled experiments, both by USEPA's Drinking Water Research Division
      and by others reporting in the open literature;
   •  case histories, where available; and
   •  the advantages and disadvantages.

   Note, although the Trihalomethane Regulation3 establishes an MCL for total
 trihalomethanes, for many of the treatment techniques studied, the four common
 trihalomethane species behave differently. Therefore, where the data are available,
 the performance of the unit processes for the removal of the individual species during
 the experiment, as well as  the removal of the arithmetic sum of their concentrations,
 total trihalomethanes (TTHM) will be reported.

 Oxidation

General Considerations—
   The possibility of removing trihalomethanes by oxidation, using either ozone or
 chlorine dioxide as the oxidant, was investigated by USEPA-DWRD in-house. An
 attempt was made to stimulate the oxidation of trihalomethanes during ozonation
 by adding ultra-violet light energy.

Experimental Results—
   Ozone—For these studies, a 3.7-cm (1.5-in) diameter glass counterflow ozone
 contactor was fabricated.  Ozone (Oi) was generated by a Welsbach Model T-408®
 generator using "aviator's breathing" grade oxygen. The ozone-oxygen gas mixture

 36  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
was dispersed through a fritted glass sparger in the bottom of the contactor. Applied
ozone concentrations were determined by an iodometric method.1* In an effort to
maximize contact between the ozone-oxygen mixture and the water, a small, high-
speed, propeller mixer was positioned just below the water surface within the
column. The propeller caused almost complete dispersion of the rising bubbles. Even
at an applied ozone dose of 25 mg/L (5- to 6-minute contact time) attempts to
remove trihalomethanes from Cincinnati tap water were unsuccessful (Table 3).

 TABLE 3. OXIDATION  OF TRIHALOMETHANES, CINCINNATI TAP
      WATER OZONATION. (Gas to water ratio 0.5 to 1 [V/V]
                     5- to 6-minute contact time.)

Sample
Tap water
Mixer only
Applied O,*
dose (mg/L)
0
0
Oxygen only 0
Air only
Ozone only
Mixer + O2
Mixer + air
Mixer + O,
•Applied don.

0
25
0
O
26
Trihalomethanes (M8/W
CHCI3
10
11
12
12
11
11
12
11
CHBrCI2
9
10
10
8
10
9
8
9
CHBr.CI
6
7
7
4
7
6
6
6
CHBr,
1
1
1
0.8
0.9
0.5
1
O.9
TTHM
(rti/U
26
29
30
25
29
27
27
27
continuous flow studias. mg/L =
mgO,
standard liter of am* (O, * O,)
standard liter gas

minute
(0, * 0,1



minute
iitarm of water
  Chlorine Dioxide—This study examined chlorine dioxide (ClOj) prepared by
reacting technical grade (80 percent pure) sodium chlorite (NaClOj) with sulfuric
acid, air-stripping the chlorine dioxide  from solution, and  trapping the gas in
nitrogen-purged distilled water. Analyses for chlorine and chlorine dioxide were
made using a DPD procedure.31 At dosages up to 10 mg/L and storage for 2 days,
chlorine dioxide, like ozone, was ineffective in removing the trihalomethanes already
present in the water (Table 4).

    TABLE 4, OXIDATION OF TRIHALOMETHANES. CINCINNATI
          TAP WATER, CHLORINE DIOXIDE TREATMENT39
            (Temperature  = 2B°C [77°F]; pH = 7.4-7.5)
CIO, dose
(mg/L)
0
7
7
0
10
Contact time
(hours)
0
24
49
0
42
Trihalomethanes (^g/L)
CHCi3
26
26
24
40
39
CHBrCI3
15
18
16
22
22
CHBr,CI
10
14
11
13
17
CHBr,
1.1
NF*
NF
NF
NF
TTHM
(Mfl/L)
52
58
51
75
78
•Nona found.

  Ozone I Ultra- Violet Radiation—Glaze et al. studied the use of ozone in combina-
tion with ultra-violet  radiation (Oj/UV) as a treatment process for removing
micropollutants from drinking water.40 Table 5 summarizes the results obtained for
the disappearance of chloroform and bromodichloromethane using a laboratory-
scale, sparged, stirred-tank, semi-batch, photochemical reactor.

              Section VI. Treatment Techniques to Remove Trihalomethanas  37

-------
    TABLE 6. HALF LIVES* FOR CHLOROFORM AND BROMODI-
     CHLOROMETHANE40 (Ozone dose rates = 0.775 mg/L mint,
                     UV intensity = 0.20 Watts/Lf)
Compound
CHCi,

CHBrCI,

Matrix
pwt
LLWs
PW
LLW
Purging
462
729
495
2660
Ozonolysis
NMD**
22,400
NMD
NMD
Photolysis
139
753
61.9
116
Ozone/UV
3.25
86.6
6.3
S3.3
 •MInutts.
 tMidranga of tho axparfmantaNy invattigatod values.        •                ...
 JSpaelaHy prepared laboratory water low in organic carbon concentration and ozone demand (pH 6.5 to 7.0).
 **No mea*urab!a dactina.
 {Natural waur from local lake (pH 8.1).


  The first order reaction rates are expressed in terms of half-life, that is, the time
required under the reaction conditions given for any concentration of contaminant
to be lowered to one-half of its initial value. Ozone alone had little or no influence on
the two trihalomethanes tested; further, ultraviolet radiation alone (photolysis) de-
stroyed chloroform and bromodichloromethane very slowly, half lives of 61.9 to 753
minutes. Incomparison, the combination treatment was much more effective, lower-
ing the concentrations of these two trihalomethanes to one-half of their initial values
in 3.25 to 6.3 minutes for the specially prepared water in the laboratory and 53.3 to
86.6 minutes in the lake water.

Discussion—
  Of these three oxidation techniques, the combination of ozone and ultra-violet
radiation  was the only  one that  showed any  promise  for  the removal  of
trihalomethanes that have already been formed. This approach is considered to be
still in  the  research stage, however, and  is not ready in a practical treatment
application.

Aeration

General Considerations—
  Among the several factors influencing  the effectiveness  of removing organic
compounds from water by  aeration  are contact  time,  ratio of air to water,
temperature, vapor pressure, and solubility of the contaminant(s). Although
contactor design will  be seen later to be very critical to unit process efficiency and
cost, the last two variables can be useful for estimating the feasibility of aeration. For
example, Henry's law states that when dissolved, the partial pressure of a compound
over a  solution varies directly with its  concentration in the liquid  phase. The
concentration of the contaminant in the gas phase, therefore, is proportional to its
concentration in the  liquid phase. Henry's law constant, sometimes called the
partition coefficient,  can  be  calculated from  experimental data  by dividing the
concentration of the  contaminant in the air by its concentration in water at
equilibrium. This constant can be estimated from the special case conditions where
the concentration of the contaminant is at saturation in both the  liquid and vapor
phase, causing the partial pressure of the  contaminant to be equal to the  vapor
pressure of the pure material.41*42 Thus, Henry's law constant, H, becomes:

                                   H oc J|                            [Eq. 1]

where:   P» = vapor pressure of the pure liquid and                  .   •
        S = solubility of the contaminant in water.

38  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
Thus, lower compound solubility and higher vapor pressure (volatility) result in a
higher Henry's law constant. By conversion of partial pressure units to concentration
in the gas phase, a dimensionless Henry's law constant:
where:  C« = concentration of the compound in air in fig/ L and
       C« = concentration of the compound in water in £tg/L

can be calculated.
  The following analysis  will show how aeration theory can be applied to the
analysis of operating aeration systems; the experimental data in the next subsection
will be analyzed by these techniques.
  Theoretically, a  counterflow aeration tower is  the most efficient system  with
regard to air use to achieve a given treatment goal.  Therefore, the performance of a
theoretically perfect "ideal" tower will be discussed to form a basis for comparison of
actual experimental treatment results given later.
  In  theory,  when a  counterflow  aeration  tower  is  operated ideally,  the
concentration in the water of the contaminant to be removed is in equilibrium with
the concentration of the contaminant in the air at any point in the system. Further,
according to Equation 2, the concentration in the water is equal to the concentration
in the air divided by the Henry 'slaw constant, at any point in the aerator. Because the
concentration of the contaminant in the air coming into the bottom of the system is
zero, in a "perfect" tower the concent ration of the contaminant in the water must also
be zero, to satisfy the definition of an ideal column being' at equilibrium at every
point. Thus, the perfect system would remove all of the  contaminant in question.
  The operation of a  counterflow aeration column or tower can  be  portrayed
graphically by plotting the concentrations of the contaminant in the air and water at
any series of points through the depth of the column.
                     WATER IN "V 	_	-^f    AIR OUT
                                                  Y,
WATER OUT
                                           COLUMN
                                                AIR IN
         Figure 22. Schematic of ideal counterflow aeration system.
                    x, = initial concentration of the contaminant in tha
                        water
                    Xj = final concentration of the contaminant in the
                        water
                    y, = final concentration of the contaminant in the air
                    yz = initial concentration of the contaminant in the air

Calculating a mass balance based on Figure 22, loss of contaminant in water equals
gain of contaminant in the air, yields:

                         (x, - X!) W» = (y,  - y2) A,                    [Eq. 3]
where:  Wv'= water volume
       A. =  air volume.

  In the perfect column that is at equilibrium throughout, from Equation 2 at any
point:

                Sect/on VI, Treatment Techniques to Remove Trihalamethanes  39

-------
                                  -•£-"                          [Eq-4]

  Therefore at the top of the column yj = (H)(xi).

  Substituting this in  Equation 3 yields:

                      (x, - x,) W, = [(H)(x,) - yd A.                 [Eq. 5]

   Because both Xz and yi are zero in the ideal system, Equation 5 becomes

                            (x,) W» = (H) (x,) A,                      [Eq. 6]

  Cancelling yields:

                           |^=Hor^=l/H                       [Eq. 7]

  This means that in the perfect system, the minimum air to water ratio that will
achieve complete removal for the contaminant in question is the reciprocal of its
Henry's law constant.
  Henry's law constants have recently been estimated for low concentrations to
be 0.152 for chloroform, 0.095 for  bromodichloromethane, 0.035  for dibromo-
chloromethane, and 0.024 for bromoform (Werner, USEPA, Cincinnati, OH,
personal communication,  1980).  Experience has  shown  that compounds with
Henry's law  constants greater than 0.05  could be removed  relatively easily by
aeration.41 Therefore,  the possibility of trihalomethane treatment by aeration was
considered. This concept was supported by a 1975 study41 that showed chloroform
lost to the atmosphere  when water was held in open vessels and by a 1976 report44 of
chloroform  being dissipated from a flowing stream  that had accidentally been
contaminated by a chloroform spill.
  As noted previously, in an ideal counterflow tower, the minimum air to water ratio
that will produce complete removal of a given contaminant is the reciprocal of the
Henry's law constant for that contaminant. More air would be wasteful (it would not
be at equilibrium with the liquid  phase), and less air would not achieve complete
removal.
  The Henry's law constants noted above for the four trihalomethanes were used to
construct  an equilibrium diagram (Figure  23).  These data show the  equilibrium
concentration in air for a given concentration in water for the four trihalomethanes.
The slope of these curves (H), proportional to the ease with which the contaminant
can be removed by aeration in a countercurrent system, indicates that  bromoform
would be the most difficult of the four trihalomethanes to remove by aeration.
  Graphically from the curves (Figure 23) or by calculation from H (as above), the
theoretical minimum air to water ratios required to achieve complete removal in a
perfect  tower are  6.7:1,  10.2:1,  28:1,  and  41:1  for chloroform, bromodi-
chloromethane, dibromochloromethane, and bromoform, respectively.
  In graphical form,  the actual performance of an aeration tower is called the
operating line. For the trihalomethanes, the equilibrium lines shown in Figure 23 are
theoretical operating lines for perfect towers operating at the theoretical minimum
air-to-water  ratios  for accomplishing complete  removals  of the respective
compounds. The degree of removal  achieved by lower air-to-water ratios can be
determined as shown in Figure 24.
  Here, as above, for chloroform with a Henry's law  constant of 0.15, an air-to-
water ratio of 6.7 to 1 is needed to achieve complete removal of the contaminant in a
perfect tower. Starting from an arbitrary influent concentration in the water of 100
/eg/ L, lower air-to-water ratios produce the theoretical operating lines as shown,
remembering that equilibrium is always achieved at the top of an ideal column
(concentration in water is 100 jig/ L and on the equilibrium line). Operating lines are
40  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
             20     4O .   60     80    1OO   120    140    160    180


                            THM CONC IN WATER, t
             Figure 23. Equilibrium lines for four trihalomethanes.
o

o
o

O
x
o
             10
                          30     40     50     80     70


                           CHCI, CONC IN WATER, »g/L
        Figure 24.   Examples of the performance of an ideal counter-

                    flow tower at air to water ratios less than the theo-

                    retical minimum for complete removal.
              Section VI. Treatment Techniques to Remove Trihalomethanes  4f

-------
then drawn with the slopes 1/5,1/4,1/2,1/1,5, corresponding to air-to-water ratios
of 5:1, 4:1, 2:1, 1:1, and 0.2:1, respectively. Extending the lines to the x intercept
(concentration of chloroform in air would be zero at the bottom of a counterflow
column) gives the concentration of chloroform remaining in the water for eacK of
these air-to-water  ratios  in an  ideal column for this compound.  From  the
corresponding effluent concentrations, a  plot of percent chloroform  remaining
versus air-to-water ratio will produce a curve for ideal tower operation against which
any field aeration data can be measured. Designs that approach the theoretical
performance should be desirable.  This type of comparison was also suggested by
Singley et al.4S
  Figure 25 is a plot of the theoretical optimum performance curves for each of the
four trihalomethanes at various air-to-water ratios developed by use of the technique
shown in Figure 24, The relative difficulties of removing each of the trihalomethanes
compared with that of chloroform  (the easiest) can be clearly seen by comparing the
theoretical minimum air-to-water ratios required to achieve a given percent removal'
of each compound, as shown in this figure.
        100   *
                              1.0                10
                             AIR/WATER RATIO (V/V)
too
          Figure 25. Performance of ideal caunterflow tower for removal of
                    four trihalomethanes.

  Very importantly, however, no actual aeration system is perfect, so less than 100
percent removal always occurs, even with air-to-water ratios much higher than the
theoretical minimum. This occurs because numerous  design factors influence the
rale of mass transfer from the liquid phase (water) to the gas phase (air). Departure
from  the equilibrium condition  provides  the  driving  force  that  causes  the'
contaminant to move across the air-water interface. This driving force is greater
when conditions are not near equilibrium and becomes  small as equilibrium is

42  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
approached.  Thus, aeration  system design becomes exceedingly important in
facilitating mass transfer if the  low theoretical  minimum air-to-water ratios, to
achieve good removal are to be approached in actual practice. Some important
design parameters to be considered are liquid or gas flow rates, selection of packings
(tower) to optimize surface area, and transfer unit height (contact time).
  Although in application temperature cannot be controlled, it must betaken into
account in both design and perhaps even selection of aeration as a unit process.
Temperature influences not only mass transfer rates, but the magnitude of Henry's
law constant (H) and, therefore, the equilibrium conditions as well. Clearly, freezing
and the entrapment of airborne contaminants (dirt) can also be a problem, especially
in towers.
  Principles for design of efficient aeration systems  have  been developed in the
chemical engineering field. For  example, these principles  have  recently been
synthesized into a design approach for countercurrent aeration towers in drinking
water  applications  by Kavanaugh and Trussel.46 These  actual system design
considerations and procedures are considered  beyond the scope of this Research
Report, however, and will not be treated in depth here.
  A review of the limited available data showing actual removals of trihalomethanes
by aeration follows. These laboratory, pilot, and field performance results will then
be compared with the results of the theoretical optimum treatment developed above.
Batch  reactor experiments will be presented first, followed by continuous-flow
experiments.

Experimental Results—
  Quiescent  Standing—To investigate the volatility of trihalomethanes under
quiescent conditions, an open vessel containing Cincinnati tap water, left standing at
room temperature (about 25°C[77°F]), was sampled periodically for InstTHM. A
nearly complete loss of trihalomethanes occurred after 3 days, even though some
trihalomethanes were being produced during the experiment by the free chlorine
residual (Table 6).                                              '

   TABLE 6. NET*  LOSS OF TRIHALOMETHANES FROM AN OPEN
                   VESSEL, CINCINNATI TAP WATERf
Time of
standing
(hours)
0
6
24
48
72




Trihalomethanes (ng/L)
CHCI,
16
13
7
3
1
CHBrCi2
4
4
3
1
<1
CHBr.CI
4
2
1
<1
NF
CHBr3
2
NFf
NF
NF
NF

TTHM
(^g/t)
26
19
11
4+
1*
Percent
TTHM
removal
—
27
58
83
94
 "Some trihelomethane produced during the experiment by the free chlorine residual.
 tRoom temperature about 26°C (77°f).
 INone found.

  Diffused-Air Aeration—.Using  Louisville, Kentucky,  tap  water, Weil studied
diffused-air aeration in a 500 mL batch reactor.4' By using various air flow rates and
exposure times, he created various air-to-water ratios. Removals of TTHM varied
from  25 to 80 percent depending on the air-to-water ratio (Table 7).
  The Contra Costa County Water  District  has also  investigated diffused-air
aeration for the removal of trihalomethanes in batch reactors.   In the first test,
treated water samples were aerated in a 4-liter stainless steel beaker using a porous
stone diffuser (Kordon Mist A-50I®) with anair flow of 0.5 L/min. Forthe second
test, a 6-cm (2.5-in),diameter glass column 0.9 m (3 ft) long was used for the aeration
studies.  Because  of the  high concentration of bromoform  (which  has  a  lower

                Section  VI. Treatment Techniques to Remove Trihalomethanes  43

-------
  TABLE 7. DIFFUSED-AIR AERATION STUDIES.* LOUISVILLE, KY,
                             TAP WATER47

Air to water
ratio (V/V)
Control
1.25:1
2,6:1
5:1
Control
2.6:1
6:1
10:1
Control
3.76:1
7.6:1
15:1
Control
8:1
10:1
20:1
Aeration
time
(minutes)
0
2.5
5
10
0
2.5
5
10
0
2.5
5
10
0
2.6
5
10




Trihalomothanas (fig/L)
CHCI,
17.3
11,9
11.2
7.9
11.9
7.5
5.8
2.8
24.6
14.1
7.9
3.4
10.5
6.2
6.1
3.6
CHBrCI2
12.3
9.5
8.8
6.7
11.7
8.2
5.9
3.2
19.7
12.8
8.3
3.5
9.5
6.0
3.0
1.2
CHBrzCI
5.8
6.1
4.9
4.2
7.6
6.4
6.1
3.9
8.2
6.4
5.1
3.5
8.8
6,1
4,6
2.0
CHBr,
NFt
NF
NF
NF
0.7
0.6
0.4
0.6
NF
NF
NF
NF
1.1
1.0
0.7
0.5

TTHM
(jig/L)
35,4
26.5
24.9
18,8
31.9
22.7
17.2
10.4
52.5
33.3
21.3
10.4
29.9
18.3
13.4
7.6
Percent
TTHM
removal
0
25
30
47
0
29
46
67
0
37
69
80
0
39
• 65
75
"Batch rtictor.
tNon* found.
estimated  Henry's law constant compared with that of chloroform) in this water,
removal of the trihalomethanes would be expected to be difficult when compared
with that  of Louisville's tap  water  in which chloroform  is  the  dominant
trihalomethane.4' The data in Table 8, when compared with that in Table 7 (both
being batch reactors), show this to be the case. As one example, at a 15 to I air-to-
water ratio, 86 percent of the chloroform was removed from Louisville's tap water,
whereas at the same air-to-water ratio, only 38 percent of the bromoform was lost
from Contra Costa's drinking water. The two systems were not exactly comparable,
however, as shown by the removal of dibromochloromethane—57 percent in the
Louisville  study and 40 percent at Contra Costa, both at a 15 to I air-to-water ratio.
  For the  DWRD in-house study, a countercurrent aeration column was fabricated
from a 3.7-cm (l.S-tn) diameter glass tube, 0.9  m (3 ft)  long, with a fritted glass
diffuser. At an air-to-water (volume-to-volume) ratio common to water treatment
aerator designs for controlling taste and odor problems (1 to 1), the chloroform
concentration in Cincinnati tap water was not significantly changed from that of the
control, although a decline in the concentration of bromodichloromethane did occur
(Table 9).  Increasing the air-to-water ratio to 8 to  1 yielded a 52 percent TTHM
concentration decline, and a further increase to 20 to  1  showed an'84 percent
decrease. For comparison purposes, a conventional activated sludge wastewater
treatment  plant is designed with about an 8 to 1 air-to-water ratio, ancl the gas-
to-water ratio in the purging step in the trihalomethane analysis3 is approximately 44
to 1 when operated as a batch system.  Although the ratio  of chloroform to total
trihalomethane concentrations are not exactly the same in Cincinnati and Louisville
tap water, 0.77 versus 0.42 (average of four experiments), the percent removals of
total trihalomethanes were similar at similar air-to-water ratios, Table 747 and Table
9, even though the data in Table 7 were from a batch reactor.

44  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                       TABLE 8. DIFFUSED-AIR AERATION STUDIES,* SEPTEMBER 1977,

                               CONTRA COSTA COUNTY WATER DISTRICT20
I

•8"


I
I
o
5"
if
a
5
Approximate
air-to-water
ratio (V/VJ
Height of
water column
(cm)
(in)
Aeration
time
Trihalomethanes (/iQ/U
CHCI,
CHBrCI,
CHBrtCI
CHBr,
TTHM
(MB/L)
Percent
TTHM
removal
OPEN CONTAINER TEST
Control
1:
4:
8:
19.

Control
12
15
6
6
Control
9
Control
sample
1
1
1
1

sample
:1
:1
:1
:1
sample
:1
sample
22:1
_
14
14
13
13

—
45
38
90
80
—
90
— .
90
—
5.5
5.4
5.3
S.2

—
18
15
36
32
—
36
. —
36

10
30
60
120


1
2
1
2

4

8

min
min
min
min


hr
hr
hr
hr

hr

hr
<1
2,
2
1
1
COLUMN
2
3
2
2
2
3
3
5
3
3
12
11
10
9
TEST
4
2
1
3
3
4
2
t8
7
24
49
43
38
30

28
18
15
24
22
33
19
84
44
239
199
160
130
75

196
140
122
171
159
229 „
139
189
133
266
262
216
179
115

230
163
140
200
186
269
163
296
187
—
1,5
19
32
57

—
29
39
13
19
—
39
—
37

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     TABLE 9. REDUCTION OF TRIHALOMETHANE CONCENTRATIONS
          IN WATER BY DIFFUSED-AIR AERATION,* CINCINNATI
                              TAP WATER

Airf-to-water
ratio {V/V)
Control
1:1
8:1
12:1
16:1
20:1
Chlorine
residual
(mg/L)
1.3
1.2
1.2
1.2
1.2
1.1




Trihalomothanes (/ug/L)
CHCI,
99
101
45
33
19
16
CHBrCI,
24
B
13
7
8
5
CHBr,CI
5
5
3
<1
3
3
CHBrj
NFJ
NF
NF
NF
NF
NF

TTHM
(jig/L)
128
111
61
40*
30
21
Percent
TTHM
removal
—
13
52
69
77
84
"Coimtflfcurrent flow.
tActfv'*t*£i cmtbon filttwd compreited air,
JNon« found.
  Tower Aeration—Rook studied the removal of chloroform in a 4-m (12.4-ft) high
cascading countercurrent aerator filled with crosswise arranged  racks of plastic
tubing." His data showed a 50 percent removal of chloroform at a calculated air-to-
water ratio of 3.2 to 1.
  Houel et al, studied the removal of chloroform spiked into water by air stripping in
a countercurrent tower having a cross section of 60 by 45 cm (23 by 18 in) and a total
packing depth of 4 m (14 ft).41 The air supply was metered and capable of delivering'a
maximum of about 35 m*/min (1,250 efrn). Water loading rates up to 27 m3/day (5
gpm) were used. Two packing materials were used: Type A, egg crate style; and Type
B, a proprietary product,  Munters Plasdek®, Code CF-1DA, inclined wavy PVC
sheets. The results in Table 10 show that at these very high  calculated air-to-water
ratios, chloroform was very effectively removed.


       TABLE 10.  TOWER AERATION  FOR THE REMOVAL OF
      CHLOROFORM FROM CHLOROFORM-SPIKED WATER48'
Run number
Variable
Packing typef
1
A
2
A
3
A
4
B
5
B
6
B
 Calculated air-
 to-water ratio
 (V/V)           6100:1   7700:1   9400:1   1800:1   2500:1   2600:1
 Initial CHCI,
 concentration
843
 Final CHCI,
 concentration
                           843
                            <0.2
843
                                              536
                                               13.2
638
                                                                536
   1.6     <0.2
 Percent CHC13
 removal         >99.98   >99.97   >99.98    97.5     99.8    >99.96

 *C
-------
  McCarty reported on a study at Water Factory 21 in Orange County, California,
in which tower aeration was included as part of the treatment scheme.43 In this study,
both large cross-flow stripping towers and smaller countercurrent decarbonators
were studied. The two stripping towers were each 63 m (210 ft) long by 19 m (62 ft)
wide and contained 7.6 m (25 ft) of polypropylene splash-bar packing. Six fans were
included per tower, each 5.5 m (18 ft) in diameter. They provided 990 nr'/sec (2 X
10* cfm) of air, or about 3,000 mJ air/m3 of water (calculated air-to-water ratio) at
design capacity. The two stripping towers were designed to treat 0.66 m3/sec (15
mgd) of flow.
  The two decarbonators were designed to treat 0,22 m3/sec (5 mgd) of flow.  Each
was 2 m square (6.5 ft) and contained 2.4 m (8 ft) of polyethylene packing. The total
volume of media in the decarbonators  was only  19 m3  (670 ft ) compared with
18,000 m3 (634,000 ft3) in the stripping  towers. Each decarbonator had a  blower
designed  to  provide 22  m3 air/m  water applied (calculated air-to-water ratio).
Although the concentrations  of the trihalomethanes were quite low, making the
calculation of a percent removal somewhat suspect, the data (Table 11) show  good
removals.
  Wood  et  al. studied  the  removal of trihalomethanes, both  spiked into and
naturally  occurring  in   Miami, Florida,  tap water,  in  a 2.7-m  (9-ft)  high
countercurrent tower 0.3 m (1 ft) square.49 The packing media was 1.3-cm (0.5 in)
diameter PVC pipe on 8-em (3 in) centers. The flow through the tower was 160
m3/day (30 gpm) and was distributed over the cross-section of the tower by nine
showerheads. To  study  increasing  air-to-water ratios, the water was recycled to
provide multiple passes. An induced draft was provided by a 4.2-mJ/min (150-cfm)
fan, resulting in a calculated 38 to 1  air-to-water ratio when the fan was on. Studies
were made both with and without the fan operating. The data in Table 12 show that
in this particular instance, the fan did not aid in thestripping of chloroform, a finding
similar to that shown in Table 11.43
  Studies  sponsored  by  the American  Water  Works Association  Research
Foundation employed a  I5-cm (6-in) diameter countercurrent column packed with
various depths of 0.6-cm (i/4-in) interlocked ceramic saddles, Intalox®.50 Various
water flows  and forced-draft air flows were used to study  different air-to-water
ratios. The data in Table 13 show the improvement of aeration with increased depth
at a constant  calculated air-to-water ratio, as well as the positive influence of
increasing the  air-to-water ratio at  a constant depth.
  The difference  between  the  initial  chloroform concentration and TTHM
concentration indicates the presence of bromine-containing trihalomethanes in this
water. The  average ratio of chloroform concentration  to  total trihalomethane
concentration  was 0.76 for the five tests. Under these circumstances, the percent
removal for TTHM should be lower than for chloroform because of the difficulties in
stripping the bromine-containing trihalomethanes. This was  not shown  in three of
these  five  tests, although  the  concentration  of  the   bromine-containing
trihalomethanes might not have been high enough to significantly influence the data.
  Two other studies demonstrated  the positive influence  of air-to-water ratio and
tower height on removal of trihalomethanes. In another test during the Miami,
Florida, study. Wood et al. investigated the effect of increasing air-to-water ratio on
the removal of the four trihalomethane species spiked into Miami tap water by
passing the water through the tower several times.   Although the air-to-water  ratio
was not known, it increased incrementally with each water pass. The same tower was
used as described previously. The data in Table 14 confirmed two previously noted
conclusions:  one, that  the increase  of air-to-water ratio with each pass had a
positive influence on the stripping of trihalomethanes; and two, that bromoform.as
expected, is more difficult to remove by aeration than is chloroform. The air-to-water
ratio' needed to obtain 61  percent bromoform  removal was twice that needed to
obtain 61 percent chloroform removal.
                Section VI. Treatment Techniques to Remove Trihalomethanes  47

-------
                 TABLE 11. REMOVAL OF TRIHALOMETHANES BY AIR STRIPPING AT WATER FACTORY 21"
I

t

Cross flow stripping towers
Induced draft
Contaminant
CHCIj
CHBrCI,
CHBr,CI
A'
W
3000:
3000:
3000:
Concen-
tration!
(/
-------
          TABLE 13. REMOVAL OF TRIHALOMETHANES AT
                  NORTH MIAMI BEACH, FLORIDA6*"

                               	Run number	
Variable	1	2	3	4	5
Packed bed depth
 meters                          1       2,1      2.5      2.1      2.1
 feet                             3.3     7       8.3      7        7

Calculated air-to-water ratio
 (V/Vj                          10:1     10:1     10:1    32:1     40:1

CHCI,
 Initial concentration (jug/L)        29      26      23      27       27
 Final concentration (Mg/L)        15       9.4      7.1      6.2      5.9
 Percent removal                 48      64      69      77       78
TTHM
Initial concentration (ng/L)
Final concentration (M9/L)
Percent removal

40
22
45

35
12
66

29
9.3
68

35
7.0
80

33
5.9
82
 *Counf«feyrr»nt flow, forced draft; tower aeration; water ternparatura = 27°C {81 °F}.

    TABLE 14. REMOVAL OF TRIHALOMETHANES SPIKED INTO
                   MIAMI, FLORIDA, TAP WATER49*


Pass
1
2
3
4
5
Relative
air-to-water
ratio
x*
2x
3x
4x
5x





Percent removal
CHCI,
61
91
97
99
99*
CHBrCI2
69
86
95
98
99
CHBr,CI
56
75
90
96
97
CHBr,
39
61
86
90
93
TTHMt
47
74
89
93
95
•Countercurrent flow; tower aeration, natural draft (air»to-watar ratio cannot be calculated).
tDominated by bromoform that w«« >pikad at e concentration about aavan time» that of the othar
 trthaJomethan«.
{Unknown.

  In another test, one of the cooling towers for the USEPA Environmental Research
Center's air conditioning system in Cincinnati was used to examine the effects of
countercurrent-induced draft-packed tower aeration on trihalomethane removal.
Cincinnati tap water was passed through one side of the tower and samples were
collected at the midpoint and the bottom, approximately 2 mand4 m (6 ft and 12 ft),
respectively, both with and without the fan in operation. This tower was designed for
over 12,000 m3/day (2,200 gpm) of recirculated flow, but the flow for this study was
limited to about 3,000 mj/day (550 gpm) for the single-pass study. The low flow
through a part of the unit prevented an estimate of an air-to-water ratio, but the
improvement in trihalomethane removal  with increasing tower depth is shown in
Table 15,

Discussion—
  The data presented above can now be compared among studies and against the
theoretical  optimum system described in the General  Considerations subsection.

               Section VI. Treatment Techniques to Remove Trihalomethanes  49

-------
TABLE 15. TRIHALOMETHANE REMOVAL IN A COOLING TOWER,»
                       CINCINNATI TAP WATERf
                       	Trihalomethanes (jig/Li
                       CHCI,  CHBrCI, CHBr,CI CHBr,
TTHM
Percent
 TTHM
removal
 Influent
  Run1                 44      21       7       1        76       —
  Run 2                 48      24      10       1        84       —

 Midpoint—2m (6 ft)
 Induced draft
  Run 1                  4       1       1        1         7       91
  Run 2                  31       1       NF*       S       94
 Natural draft
  Run 1                 10       6       4       1        20       74
  Run 2                  8       4       3       1        16       81
Bottom— 4m (12 ft)
Induced draft
Run 1
Run 2
Natural draft
Run 1
Run 2


3
3

6
7


1
1

2
3


1
1

2
2


NF
NF

1
1


5
5

11
13


93
94

86
85
 •Unknown *!r*to-wat*r ratio,
 tCounttfCurr*nt flow.
 iNon« found.

Figure 25 is based partly on the assumption that the initial concentration of a
contaminant does not influence the percent remaining for a given air-to-water ratio.
To verify this concept, the data from the multi-pass experiment reported in Table
144'  were reanalyzed. The data in Figure 26 show  that for chloroform,  in this
experiment, the same percentage of the chloroform  concentration present in the
water at the start of each pass was remaining at the end of that pass, for all four passes
through  the  column. Therefore, the percent  remaining after  each pass was
independent of the starting concentration (lower at the beginning of each pass) and
thus, a single "perfect counterflow column" curve can be used for the analysis in
Figure 25, Similar data were also obtained for the other trihalomethanes measured
in this  experiment.
   Having verified the "universality" of Figure 25, all data were plotted on the same
graph.  Figure 27, to compare the performance of all the systems with data on
chloroform removal where air-to-water ratios were available with the operation of a
perfect counterflow system. Figure 27 can be used to compare system efficiencies.
The farther a given datum point is to the right of the perfect counterflow column line,
the less effectively air is  being used for a given percent chloroform remaining.
   In inefficient cases, mass transfer (water to air) must be improved to accomplish
more effective use of air. As described earlier, this can be done by changing design
parameters such  as liquid or gas flow rates, selecting packings (for towers), and
increasing contactor height. Any of these changes may affect the cost of the system or
its operation, and therefore, cost benefits realized by using less air must be weighed
against cost increases brought by improvement in system mass transfer efficiency.
   From  Figure  27,  in  general, the best  removals of chloroform were by
COuntereurrent towers (greater than 90 percent)  although air use was relatively
inefficient; more efficient use of air was observed in batch diffused air experiments,
but actual chloroform removals were poorer (approximately 50 percent). For this
50  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
        100
      O
      z
      O
      O
       n
      CJ

      O
                        1  -        2          3          4

                     NUMBER OF PASSES THROUGH TOWER

               Figure 26.  Miami, Florida, tower aeration study.48
application, diffused air'systems generally require higher air-to-water ratios (because
of poorer mass transfer efficiency) than do countercurrent towers to accomplish the
same treatment goal. When required, scaleup of the diffused air systems to achieve
percent removals greater than 90 percent by increasing air-to-water ratios may prove
to be difficult. Conversely, tower design improvements may result in more efficient
use'of air for the higher percent removal examples shown in Figure 27. Studies may
show that diffused  air  systems  are appropriate when  required removals  of
trihaiomethanes are minimal whereas towers may be generally preferred for utilities
requiring larger percentage removals.
  In summary, aeration is a feasible approach to trihalomethane removal, with the
difficulty  of removal 'increasing with  molecular weight from chloroform  to
                Section VI. Treatment Techniques to Remove Trihatomethanes  51

-------
IvJ


?


I
3
I
•o*
I
r>
Q
                       100
I
3"
$
Sf
I
                                                                                                  kfchouu Oiniued Air Counter Curttm
                                                                                                2 CMfoud Air Btieh"
                                                                                                3 Towot Countgr Cuiionl"
                                                                                                4 Towtr Counter Current"
                                                                                                5 T
-------
bromoform.  A utility considering aeration  for  trihalomethane control  should
consider the feasibility on the basis of known sound aerator design principles.
Because of variations among utilities, such as degree of treatment required, mixture
of trihalomethanes present, temperature, and other water quality considerations,
this should be followed by pilot study verification at that location,

Adsorption

Powdered Activated Carbon (PAC>—
   General Considerations—To  determine  what  degree  of removal of dissolved
organic material can be effected  by adsorption, an isotherm test is usually run. The
adsorption isotherm is the relationship between the amount of substance adsorbed
and  its concentration in the surrounding solution at equilibrium. The adsorption
isotherm consists of a curve plotted with residual concentration of the solute in
solution on the"x"axisand the amount adsorbed per unit weight of adsorbent on the
"y" axis. Thus, any point  on the line gives the adsorption capacity or loading at a
particular concentration in solution. With activated carbon adsorption from dilute
solutions, such  as trihalomethanes in drinking water, a  logarithmic plotting
according to the empirical Freundlich equation,

                                x/M  = kC"°                           [Eq. 8]

where: -x  = amount of substance adsorbed, calculated  from original and equilibrium
            concentrations, C, and Cr,
       M  = weight of activated carbon, and
        k and n are constants; k is the intercept at O =  I (logO = 0)and I/n is the slope of
        the line

usually yields a straight line over the concentration ranges  for trihalomethanes
usually found in drinking water.
   Data points required to construct the adsorption isotherm are usually obtained by
applying varying doses of PAC  to replicate samples  of a solution of the solute in
question (a trihalomethane) in -water. These samples are held in suitable containers
to prevent losses. After  equilibrium is  achieved,  no further change  rn  solute
concentration occurs.  The activated carbon is then separated from the liquid sample,
and residual dissolved solute concentrations are measured. The calculated values of
X/ M are plotted against respective Cr values on log/ log  coordinates.
   Using closed containers and under controlled conditions with 2 hours of contact,
Dobbs and Cohen determined the adsorption isotherms for the trihalomethanes in
distilled water using ground Filtrasorb® 300,5!* Adsorption isotherms can be used to
calculate the required PAC dose needed to reduce a contaminant concentration from
some given influent concentration to some target effluent concentration. Using
Figure 28 as an example, to reduce the chloroform concentration from 150 fug/ L to
75 Mg/ L, the required  PAC dose  is calculated as follows. The equilibrium  "loading"
(X/M) on the adsorbent at the final chloroform concentration  of 75 ^g/L (arrow) is
about 0.38 #g chloroform adsorbed per mg of PAC (Figure 28).  Because (150
Mg/L - 75 Mg/L) -  75 Mg chloroform/L that must be adsorbed, 75/0.38 = 197
mg PAC/ L is required. As this  is a very high PAC dose, it indicates the generally
poor adsorbability of chloroform by activated carbon.
   Figure 29, in which the adsorption isotherms for all four common trihalomethanes
are shown together, indicates the increased adsorbability of the bromine-containing
trihalomethanes. Using the same example as above for bromoform, 15 mg powdered
"Manufactured by Calgon Corporation. Pittsburgh. PA 15230. Hereafter Calgon Corporation products arc either designated
 Fllirasorta* 200 or F-200. Filtrasorb* 300 or F-.'OO, or Filtrasorb* 400 or F-400.


                Section VI. Treatment Techniques to Remove Trihalomethanes  53

-------
         10  -IT
      o>
     u
     <  1,0
     m
     ee
     O
     o
     21      ™" *°
     5

     o      4-
        0,01
           0.001
I  I lllll|—I  I  I I  I lli|	1   1 I  1 I  III]	1  I  I I I

      0,01           0.1             1.0


       EQUILIBRIUM CONC (C(),  mg/L
                                                                       10
          Figure 28.  Adsorption isotherm for chloroform with F-300.81
         0.01
           0,001
                           0.01           0.1             1.0


                            EQUILIBRIUM CONC (Cf), mg/L
                                                                      10
         Figure 29.   Adsorption isotherm for four trihalomethanes with

                     F-300."
54   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
Filtrasorb® 300/ L would be required to lower a concentration of ISO fig/ L to 75
^g/L,  or  only  7,6 percent of the PAC dose required for  the same amount of
chloroform removal.
  The above discussion assumes that equilibrium is reached during the normal water
treatment process  where PAC is applied.  Even though the rate of adsorption
(approach to equilibrium) is typically rapid when PAC is used, normally measured in
minutes to hours, equilibrium  may not always be reached at utilities using a short
contact time. This kinetic effect  would reduce the effectiveness of this treatment
technique.
  Additionally, other solutes present in the water being treated may compete for
"active sites" on the adsorbent, and disinfectant residuals may influence adsorbent
qualities. Adsorption capacities for different activated carbons will also vary. These
effects complicate extrapolations from published isotherm  data to  actual water
treatment practice, as will be seen below.

  Experimental Results—In  one  study,  where the  trihalomethanes  occurred
naturally, Weil exposed  Louisville, K.Y, tap water  containing little free chlorine
residual, 0.12 mg/L, to various  doses of PAC in 1-liter mixed, open containers, and
determined the residual trihalomethane concentrations after  various exposure
times.47 His data (Table 16) confirm that at least 50 mg/ L PAC was needed to bring
about 50 percent removal of total trihalomethanes. As expected, the percent removal
of bromodichloromethane and dibromochloromethane was higher than the percent
chloroform removal for each PAC dose and exposure time. This, again, shows the
increased adsorbability of the bromine-containing trihalomethanes. The adsorption
isotherm of the 60-minute exposure data for chloroform compares fairly well with the
results of Dobbs and Cohen, ' the slope being similar, but the line displaced upward
(Figure 30). Note that the use of open containers may have contributed to the loss of
the solute attributed  to adsorption.
  In another jar test study, Hoehnetal. chlorinated simulated lake water containing
3 mg humic acids/ L." To avoid the complicating factor of the presence of a chlorine
residual, in one experiment they dechlorinated the  water before adding the  PAC
(lower curve. Figure  31). These data, when transferred to an adsorption isotherm
format, produced a typical adsorption isotherm, although displaced from the data of
Dobbs and Cohen51 (Figure 32). Two factors that may have influenced these data are
the type of PAC used in the Hoehn et al.s2 study and the presence of floe.
  In another experiment, these investigators allowed the chlorine residual, 10 mg/ L,
to remain when the PAC was added to the test vessels." The increase in chloroform
concentration for the same PAC dose (upper curve. Figure 31) is likely to be caused
by the influence of the chlorine  residual present during this type of test. The residual
chloroform concentration increased because chloroform  was being formed by the
reaction of precursor and free chlorine during the 30-minute exposure in the jars, as
evidenced by the increase in chloroform concentration at the zero PAC dose. At
other PAC doses, however, the increase in chloroform concentration could be
influenced by: 1) the alteration of the surface of the activated carbon by the free
chlorine so it was less able to adsorb chloroform (McGuireet al.55); 2) the PAC itself
because it was acting as a chloroform precursor or introducing associated precursor;
3) a combination of both factors; or4) the reason noted above, even though the PAC
would tend to lower the chlorine residual.  Nevertheless, the resulting adsorption
isotherm does not deviate from the adsorption isotherm using data collected in the
absence of a chlorine residual (Figure 32, page 58), which indicates that the reaction
of free chlorine and precursor  in the water  is probably the most important factor
in this case.
  Many water treatment plants are designed to add PAC to  water containing both
coagulant and chlorine residual for taste and odor control. Therefore, studies of this
type are typical of some situations encountered in the field. For example, before July
1975, the Cincinnati  Water Works added chlorine and alum to Ohio River water

                Section VI, Treatment Techniques to Remove Trihalomethanes SS

-------
                TABLE 16. TRiHALOMETHANE CONCENTRATIONS IN POWDERED ACTIVATED CARBON
                              (PAC) EXPERIMENTS,*7 LOUISVILLE, KY, TAP WATER*
I

I
 "
Ci
3'
5-
PAC dose
(mg/L)
0
{Control)



25




50




100




Exposure
time
(minutes)
0
5
15
30
60
0
5
15
30
60
0
5
15
30
60
0
5
15
30
60
Trihalomethanesf
CHCU
l*«g/L)
35.2
30,3
31.8
30.2
29.4
3S.2
26.3
24.1
23.2
19.2
35.2
25.0
18.1
17.7
15.5
35.2
17.4
13.2
10.1
9.7
Percent
removal
—
—
—
—
—
0
13
24
23
35
0
17
43
41
47
0
43
58
67
67
CHBrCI,
teo/L)
12.3
10.3
10.2
10.5
8.7
12.3
7.2
5.9
S.3
3.9
12.3
4.9
3.1
2.7
2.1
12.3
2.8
1.4
1.0
0.8
Percent
removal
—
—
—
—
—
0
30
42
50
55
0
52
70
74
76
0
73
86
90
91
CH8r,Cl
teo/L)
0.7
1.1
0.7
0.7
0.5
0.7
0.3
0.3
0.2
0.1
0.7
0.2
0.1
0.1
0.1
0.7
0.1
0.0
0.0
0.0
Percent
removal
	
—
—
—
—
0
73
57
71
80
0
82
86
86
80
0
91
100
100
100
TTHM
teO/D
48.2
41.7
42.7
41.4
38.6
48.2
33.8
30.3
28.7
23.2
48.2
30.1
21.3
20.5
17.7
48.2
20.3
14.6
11.1
10.5
Percent
TTHM
removal
	
—
—
—
—
0
19
29
31
40
0
28
50
50
54
0
51
66
73
73
               "Free chlorine residual = 0,12mg/L.
               f No bromofotfn found.

-------
    10
o>
o
&
X
OQ
tr
O
z
o
<
o
   0.01
                                                      r r i r I n
                             Dobbs and Cohen
                             120 Minute Contact Time
i  i  111ml—i  i n i  ml—i  i  in m|—i  11 mi
      0.001
                    0,01           0.1            1.0

                      EQUILIBBIUM CONC (Cf), mg/L
                                                               10
    Figure 30.   Comparison  of  chloroform adsorption isotherms
                from Weil*' and Dobbs and Cohen.61
         Samples
         Dechlorrnated
         After 30-Min
      0    10  20   30   40   50   60   70   80   90   100  110   120

                            PAC DOSE, mg/L

    Figure 31.   Treatment of simulated lake water with PAC. pH 7.9;
                27°C (81 °F); 3 mg/L humic acid
                Treatment:
                a. 10 mg/L prechlorination.
                b. coagulation/flocculation/sedimentation
                c. activated carbon; 30-rnin contact; pH 6.7
                d. filtration8*
          Sect/on VI.  Treatment Techniques to Remove Trihalomethanes  57

-------
        10 f

     o>    ~~
     O)
    xJJE
     o
     2
    ~f- From Hoehn et al.
       30 Minute Contact
1.0 -=-
     K
     O
     §  0.1 -

     i      :
     o
     I
        0.01
               • - Deehlorinated
               O - Chlorine Present
                                              From Dobbs and Cohen
                                              120 Minute Contact
           0.001
                 m—i  i  ii i  ml—i  11niiii
                  0.01           0.1            1.0
                   EQUILIBRIUM CONC (Cf>, mg/L
                                                                    10
         Figure 32.
             Comparison of the adsorption isotherms for chloro-
             form from Hoehn et al.s2 and Dobbs and Cohen.51
before 2 days'storage in off-stream reservoirs. For taste and odor control, PAC was
often added at the rapid mix in the presence of free chlorine residual and coagulant.
Although this practice is common, it should be avoided where possible and in new
designs. In an in-house study of this water, PAC was added to the water samples,
mixed at 100 rpm for 2 minutes and 50 rpm for 5 minutes, settled for 30 minutes,
centrifuged at 1,500 rpm (480 gravities) for 20 minutes, decanted, and analyzed for
trihalomethanes. The data in Table 17 show that  doses of PAC far higher than
conventionally used for taste and odor control were required to obtain significant
 TABLE 17. REDUCING TRIHALOMETHANE CONCENTRATIONS IN
             CHLORINATED OHIO RIVER WATER USING
              POWDERED ACTIVATED CARBON (PAC}»
Trihalomethanes (^g/L)
PACt dose (mg/L)
0
1
2
4
8
16
32
64
100
CHCI,
64
52
53
51
51
48
45
35
30
CHBrCl,
9
7
7
7
8
8
6
4
2
CHBr2CI
2
1
1
<1
1
<1
1
<1
<1
CHBr,
NFf
NF
NF
NF
NF
NF
NF
NF
NF
TTHM
(M9/L)
75
60
61
58+
60
56+
52
39+
32+
Percent
TTHM
reduction
—
20
19
23
20
25
31
48
58
•Alum and chlotina *ddad end w*Mr itorad off-»«ream In open rmervoirs for 2 days,
tWMercarbS, minufacturod by Huiky Induitrloi, Dunnollon, FL 32630.
(Nona found.
58  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
removals. The data in Figure 33 show the relationship between the reaction of free
chlorine and PAC and the adsorption of chloroform by PAC. Converting these
chloroform data to an adsorption isotherm format produced a very atypical pattern
(Figure 34)  which suggests that the presence of the free chlorine residual had a
significant influence on the adsorption  phenomenon in this case,
  Singley et al," in North Miami Beach, Florida, and Cams and Stinson55 at the
East Bay Municipal Utility District in California attempted to evaluate the use of
PAC for  the adsorption of trihalomethanes. None of the trials were unusually
successful, and all had at least the complicating problem of the presence of chlorine
residual.  Because  some  polyelectrolytes  used in  water treatment can  act  as
trihalomethane precursors (Feige et al.*6), investigators conducting jar tests or full
plant experiments where these materials are present should control for their possible
influence.
      X  2.0
      0
      55
      ul
      
-------
        10
     CD
    X5    II

    2  t.O
    x      .
    UJ
     CO
     K
     o
     <  0,1
     <2     3:
     z

     1     1
       0,01
                     From Figure 33
                     37 Minute Contact
                                              From Dobbs and Cohen
                                              120 Minutes Contact
           0.001
                         0.01           0,1            1.0

                          EQUILIBRIUM CONC (C{), mg/L
                                                                    10
         Figure 34.   Comparison of adsorption isotherms for chloroform
                     from a USEPA-DWRD in-house study and Dobbs and
                     Cohen.51
    01
    CQ
    o:
    O

    Q
    < 0,1  -4r

    C3

    5

    g
       0.01
                                              Dobbs and Cohen
         0.001
0.01           0.1             1.0

 EQUILIBRIUM CONC (Cf), mg/L
                                                                   10
         Figure 35.   Summary of four studies (References 47,51,52, and
                     a USEPA-DWRD in-house study) of the adsorption of
                     chloroform on powdered activated carbon.
60  Treatment Techniques for Controlling Tr/halomethanes in Drinking Water

-------
effective for the removal of chloroform. The bromine-containing trihalomethanes
were much more adsorbable, however, and if they dominate the trihalomethane
mixture in a given location, treatment with PAC might be considered as an effective
treatment.

Granular Activated Carbon (GAC)—
  General  Considerations—GAC  adsorption  systems used in  drinking water
treatment typically use stationary beds with the liquid flowing downward through
the adsorbent. Under these conditions adsorbed material accumulates at the top of
the bed. until the amount adsorbed at that point reaches a maximum. The maximum
amount of a contaminant that can be adsorbed on activated carbon occurs when the
adsorbed material is in equilibrium with the concentration of the contaminant in
solution surrounding the adsorbent. For any given concentration of material in the
liquid phase, the "loading on" or "capacity of" the activated carbon at equilibrium
can be determined from the appropriate adsorption isotherm, as discussed above.
When the adsorbed material is in equilibrium with the  influent concentration, the
adsorbent is "loaded" to capacity and that portion of the bed is "exhausted." In an
ideal "plug flow" operation, the exhausted zone moves downward with time in
service until the entire adsorbent bed is exhausted. This is shown graphically in
Figure 36 where the shaded area represents the exhausted activated carbon and the
clear area is the remaining fresh activated  carbon in the lower portions of the bed.
Figure  36  also represents the  corresponding  breakthrough  profile  of  the
contaminant in solution with time. The effluent concentration (Coirr) remains near
zero until the exhausted zone of the GAC reaches the bottom of thecolumn and then
abruptly increases to the influent concentration when the  entire column is exhausted.
Thus, the effluent concentration is equal  to the influent concentration when the
column is exhausted or at equilibrium, and ideally, therefore.thetimetoexhaustion
of an adsorber can be predicted from isotherm test information.
  For a given situation, the time to reach exhaustion can be estimated by knowing
the influent contaminant  concentration, the approach  velocity (to calculate mass
loading), the adsorber bed depth, the density of the adsorbent, and the equilibrium
loading from an adsorption isotherm. This estimation assumes a constant influent
concentration of contaminant and neglects the influence of competitive adsorption.
For example, assume an influent chloroform concentration of 100 ng/L, a 5 m/hr
(2 gpm/ft) approach velocity, a 0.9-m (3-ft) bed depth, and an adsorbent density of
490 kg/m' (30 Ib/ft3). According to Figure 28, at exhaustion (d  = Cf), the loading
on or capacity of the adsorbent would be 0.49 mg/g or g/kg.
  For a 0.09m2 (1ft2) cross-section of this  bed 2 gal/min X !,440min/day X  3.78
L/gal = 10,886 L/day pass through. Multiplying by the  chloroform concentration.
10,886  L/day X 100 ng/L, yields 1.09 g/day of chloroform applied to the 0.09 nr
(I ft2) cross-section. This cross-section, 0.9 m (3 ft) deep, contains 0.08 tn3 (3 ft*) of
media. Converting this to weight yields 41 kg (90 Ib) of adsorbent. Therefore, the
days required to "load" this adsorbent to  equilibrium is:

  Days of operation  = Total weight of adsorbent X                   [Eq. 9]
                      equilibrium loading/daily load

  Days of operation  = (41 kg) (0.49 g/kg)/1.09 g/day
                . .   18.4 days

Thus, an estimated 18.4 days would be required to exhaust this bed. The data in
Table 18 are examples of these calculations  for a GAC  adsorber with a  10-minute
empty  bed contact time (EBCT)* and an approach velocity of 5  m/hr (2 gpm/ft2).
•Empty bed contact time (EBCT) equals "empty bed volume" divided by the -flow rale" through the bed.


                Sect/on VI. Treatment Techniques to Remove Trihalomethanes  61

-------
                    ADSORBED CONTAMINANT PROFILE


          FLOW IN            IN            IN            IN
           o

           2
           m
           a:
           O
           en

           §
          FLOW OUT          OUT          OUT          OUT



                     EFFLUENT CONTAMINANT PROFILE
        I
        o

        o
        u
                                                 'OUT

                              TIME IN OPERATION
               Figure 36.  Ideal adsorption column performance.
 TABLE 18. THEORETICAL TIME IN SERVICE UNTIL EXHAUSTION

               FOR TRIHALOMETHANE ADSORPTION


Constituent
CHCI,
CHBrCl,
CH8r,CI
CHBrj
Influent
concentration
CMS/LJ
75
50
25
10
Loading at
equilibrium*
(mg/g)
0.35
1.3
1.4
1.8
' Time to
exhaustion!}
(days)
15
87
189
606
"From Figur* 29.**

t1O mJnuta EBCT, approach velocity - 5 m/hr (2 gpni/ft1), GAG density - 490 kg/m* (30 Ib/ft3).

jExhauttlon for total trihalomethanas will not occur until tho species with the feast adsorption cHarccteriitic

 r**ches OJthauitfon,                                               .      -•    -
82  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
 Because, in this example, chloroform is present in the highest concentration and is
 the trihalomethane most poorly adsorbed, the "service time to exhaustion" is the
 shortest for that compound.
  This same approach can be used to estimate the influence of the three factors that
 control the time in  service to exhaustion for  a  GAC adsorber. Based on  the
 adsorption isotherm data (Figure 29), the data in Table 19 show that, to a varying
 degree, EBCT, influent concentration,  and trihalomethane species all have an
 influence on the calculated time in service to exhaustion.

      TABLE 19, INFLUENCE OF INFLUENT CONCENTRATION,
           EMPTY BED  CONTACT TIME, AND SPECIES OF
   TRIHALOMETHANE ON SERVICE TIME TO EXHAUSTION* OF
                 GRANULAR ACTIVATED  CARBONf
Constituent/
EBCT
(minutes)
Chloroform
3 • ' •
10
40
Bromoform
3
10
40
Influent concentration at exhaustion (/*g/L)
5*

10 days§
34 days
1 35 days

242 days
808 days
3232 days
25

7 days
24 days
96 days

117 days
390 days
15 60 days
100

5 days
1 6 days
66 days

61 days
202 days
808 days
•Based on Figure 29."
tApproach velocity = 6 tn/hr {2 apm/ft1); GAC density = 49O kg/m1 (30 Ib/ft'j.
IFlgure 29 extrapolated to this concentration.
§S«rvice time to exhaustion.

  When the other two variables are constant, the time in service to exhaustion is
directly proportional to EBCT. For chloroform, a twenty-fold increase in influent
concentration  resulted in a 50 percent decline in the service  time to exhaustion,
whereas the same increase in the bromoform influent concentration caused a 75
percent decline in  the service time to exhaustion.  Finally, the time in service to
exhaustion for bromoform was 24, 16, and 12 times longerthan that for chloroform
at the influent concentrations of 5 jug/L, 25 /ig/L, and 100 jtg/L, respectively.
  Although this approach may be  useful to determine the service life of an ideal
adsorber,  these estimates may be of  only marginal use in practice.  Various
parameters affecting the rate of mass transfer within the adsorber (kinetic aspects of
adsorption) severely limit its application, and make necessary the use of pilot column
studies for accurate prediction of performance.
  Schematically illustrated in Figure 37 is a diagram showing the concentration of
adsorbed species* on the surface of the adsorbent (X/M)  with bed depth.  Under
operational conditions, adsorbed material accumulates at the top of the bed until the
amount adsorbed is in equilibrium with the influent contaminant concentration. At
this time the adsorbent is loaded to capacity and that portion of the bed is exhausted.
Below that zone is a second zone where dynamic adsorption is taking place, i.e., the
contaminant is being transferred from the liquid solute to the adsorbed phase. This
zone is called the "mass transfer zone,"57 and its depth (deviation from ideal plug
flow) is controlled by many factors,  depending on the contaminant being adsorbed,
characteristics of the adsorbent, hydraulic factors, and others. The depth of the mass
transfer zone is a  measure of physical/chemical resistance to mass transfer. Once
formed, the mass transfer zone moves down through the adsorbent bed until it
reaches the bottom, whereupon the effluent concentration of the contaminant in the

               Section VI. Treatment Techniques to Remove Trihalomethanes 63

-------
                       ADSORBENT LOADING (X/M)
                BED
                DEPTH
                                                  X/M
                                                '  at Saturation
                                                  (Exhausted)
                                              Mass
                                              Transfer
                                              Zone
              Figure 37,  Mass transfer zone in a GAC adsorber.


aqueous phase begins to rise (Figure 38).  Figure  38A shows the concentration
gradient of adsorbed material (X/ M) in an adsorber as the mass transfer zone moves
down the column with time. As the mass transfer zone reaches the bottom of the
column, "breakthrough" of the contaminant occurs as noted by a detectable increase
in effluent concentration (Figure 38B). When the adsorber is operated to exhaustion
(at  equilibrium;  CIN = COUT),  the breakthrough  profile  (plot   of  effluent
concentration with time) takes on a classical "S" shape — a shape controlled by the
shape and length of the mass transfer zone.
  Thus, any estimate from isotherm data of a dynamic adsorber service time to
exhaustion is at least subject to error caused by the differences in mass loading
calculations based on ideal plug (low (Figure 36) and typical column performance
(Figure 38) as represented by Areas A and B in the effluent concentration profile
(Figure 38B). Clearly, undesirable concentrations of contaminant may appear long
before exhaustion  occurs in practice.
  When an  adsorber  is removing all of a contaminant, the mass transfer zone in
Figure 37 may also be called the "critical depth" because this is the minimum design
depth for an adsorber that will allow it to remove all of a contaminant. Although the
mass transfer zone is constant for a given situation  (based on the contaminant, its
concentration, the adsorbent used, and the flow rate), the critical depth changes
depending on the allowable effluent target. This change is because the critical depth
is defined as the  minimum design depth for an adsorber that will allow it to achieve
some target effluent concentration. The higher the target effluent concentration, the
smaller the critical bed depth.
  Figure 39 is a schematic illustration of the concentration profile of a contaminant
in solution within an adsorber in the region of the mass transfer zone showing the
relationship  between the size of the critical depth and three different target effluent
concentrations. In Figure 39A, the effluent target concentration is not reached
because the physical bed depth is less than the critical depth. Figure 39B shows that
the  effluent target is reached because the bed is deeper than the critical depth, and
39C shows  a decrease  in  critical depth  for a  less stringent effluent  target
concentration. Finally, if the adsorber can be allowed to operate to exhaustion, then
the  critical depth becomes zero as the target effluent concentration would equal the
influent concentration.
 64  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                        ADSORBENT LOADING (X/M)
      TOP
       ui
       Q
       Q
       UJ
       00
 BOTTOM
     TIME   T = O       T/4
T/2
3T/4
    Breakthrough
                            TIME IN OPERATION

           Figure 38.  Typical adsorption column performance.
       Comaminan! Cone
                                     B

                              Contaminant Cone
                                                   Contaminant Cone
    oo
  BED
DEPTH
           I
         Target
                                                        Cniical -
                                                        Depth
                               Target
       Target not reached.   Target Reached
       bed depth less than
       critical depth
                       I
                     Target

               Smaller critical
               Depth with
               Higher Target
               Concentration
        Figure 39.  Critical depth relationships in'a GAC adsorber.
             Section VI, Treatment Techniques to Remove Trihalomsthanos  65

-------
  From the above discussion, an additional factor complicating predictions of
adsorber service life can be deduced, namely, the effect of changing the influent
concentration of the contaminant. For example, if after a period of time in service
the influent concentration of the  contaminant suddenly  decreases, previously
adsorbed  material must desorb  to establish a new equilibrium condition. This
desorption creates a higher-than-predicted "wave" of contaminant concentration to
move down the column.  In the extreme, the effluent concentration of a given
contaminant may be higher than the influent concentration for a period of time.
"Chromatographic" effects caused by displacement of the adsorbed contaminant by
other materials with stronger adsorption characteristics also cause desorption to
occur with similar effluent/influent characteristics being observed.

  Experimental Results—For the studies done  in-house by USEPA's Drinking
Water Research Division,  glass columns, 3.7 cm (1.5 in)  in diameter, filled with
different depths and types of GAC (Table 20), were exposed to Cincinnati tap water
at various approach velocities and empty bed contact times to determine the ability
of GAC to remove chloroform and two other trihalomethanes. At an approach
velocity of 5 m/hr (2  gpm/ft2), the decrease in trihalomethane  concentrations
through 76 cm (30 in) of a  coal base and through a lignite  base GAC are shown in
Figures 40 and  41, respectively. These systems each had an  EBCT of 9 minutes.

 TABLE 20. GRANULAR ACTIVATED CARBON  CHARACTERISTICS

                               Coal base        Coal base      Lignite base*
 	Filtrasorb®200  Filtrasorb®400    HP 10x30
 Surface area by nitrogen gas
  BET method
  mVfl                        850-900       1060-1200         600

 Density
  kg/m»                         490             410            385
  Ib/W                           30               25             23.5

 * Kydrodarco! 1030 manufactured by ICI Amorfea. Inc., Alias Chemicals Division, Wilmington, DE19899,
  hcroiltor callad HO 10x30.
  These columns  were  started  at  different   times,  but the trihalomethane
breakthrough patterns are similar. The chloroform concentration was lowered 90
percent or more for  about 3 weeks, then  the effluent  chloroform concentration
steadily increased until it equalled the influent concentration at about the ninth or
tenth week.  The  trihalomethanes  containing  bromine were more effectively
adsorbed by the GAC. Positive reductions were observed for  26 to 30 weeks for
bromodichloromethaneand for about 40 weeks for dibromochloromethane (Figure
42, page 69) because of both a lower concentration in  the water and because the
bromine-containing trihalomethanes are  better adsorbed (Table IS, Figure 29). In
 1976, Rook reported similar findings.26
  Because adsorption is a  reversible process, after the bed is exhausted and if the
contaminant concentration declines, a new equilibrium will be established with less
material adsorbed on  the adsorbent. To reach this  lower adsorbent loading,
desorption  must  occur.  In this  study,   periods  existed when  the effluent
trihalomethane concentrations exceeded the influent, e.g.,  note chloroform  and
bromodichloromethane desorption in  Figure 42. A material balance after 30 weeks,
however, accounted for all but 6 percent of the total trihalomethane influent to the
coal base GAC  system and 16 percent to the lignite base GAC system. The influent
total trihalomethane loading used in the material balance was a summation of the
product of  the averaged  weekly flows and the influent  total trihalomethane
concentrations.

6S  Treatment Techniques for Controlling  Trihalomethanes in Drinking Water

-------
§'

                150
             x
             S  100 - -
             u
             z
             o
             u
             5   50-
             x
        I       T

    CHLOROFORM
                                    V
                          ,   Effluent
                 0  boA=S
                                                     30
                                                                                         6  p
01        234

     TIME IN OPERATION, rno
                                 10
0123

      TIME IN OPERATION, mo
                                                                                                    1       2       3

                                                                                                   TIME IN OPERATION, mo
1
                                        Figure 40.   Removal of trihalomethanes from Cincinnati, OH,
                                                    tap water by coal-base GAC. Test period, February-
                                                    May 1975; GAC type, Fittrasorb® 200, bed depth, 76
                                                    cm (30 in); hydraulic loading, 5 m/hr (2 gpm/ft2),
                                                    EBCT, 9 min. Bromoform was not found.

-------
2
i
1
51
I

I
 3-
 b
 a-
 3
 a
 a-
 s
 (ft
 
-------
1
§""' 8S
..
— Q
§ g 50 -
•H 0
§«£
til
•5 cc
5 v, A
I I
*"
§• -200 1
>,
\
\
y
\
A
;\

\'
CHLORO
'





ji — \ •,
/!; Vj
ill
1 I,
1/Tt fx_
/ \ / \
\l
FORM



I
— LIGNITE GAC
— COAL GAC
,
I
1
^

I A
ryx/y
V S *
"**rfi
1
IUU


50-







-50
h
\ \
\\

\




^
,-''\ /N -
' A^A ll \ f
'/v\i/ rA
f V V|
' r



BROMODICHLORO-
METHANE




•g' 0 10 20 30 40 0 10 20
<&




i LIGNITE GAC
COAL GAC

I
/•'I


1
1 A
M-
V /
* k/

IUU


SO -







-50
v"l -*^^*^
— UGNITE GAC \
— COAL GAC \ -
tai— _
I
I
\
i
V, /
OIBROMOCHLOROM ETHANE

I 1
	 H 	
30 40 0 10 20 30 «

* TIME IN OPERATION, wk TIME IN OPERATION, wk TIME IN OPERATION, wk
o
re
3
I

3
"V
to
1
a
s-
a
1
Ol
(0







f
Figure 42. Comparison of removal of trihalomelhanes from
Cincinnati, OH, tap water using two types of GAC. '
GACtype: lign te base, HD 10
x 30; coal base, Filtra-
sorb® 200; bed depth, 76 cm (30 in); hydraulic
loading, 5 m/hr (2 gpm/ftz);
EBCT, 9 min. Bromo-
form was not found.

























-------
  The trends shown in Figures 40 and 41 have been observed many times by others.
For  example, from  the  data  ORSANCO collected at  the  Huntington  Water
Corporation on a full-scale G AC bed, as expected, the time to exhaustion is greater
for the trihalomethancs containing bromine than for chloroform'8 (Figure 43).
  A  recent study at  the Cincinnati, Ohio, water treatment plant compared the
performance of  four  10-cm (4-in) diameter pilot columns receiving chlorinated
filtered water for the removal of trihalomethanes.JO Different adsorbent depths were
used to produce four different EBCT's. These data (Figure 44) show the influence of
both EBCT and  trihalomethane species on the.removal of these contaminants by
adsorption. Note, the point  of chlorination was moved closer in the treatment train
to the test units on 12/4/78, and the shorter reaction time resulted in lower influent
trihalomethane concentrations.
          ISO --
          30

          20

          10
                                        Effluent CHBr.CI
                   IIIIIII-I      I
             0     5     10    IS    20     2S    30    35    40    45
                            TIME IN OPERATION, wk
         Figure 43,   Trihalomethane removal at the Huntington Water
                     Corporation by GAC. GAC type, WVW 14 x 40; bed
                     depth, 76 cm  (3O in); approach velocity, 6.1 m/hr
                     (2.6 gpm/ft1);  EBCT, 7.1 min.">
7O  Treatment Techniques for Controlling Trihatomethanes in Drinking Water

-------
  G AC manufactured by four U.S. companies was compared for the adsorption of
chloroform at Miami, Florida.31 In this case, four parallel 2.5-cm (i-in) diameter
glass columns received filtered water from the treatment plant. These data (Figure
45, page 74) show three G AC's—the WVG,* the H D X 30, and the F-400—performed
similarly, agreeing with the results of the earlier comparison of HD 10 X 30 and F-
200 (Figure 42). These data also show that only the W950f GAC was significantly
better than the other three materials.
  Data on the adsorption of trihalomethanes on virgin GAC have been assembled
(Table 21, page 75). Because the influent concentration of TTHM was less than the MCL in
theTrihalomethane Regulation3 for many of these studies, tabulatinga time to reach
the MCL was  not  possible in those cases. Therefore, as  a measure of when the
adsorption process stopped, the time to reach exhaustion for TTHM removal was
tabulated  for each location. This, then, shows the general effectiveness of GAC
adsorption in a variety of places.
  Because of the strong influence of EBCT on the service time to exhaustion (Table
19, Figure 44), the data have been ranked in ascending order of EBCT. The mix of
trihalomethane species also influences the service time to  exhaustion  (Table 19).
Because of this, the Cl/Br ratio in the influent trihalomethanes at  the  time of
exhaustion is reported as a way to indicate the mixture in that particular water.
Finally, because the average influent concentration of TTH M influences adsorption
(Table 19), this information is also given. These data should help the reader select for
further study the reference citation of most interest. Combining data from different
locations  cannot be done reliably, but generally (Table 21), for typical  EBCT's,
service time to exhaustion is quite short.
  Finally, Blanck showed that at the Davenport, Iowa, water treatment plant nearly
80 percent breakthrough of TTHM occurred on or before 14 weeks of operation
(Table 22, page 78).66
  As  noted  earlier, if  some  effluent  concentration  less  than  the  influent
concentration, such  as the MCL for TTHM, is chosen as the target performance
criteria  for GAC adsorber, a  critical depth will be established. This  then is the
minimum design depth of the adsorber that will enable the target concentration to be
reached. To illustrate this, the chloroform data from Table 23 (page 78)s* arc plotted
in Figure 46 (page  79). Here, both the "service time to exhaustion" and the "service
time to some target less than exhaustion" (arbitrarily selected as 2 pg/ L for chloro-
form in this case) are positively correlated to bed depth or EBCT. The minimum bed
depth or critical depth to  remove the chloroform to the target concentration of 2
Mg/L is 49 cm (1.6 ft) for these data.
  Of course, the closer the target concentration  is to the exhaustion (influent)
concentration, the smaller is the minimum bed depth required to meet the target
concentration. Further, as shown in Figure  39, when measuring service time to
exhaustion, the target effluent concentration equalling the  influent concentration,
the critical depth is  zero.  The vertical distance in weeks between the two lines in
Figure  46 is  a measure  of the error in predicting  service  life if-equilibrium
(exhaustion)  studies are used, when the treatment target  is not exhaustion "but a
lower effluent chloroform concentration (2 //g/L in this case).
  Figure 47 (page  79)5' showing the "bed depth-service time" plots'18 for the four
trihalomethanes in Table 23 demonstrates that the more strongly adsorbed bromine-
containing trihalomethanes have a smaller critical bed depth, that is, a thinner mass
transfer zone. Waters in which the mixture of trihalomethanes is dominated by the
bromine-containing species might be effectively treated longer and with shallower
GAC  beds than waters containing predominantly chloroform.
•Nuchar* WV-G manufactured by Wesivaco Corporation, Covinglon. VA 24426. hereafter called WVG. When available the
 Msih si?e. e.g.. 12 » «. is included. Other types of GAC Mich m Nuct»r« WV-W are WVW.
'W1TCARB® Grade 950 manufactured by Wiico Chemical Corporation. Inorganic Specialties Division. New York, NY
 100!', hereafter called W950.


                 Section VI. Treatment Techniques to Remove Trihalomethanes 71

-------
•Q'
c
I
s
3'
o
I
I"
                                                                                   \          I        EMPTY BED
                                                                                         LEGEND   CONTACT TIME
                                                                — Flam Effluent
                                                                •••• 0,9 m (3 ft.) Depth
                                                                - 2.1 m (7 It.) Depth
                                                                — 3.4 m {11 ft.) Depth
                                                                — 4.6 m(15 ft. Depth
                                                                3.2 min
                                                                7.5 min
                                                               11,8 min
                                                               16.0 min
10/24     11/13
      1978
12/3      12/23      1/12       2/1       2/21


                        DATE OF SAMPLING
                                                                         3/13
                                                                                    4/2
4/22        5/12
      1979
                        Figure 44.   Removal of trihalomethanes by GAG at the Cincin-
                                    nati Water Works (OH), GAC type, WVG.30
             Continued

-------
                                               c
                                               o
                                               o
                                               3

                                               S
                                               '
Section VI. Treatment Techniques to Remove Trihalomethanes  73

-------
                                 100
S1
to


I


I

I
tn
O
§
9!
S"
3
a
  '
5-


-------
                TABLE 21. SUMMARY OF DATA ON ADSORPTION OF TOTAL TRIHALOMETHANES ON

                               VIRGIN GRANULAR ACTIVATED CARBON (GAC)
O)
a
i
I
•51

I
a>
I
Location
Cincinnati, OH
Cincinnati, OH
Cincinnati, OH
Cincinnati, OH
Mt, Clemens, Ml
Mt. Clemens, Ml
Miami, FL
Evansvilla, IN
Huntington, WV ,
Cincinnati, OH
Cincinnati, OH
Cincinnati, OH
Cincinnati, OH
Philadelphia, PA
Little Falls, NJ
Little Falls, NJ
Little Falls, NJ
Cincinnati, OH
Newport, Rl
Cincinnati, OH
Cincinnati, OH •
Evansville, IN
Cincinnati, OH
Type of
GAC
WVG12K40
, HD 10x30
WVG 12x40
Filtrasorb® 400
HD 3000"
HD 3000"
Filtrasorb® 400
HD 10x30
WVW 14x40
HD 10x30
WVG
WVG 20x50
WVG 12x40
UNK§
HD 10x30
WVW
Filtrasorb® 400
HD 10x30
Filtrasorb® 400
Filtrasorb® 200
WVG 12x40
HD 10x30
Filtrasorb® 400
Type of
system '
PC/PA§
.PC/PA
FS/SR§
PC/PA .
FS/SR
FS/SR
PC/ PA
PC/ PA
FS/SR
PC/PA
PC/PA
FS/SR
FS/SR
PC/ PA
FS/PA
FS/PA
FS/PA
PC/PA
PC/ PA
PC/ PA
PC/SR
PC/PA
PC/PA
iBCT
(minutes)
3.2
3.2
4.5
5
5.8
58
6.2
6.6
7.1
7.5
7.5
7.5
7.5
7.5
8
8
8
9
9
9
9.4
9.6
10
Influent TTHM
CI/Br Concentrationf
ratio'f (ffl/L)
2.3
1.9
2.3
2.3
4.4
4.6
1.8
13.2
11.3
2.9
3.8
4.1
2.3
INF§
12
52
12
3.0
6.1
6.3
3.4
19.9
2.3
50
71
51
121
22
25
156
0.7
145
31
31
51
51
80
91
123
91
44
111
54
57
0.7
97
Time to
Exhaustion}
(weeks) Ref.
5
4
22
6
13
12
12
3
7
8
8
22
22
9
14
13
14
9
10
9
22
-' 3
12
30
30
62
IH§
NR§
NR
59
63
18
30
30
62
62
58
65
65
65
IH
NR
IH
30
63
35
              Continued "•

-------
                TABLE 21. (Continued)
3

I

X1

I
•§'
c
a

-------
                        TABLE 21. (Continued)
05



3!
CD
5"
3
I
&
i
Location
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Jeff.
Parish,
Parish,
Parish,
Parish,
Parish,
Parish,
Parish,
Parish,
Parish,
Parish,
Parish,
LA
LA
LA
LA
LA
LA
LA
LA
LA
LA
LA
Type of
GAC
Filtrasorb® 400
Filtrasorb® 400
Filtrasorb® 400
VWG
Filtrasorb® 400
VWG
WVG
VWG
Filtrasorb® 400
WVG
Filtrasorb® 400
Type of
system
PC/PA
PC/SR
FS/SR
PC/PA
PC/PA
PC/PA
FS/PA
PC/PA
PC/PA
PC/PA
PC/PA
EBCT
(minutes)
21
21
21
22
22
25
26
32
.4
.6
.9
.1
.6
.3

.6
34.6
43
46
.S
.3
Influent TTHM
CI/Br Concentration!
ratio't Oig/L)
10.0
33.0
10.0
74.8
INF
9.0
20.8
88.8
INF
INF
INF
2.4
3
2
4
5
4
4
3
3
.8
.4
.3
.5
.4
.0
.0
.6
UNK
UNK
Time to
Exhaustion!
(weeks) Ref.
14
15
14
16
14
18
>25
26
18
>2S
>26
14
14
14
61
14
61
60
61
14
61
14
 tAI time of exhaustion.
 (Satvica tima until effluent concentration nearly equals influent concentration.
 §FS. Full ical*.
  IH, In-housA.
  jNF, Infinite, chloroform only preterit.
  NR. Not reported.
  PA, Po»t-fUtar ttltoriMr.
  PC, Pilot column.
  SR, Sand replacement.
  UNK. Unknown.
"Manufactured by ICI America Inc., Atlas Chemical! Divhion, Wilmington, Oi 19899.
ttFowign.
    t commercially availabta.

-------
  TABLE 22. REMOVAL OF TRIHALOMETHANES AT DAVENPORT,
        IOWA, BY GRANULAR ACTIVATED CARBON (GAG)66
Age of GAC
(weeks)
14
18
22
TTHM (/
Influent
152
93
71.
"g/U
Effluent
120
97
62
Percent
removal
21
-4
13
 TABLE 23, REMOVAL OF TRIHALOMETHANES IN MIAMI, FLORIDA,
   WATER BY GRANULAR ACTIVATED CARBON* ADSORPTION'9
Compound
CHCI,



CHBrCI,



CHBr,Cl



CHBr,



Bed
m
0.8
1.5
2.3
3.0
0.8
1.5
2.3
3.0
0.8
1.5
2.3
3.0
0.8
1.5
2.3
3.0
depth
ft
2.5
5.0
7.5
10.0
2.5
5.0
7.5
10.0
2.5
5.0
7.5
10.0
2.5
5.0
7.6
10.0
Average
influent
EBCT concentration
(minutes) (ttg/t.)
6.2
12
19
25
6.2
12
19
25
6.2
12
19
25
6.2
12
19
25
67
67
67
67
47
47
47
47
34
34
34
34
2.5
2.5
, 2.5
2.5
Time to
2 Mg/L
breakthrough
(weeks)
1.1
4.1
7.0
10.3
2.0
6.0
10.4
15.0
3.0
8.4
14.0
CE
6.0
13.0
CE
CE
Time to
exhaustion!
(weeks)
3.4
7.0
10.9
14.0-
8.0
14.0
19.9
CE*
14.4
24.8
CE
CE
13.4
CE
CE
CE
 •Filtr.iorb J 400.
 tSometlmam predicted by extrapolation.
 $Gartnot axtrapolata.
 1 Finally, in a GAC adsorption bed, EBCT is influenced both by bed depth and
approach  velocity. Therefore, various combinations  of these two factors can
produce the same EBCT. Figure 48 illustrates a study where both the flow rate and
GAC dtpth were manipulated to give a constant EBCT. These'data show that, in this
case, the various combinations of approach velocity and bed depth that produced a
9- or 18-minute EBCT resulted in the same chloroform breakthrough pattern. This
may not be extrapolated to extremes, however. When a very shallow bed depth and a
very slow approach velocity are used a reasonable EBCT might result, but because
the  size of the resulting critical depth may be too large under these operating
conditions, a low target concentration may not be reached.

  Discussion—Using equilibrium adsorption isotherms to predict service time to
exhaustion, as in Table 18, is based on several assumptions. Neglecting competitive
adsorption, this approach assumes that the adsorber.column performance is as

 78  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
o.


DC
LU
       o    i
                                                  8.9    10
                       1                2

                           BED DEPTH, m
       05         10         IS         20         25

                   EMPTY BED CONTACT TIME, min


   Figure 46.   Bed depth-service times for the removal of chloro-

               form in Miami, FL, water by GAC.*9
    14
    12 --
    10 - -
     8 - -
LJJ



P

LU
zz    6 ~ ~
K
UJ
to
     2 - -
                           BED DEPTH, ft
                           BED DEPTH, m
   Figure 47.   Bed depth-service times*8 to reach 2 jig/L in the ef-
               fluent for the trihalomethanes being adsorbed by
               GAG."-*7


         Sect/on VI. Treatment Techniques to Remove Trihalomethanes  79

-------
      100-
       80 - -
    o
    uj
    O
    O
    o
60
       40
       2O
      -20
                                  I   I  I  I
                                              2,5 m/hi
                                               (1 gpm/d«)
                                                O.9 m 136 in.)
                                          \
10 m/hf
(< gpm/lt*l
 1.8m (72 in.)   \ \
                                     . V*
                                     \ x
                                                  12 flom/ll'I
                                                   1.8 m(72 in,)
                                                50% Effeclive
                                                (CHCI,*12jig/L)
                                        II
                                        e C
                   X
                               10         15         20

                             TIME IN OPERATION, wk
                                                               25
  Figure 48.
                     Effect of empty bed contact time on chloroform ad-
                     sorption on GAC using Cincinnati, OH, tap water.
                     Average applied chloroform concentration, 24fig/L;
                     GAC type, Filtrasorb® 400.
shown in the "ideal case" (Figure 49). In the ideal case, theshaded area represents the
loading on the adsorbent at exhaustion and should equal the equilibrium loading or
capacity for that influent contaminant concentration.
  The "typical case" in Figure 49 is what occurs in practice. The total quantity of
adsorbed contaminant is "Area A 4-  B +  C," and the predicted time in service to
exhaustion using equilibrium data would be calculated such that "Area B" equals
"Area A," This predicted time might be quite different from the actual exhaustion
time, depending on the shape of the influent concentration and breakthrough curves.
             TYPICAL CASE
                                          IDEAL CASE
         Figure 49.  Comparison of ideal and typical GAC adsorber per-
                     formance.
80  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
  In their work in Miami, FL, Wood and DeMarco calculated "Area A + C"to
determine the GAC loading at exhaustion.5* Although different activated carbons
were used and other factors such as water quality were different, these data were
compared with those determined by Dobbs and Cohen51 (Table 24). As expected,
loadings calculated from isotherm data were similar, but not the same as those
observed for the GAC columns.

   TABLE 24. COMPARISON OF ADSORPTION ISOTHERM DATA61
       WITH GRANULAR ACTIVATED CARBON (GAC) COLUMN
                ADSORPTION DATA AT EXHAUSTION69


Constituent
CHCia
CHBrCla
CHBr3CI
Influent
concentration
ifS/l)
67
47
34
Isotherm
loading*
(mg/g)
0.35
1,2
1.4
GAC column
loading!
(mg/fl)
0.67
O.83
1.0
 •From Figure 29".
 tFrom Reference 69; bed depth = 1.6 m (6 ft); EBCT = 12 minutet.

Furthermore (referring to Figure 41), with an influent chloroform concentration of
about 50 /ig/ L, a 9-minute EBCT, and a 5 m/ hr (2 gpm/ ft2) approach velocity, use of
the adsorption isotherm illustrated in Figure 28 would indicate a time in service to
exhaustion of 2.6 weeks, whereas exhaustion actually occurred after 8 or 9 weeks of
operation.  The effects on  treatment  effectiveness caused  by competition  for
adsorption sites with other organic species, as well as the difficulty in selecting the
service time corresponding to "true" exhaustion when the influent concentration is
highly variable, can also contribute to the disagreement between predicted and
actual service times to exhaustion.
  Finally, calculating service times  to exhaustion from the adsorption  isotherms
(Figure 29) also shows that EBCT, contaminant influent concentration, and fraction
of TTHM's that contain bromine all influence the service life to exhaustion (Table
19). The data  in  Table 21  show the  influence  of these  three  factors on  the
performance of GAC adsorbers.
  Thus,  the data in Tables 18  and  19 calculated  from adsorption isotherms  are
instructive on a relative basis, but cannot be used to accurately predict GAC column
service times. Isotherms may be used at a location to indicate the feasibility of GAC
treatment,  but  pilot studies  will always be needed to  accurately predict GAC
adsorber performance.  The data in Table 21 also show that, generally, except for
very long EBCT,  service life to exhaustion is short for GAC adsorbers  removing
TTHM. Therefore, GAC for TH M removal alone may not be recommended partly
because of the high reactivation frequency  required. However, if other synthetic
organic  contaminants  are  diagnosed  to be a problem,  then GAC  might be
appropriate for removing both  these and THM's. GAC  may be considered more
applicable  for  precursor removal  (especially prior to  chlorination) where  the
required  reactivation frequency may be less, to be discussed under Section VII of this
report.

Synthetic Resins—
  General Considerations—As  alternatives to using PAC or GAC, the ability of
several synthetic resins to absorb TTHM has been evaluated.
  Experimental  Results—Ambersorb®  XE-340 *—Ambersorb®  XE-340   was
specifically  designed  to adsorb lower molecular  weight  halogenated organic
compounds.! Cincinnati tap water containing trihalomethanes was passed through
•Ambersorb* XE-340 manufactured by Rohm & Haas Company, Philadelphia, FA  1910S.
t Another advantage claimed by the manufacturer is the ability la regenerate this material in-plaee by steaming.
                 Section VI. Treatment Techniques to Remove Trihalomethanes 81

-------
 a 3.7-cm (l,5-in) diameter, glass pilot column containing 81 cm (32 in) of the resin.
 At an approach velocity of 5 m/hr (2 gprn/ff1), a 10-minute EBCT resulted. The
 previously unpublished data in Figure 50 show that  TTHM's were  still being
 removed after 40 weeks. According to Table 21 GAC  systems with a 10-minute
 EBCT were exhausted forTTHM removal after 12 to 15 weeks. Thus the synthetic
 resin appeared in this case to be significantly more effective than granular activated
 carbon forTHM removal.
      150
           0      5     10     15     20     25     30

                            TIME IN OPERATION, wk

          Figure BO. Removal of trihalomethanes by Ambersorb® XE-340;
                    EBCT, 10 min.

   Studies in Miami, FL, confirm the capacity of Ambersorb® XE-340 to remove
trihalomethanes (Table 25).5* As with GAC (Table 23), the time for this resin to reach
exhaustion  is  longer for the  bromine-containing trihalomethanes  than  for
chloroform.
   The comparison of trihalomethane loadings on the two adsorbents at similar
Influent concentrations (Table 26) shows the increased adsorption capabilities for
the Ambersorb® XE-340.
   Between February 1977 and March 1979, the American Water Works Association
Research Foundation, along with the University of Missouri, Iowa State University,
and the University of Illinois, conducted pilot scale adsorption studies at the Kansas
City,  Missouri, Water Treatment Plant.64  There, Missouri River water receives
coagulants, lime for softening, settling, filtration, and approximately 6 hours of free
chlorine contact time before ammonia is added to ensure a combined residual. Pilot
scale adsorption units (described in detail in Reference 64) were installed following
filtration. They were 15-cm (6-in) diameter glass columns containing 0.9 m to 2.7 m
(3 ft to 9 ft) of adsorbent. Over a 2-year period, Ambersorb® XE-340 was examined
for its effectiveness for removing trihalomethanes.  Variations in the trihalomethane
concentrations  in  the  applied water makes selecting  an  absolute  time  for
breakthrough (effluent >10 percent of influent) and exhaustion difficult; however,
Ambersorb* XE-340 effectively removed trihalomethanes, exhibited a very gradual

82  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
 TABLE 25. REMOVAL OF TRIHALOMETHANES IN MIAMI, FLORIDA,
                       BY SYNTHETIC RESIN*69
 Compound
  Average
  influent
concentration
   teg/t)
  Time to
  2 p.g/\-
breakthrough
  (weeks)
 Time to
exhaustionf
 (weeks)
 CHCI,
 CHBrCI,
 CHBr,CI
 CHBr,
     80
     69
     64

     37
     43
     42

     12
     25
     27
      1.9
      3
      3
      0

    20
    20
    22

    47
    45
    25

    63
   156
   150
   150

   216
   210
   CEt

   26O
   26O
   CE

   CE
 •Ambaraarfce XE-34O; EBCT = 6.2 minutei; bad depth = 0.8 m (2.5 ft).
 tSomatimoi pr«dlct*d by «Ktr«pol«tion.
  TABLE 26. COMPARISON OF GRANULAR ACTIVATED CARBON
     (GAC) (F-400) AND AMBERSORB® XE-340 COLUMN DATA
                         AT EXHAUSTION*89




Constituent
CHCI,
CHBrCI,
CHBr,CI


Influentf
concentration
(^9/U
67
47
34

GAC
column
loading
(mg/g)
0.53
0.84
1.0


Influent
concentration
(M9/U
69
43
25
Ambersorb®
XE-340
column
loading
(mg/g)
2.2
2.0
1.6
 •EBCT = 6.2 minutes; bud d»pth = 0,8 m (2.6 ft).
 tSaa Table 23.

breakthrough curve, and, thereby, yielded a long service life. Although effective, like
any adsorbent that is  not used on  a one-time basis, Ambersorb® XE-340 must be
regenerated when saturated with adsorbate. Also, adsorption of trihalomethanes on
Ambersorb® XE-340  is a reversible process, and these materials will desorb if the
influent concentration' declines. This is shown in Figure 51 where chloroform-free
water was passed over a bed of Ambersorb® XE-340  that had previously been
exhausted for  chloroform  removal.  Under these circumstances, the expected
desqrption occurred.59

  Other Resins — Although the trihalomethanes are neutral species, strong and weak
base anion exchange resins were investigated to determine their capacities to remove
trihalomethanes as a part of other investigations. The strong base anion exchange
resin  Amberlite® IRA-904,  manufactured  by the  Rohm & Haas  Company,
Philadelphia, PA 19105,  was studied at both Miami, FL,$» and Kansas City, MO;*4
the weak base  anion exchange resin ES-561, manufactured  by the Diamond
                Section VI. Treatment Techniques to Remove Trihalomethanes  83

-------
                            Effluent
                            From
                            Previously
                            Loaded
                            Column
                                        Influent to
                                        Previously
                                        Loaded
                                        Column
                          20      30      40      SO

                           TIME IN OPERATION, day

            Figure 61.  Desorption of chloroform from Ambersorb®XG-340;
                       EBCT, 6.2 rnin."
Shamrock Corporation, 800 Chester Street, Redwood City, CA 94064, was tested at
Kansas  City,  MO." As expected, these resins were  not useful for removing
trihalomethancs.

  Discussion—Of the synthetic resins tested only Ambersorb®  XE-340, the one
specifically designed by the manufacturer to have high adsorptive capacity for low
molecular weight halogenated compounds, showed promise. In parallel experiments
loadings on this resin were greater than those on OAC. Although this resin has been
regenerated by steaming in the laboratory, as claimed  by  the manufacturer, the
scaleup to full plant size is still being developed, and this resin ia not available in
commercial quantities.
Summary of Using Trihalomethane Removal as an Approach to
Trihalomethane Control

Advantages of Trihalomethane Removal—
  As a treatment approach, removal of trihalomethanes has some advantages. The
more Important are that the water utility would not need to change its disinfection
practices and the treatment is targeted to the regulated eontaminant.iChlorination, a
process in which many designers and operators have confidence, could continue to
be used as a disinfection process, with the resulting trihalomethanes being removed
by some unit process  added to the treatment  train. The flexibility  to  permit
noncentral treatment of the finished water may also prove to be advantageous.

84  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
 Disadvantages of Trihalomethane Removal—

   Other  Organic  Disinfection  Byproducts—To  evaluate  one disadvantage of
 maintaining chlorination practice  and treating the trihalomethanes formed, the
 behavior of the other disinfection byproducts formed during disinfection with free
 chlorine must be understood. Recall that the reaction of free chlorine and precursors
 is:

                                                               OTHER
                 PRECURSORS                               HALOGENATED
   FREE    + (HUMIC SUBSTANCES) -  TRIHALOMETHANES +  „„       ®,  •„*
CHLORINE      AND BROMIDE                            NONH ALOGENA TED
                                                              OXIDIZED
                                                            BYPRODUCTS

As indicated  by  this reaction,  during free  chlorination, other  halogenated
byproducts result. Most of these byproducts cannot be measured individually by gas
chromatographic techniques, but they can  be estimated as  a group, as "organic
halogen" (OX). Although not perfect, this test70 is useful for evaluating the behavior
of nontrihalomethane halogenated  byproducts during  any proposed  treatment
scheme. Although the health significance of these halogenated byproducts has not
been fully evaluated," these byproducts should be viewed  with suspicion.  (The
nature of these other chlorination  byproducts is discussed  in the subsection on
Disinfection Byproducts in Section VIII.)
  Therefore, one disadvantage of a treatment approach, the objective of which is to
remove trihalomethanes after formation, is that other disinfection byproducts may
not be removed by the treatment process.  Although the concentration of these
compounds is not now subject to regulation,  minimizing their concentration, where
possible, would be prudent.
  Further, because chlorine  is an oxidant, the possibility of producing oxidation
byproducts during chlorination also exists (note the reaction above). At the present
time,  few of these oxidation byproducts can be measured,  but their toxicologic
significance  is  being evaluated.

  Lack of Precursor Removal—As mentioned earlier in this report, because the
formation of trihalomethanes is not instantaneous, their concentrations increase in
the water as it flows to the consumer. This is the second disadvantage of a treatment
strategy based on the removal of trihalomethanes only. The precursor remaining in
the water will  react with any free chlorine present and more trihalomethanes will
form after the trihalomethane treatment step.
  For example, during an aeration study (see Table 9), chloroform was removed at
higher air-to-water ratios, but the chloroform formation  potential was not (Figure
52). The chloroform concentration did decline during aeration, but because of the
lack of precursor  removal, the chloroform  concentration reaching the consumer
would be higher than that measured in the effluent of the treatment unit process.
Some benefit would be gained, however, as I nstTH M concentrations would be lower
at any point in the distribution system after aeration treatment than it would be
before treatment. The adsorptive treatment techniques covered in this section also
have an incidental precursor  removal function that is more completely explained in
Section VII. Avoiding post-treatment  trihalomethane formation by converting all
precursors into trihalomethanes before aeration is not  practical because of the
chlorination byproducts that would be formed and probably not removed during
aeration and because of the typically slow trihalomethane formation rate.
                Section VI. Treatment Techniques to Remove Trihalomethanes  85

-------
                                            InstCHCI, Concentration
                                            After Aeration
                                            Rechtorination and 2 Days Storage
                                            @ 25°C (77°F). Chloroform
                                            Formation Potential
                             1:1        4:1        8:1       16:1

                                AIR/WATER RATIO (V/V)
                                                                    20,1
           Figure B2.  Removal  of chloroform from Cincinnati, OH, tap
                     . water by aeration.
SG  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                             SECTION VII
             TREATMENT TECHNIQUES TO REMOVE
          TRIHALOMETHANE PRECURSORS (THMFP)

   Because trihalomethanes  are  formed when free  chlorine is  added to water
containing trihalomethane precursors, one approach to lowering TTHM concen-
trations would be removal of the precursors. This section examines this approach in
detail by discussing eight techniques for removing trihalomethane precursors from
drinking water-—clarification, source control, aeration, oxidation, adsorption, ion
exchange, biologic degradation, and lowering  of pH.
   Trihalomethane precursors are measured by the trihalomethanes that are formed
upon chlorination  and storage. But the resulting measurements may be influenced
greatly  by variations in test  conditions  (storage time,  temperature, pH,  and
trihalomethane species measured) among the locations reporting data. Thus the
results presented in this section will be influenced by the vary ing test conditions in an
unknown way. For example, two locations with the same type and quantity of pre-
cursor could report different THMFP's if the TermTHM tests were performed under
different conditions.
   In addition, in many experimental plant evaluations reported here, the conditions
of the TermTH M test were selected and known to be somewhat different from those
existing in that utility's  distribution system. Thus in these cases, the  TermTHM
concentrations reported should not be considered to reflect actual concentrations of
trihalomethanes reaching the consumer.  Because of these test variables, precursor
test conditions and rationales for their selection will be stated wherever possible to
facilitate comparisons of data.
   As  discussed earlier in the "Measurement" Section, another  consideration  is
selecting units of expression of trihalomethane concentration. This is an especially
important consideration when the investigator is interpreting precursor removal
data. Although, for a given amount of precursor present, observed molar yields of
trihalomethanes  after bromination are generally higher than when chlorination
alone is practiced, this result is likely to be a reaction rate phenomenon, and the
actual number of potential reactive sites (chemical equivalents) available is probably
similar regardless  of the attacking  halogen species. So because trihalomethane
precursors are measured" by chlorinating a sample and analyzing the trihalomethanes
produced, any summation should theoretically be made on a molar basis. Such a
summation would allow the most accurate comparison of precursor concentrations
(number of active sites) in various samples tested, because this measure is unbiased
by the differing molecular  weights of the trihalomethanes formed  in varying
mixtures.
   Again, however, because the Trihalomethane Regulation3 is based  on TTHM
summed on a weight basis (/tg/ L),the data will usually be reported in terms of jig/ L
THMFP rather than (or in addition to) the more chemically meaningful ^mol/L,
Major exceptions  to this are the Subsections  Powdered  Activated Carbon  and
Granular Activated Carbon (General Considerations), where adsorption isotherms
of TTHM's are  discussed on a  micromolar basis only. These exceptions were
considered necessary because of the  variable relative yields of the trihalomethane
species observed when different amounts of precursor were chlorinated under the
same  test conditions. The differing molecular weights of  these species would
influence the shape of THMFP adsorption isotherm curves if the summations were

      Section VII. Treatment Techniques to Remove Trihalomethane Precursors  87

-------
 made on a fig/L basis. The units reported in the cited literature vary, and reference
 should be made to the respective sources for data when individual species or TTH M
 data expressed in molar units are desired and not included here.
Clarification (Including Moving the Point of Chlorine Application)

 General Considerations—
   The American Water Works Association Research Committee on Coagulation
 has provided an excellent summary of the general subject of organics removal by
 coagulation,72 The Committee recognized that although coagulation is most often
 considered a treatment technique for turbidity reduction, the process plays a very
 significant role in organics removal at the same time. This role occurs both because
 some organic materials are probably adsorbed on suspended particles (turbidity)
 and because direct interactions of the natural huraic materials (usually recognized as
 color) take place with the coagulants themselves. Several reports have documented
 the stoichiometric relationship between the precipitated humic  materials and
 coagulants.11'74*'5 The Committee report72 concludes that both iron  salts and alum
 are effective for removing humic  and  fulvic acids from water, and that cationic
 polymers that interact with theanionic humates can also play a useful role as coagu-
 lants for organics  removal. Doses  required depend on both the amount of humic
 material present and the pH. The pH affects both the precipitation of the coagulant
 and the stoichiometry of the coagulant-humate interaction by way of protonation of
 the humate itself. Removal of organics by coagulation is best under slightly acidic
 conditions, pH 4 to 6.
   Iron or aluminum salts, calcium  hydroxide (if softening is  also a  goal), and
 polymers are commonly used coagulants in different types of water treatment plants
 designed to remove color and turbidity. Thus the study of these coagulants for the
 removal of trihalomethane precursors was logical  because a major fraction of
 trihalomethane precursors are humic and fulvic acids that cause natural color.

   Early Experiments with Clarification Processes for Precursor Removal—Early in
the USEPA in-house studies, samples were collected  before and after the various
unit processes within  a conventionally operated pilot plant and analyzed for nori-
purgeable organic carbon (NPOC) concentrations. Although removals vary, the
relative results (Figure 53) are fairly typical and generally as expected, because
similar results have been reported in the NORS7 and subsequently demonstrated in
another full-scale  water  treatment  plant.76  In  these  studies,  coagulation,
fiocculation,  and sedimentation had a  marked effect on  the general  NPOC
concentration—approximately a 60  percent reduction. Kavanaugh77  also  cited
similar data from other literature.
  To determine whether or not trihalomethane precursors were removed in a similar
manner during conventional treatment, samples of source water, coagulated and
settled water, and dual-media-filtered water from the  USEPA pilot plant were
chlorinated in closed  containers to determine the production pattern of trihalo-
methanes (Figure 54A). These experiments revealed that the pattern for lowering the
chloroform formation potential  paralleled the general  decline of NPOC for the
various qualities of water (Figure 54B). This conventional treatment, however, had
relatively much  less effect  on preventing the formation of bromine-containing
inhalomethanes (Figure 54B).  The reason is probably that bromide is not signifi-
cantly affected by coagulation and remains available for oxidation to the active
bromine species, which then effectively competes with chlorine in the trihalomethane
formation reaction with the precursor that remains after clarification.
  Work by Semmens7* and Babcock and Singer7' on coagulation also revealed
important  information about  the  potential  of' this  process   for   removing
trihalomethane precursors. Semmens showed that  up  to 65  percent precursor

S3  Treatment Techniques for Controlling  Trihatomethanes In Drinking Water

-------
             1.0 --
           o
           20,75.
           O
           u
           o
           D_
           z
           nj 0.5'
             0.25
                       Source Water
Coagula-
tion And
Sedimenta-
tion Basin
Efflueni
                                                   Dual-Media
                                                   Filter
                                                   Efflueni
                               STAGE OF TREATMENT

           Figure 53.  Relative NPOC removal during water treatment in a
                      pilot plant. Source water NPOC concentration rang*,
                      2.2-3.9 mg/L.

removal occurred for a dose of 100 mg/L alum in reconstituted Mississippi River
water at a pH range of 5.0 to 5.5, The removal of trihalomethane precursors followed
the same trend as TOC and ultra-violet absorbance removal, but the relative slopes
of the various removal curves were somewhat different.
  Babcock and Singer" showed that  about 80 to 90 percent of humic acid, and
approximately 20 to 39 percent of fulvic acid (both with a starting concentration of
10 mg/ L TOC) could be removed by the addition of 100 mg/ L alum at pH 5.0. In a
second series of tests, they found that a residual of 1.4 mg/L humic acid TOC
(starting with 10 mg/L humic acid and 50 mg/L alum)  was capable of producing
about 100 fig/L of chloroform within a  48-hour chlorination time. Furthermore,
they found that a residual of 7,8 mg/ L fulvic acid TOC (starting with 10 mg/ L fulvic
acid TOC and 100 mg/L alum) was also capable of producing approximately 100
fig/L chloroform during a  48-hour  chlorination time.   Thus the  yield  of
trihalomethanes from residual TOC  may vary significantly, indicating that  the
success of coagulation for  precursor removal is likely to be highly variable. Both of
these investigators showed that  the potential  for  removing  trihalomethane
precursors by coagulation and settling may be enhanced by carrying out this process
at a lower pH,

  Anticipating Success of Clarification for Precursor Removal—Successful trihalo-
methane control can be measured in two ways: 1) by a low finished waterTermTHM
(precursor)  concentration, which affects the trihalomethanes  formed  during
distribution, and 2) by a low finished water InstTHM concentration, which will
benefit consumers to  a varying degree, depending on their distance from the plant.
Either of these results from a unit process will benefit the consumer.
  At existing plants already  employing clarification  unit  process(es),  only  a
laboratory analysis is needed to  mca.sure TermTHM reductions through the unit
processes ("Amount B"and "Amount B'" in Figure 55, page 92). The magnitude of
these reductions is often quite significant.  Efforts can then be made to improve plant
performance for  increasing the  removal of precursor by modification of pH,
coagulant dose, or changing the coagulant used.

      Section VII. Treatment Techniques to Remove Trihalomethane Precursors  89

-------
1
!
i
§
                                                       60
                            40      80      120

                             REACTIONTIME.hr
                                                                   I        1        \
                                                              — Untreated Ohio Rivsr Water
                                                            -o- Coagulated And Settled Water
                                                            -*- Dual-Medin-Filtered Water
                                                   160
40      80     120

 REACTION TIME, hr
                                                                                         160
40      80      120

 REACTION TIME, hr
                                                                                                                                160
a'
D
I
                                           Figure 54.   THMFP and NPOC in various qualities of water.

                                                       A. Production of trihatomethanes in  chlorinated
                                                         water samples of various qualities. Storage condi-
                                                         tions: pH 7,4; 25°C(77°F); 5 mfl/L chlorine dose.
             Continued

-------
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o
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1H InstTHM





reatmen
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i






















D THMFP
rH+iH TormTHM
B

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UJ
BC
   1.0 --
  0.5
              M
  .-» Q;
f*3?'  T»!
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-------
   For example, when conditions involve a fast reaction rate (Figure 56A), the
formation of trihalomethanes is delayed when the point of chlorination is moved
from  R to  M {routine to  modified); but  no difference  in  trihalomethane
concentrations occurs at any point in the distribution system. The concentrations C,
and Cm are equal, and so are Q and Cr'. U nder the more typical reaction conditions in
Figure 56B, some improvement can be noticed (Cr - Cm) at the entrance to the distri-
bution system. The magnitude of this benefit decreases with time to a minimum
(Cr - CrO at the end of the distribution system.
   In the presentation of data from operating water treatment plants that follows, the
absolute effectiveness of clarification for precursor removal, B'/( A+B+C), as well as
various unit process changes (including moving the point of chlorination) will be
discussed together, as they are so closely related.

Experimental Results—

   Coagulaiion-Sedimentation-Filtraiion—Ohio River Valley Water Sanitation
Commission  (ORSANCO)  Results—Field studies  conducted   by ORSANCO
measured the removal of precursor at  10 water utilities treating  river water with
various combinations of coagulation, settling, and filtration.'* In this study, samples
collected for determination of TermTHM were buffered to  the finished water pH,
received an additional IS mg/L  chlorine, and  were stored for 7  days at ambient
temperature.  Unpublished rate curves suggested that these conditions were sufficient
to complete the trihalomethane reaction so that changes in precursor concentration.
through a treatment process could be assessed. The curves also suggested, however,
that these conditions would produce a finished water TermTHM  concentration
higher than would  be found at the extremities of a 3-day distribution system'
maintaining a minimal free chlorine residual—the ambient  conditions at many of
these utilities. Therefore, the TermTHM concentrations do not reflect the actual
quality of Uie consumer's drinking water even though the removal comparisons were
possible.                                                                   -
  The effectiveness of clarification as" a process for trihalomethane precursor
removal is demonstrated by data for the 10 locations (Table 11), which show that an
average of 29 to 51 percent of the Ohio River source water precursor was removed by
the treatment plants.
  Three utilities—the Cincinnati Water Works, the Pittsburgh  Department  of
Water,  and the Wheeling Water Department—were selected for more detailed
investigations. Two-week studies  were made of trihalomethane precursor removal
by individual  unit processes in the treatment plant and of the effects of moving the
chlorine application point further into the treatment process to allow clarification to
reduce precursor concentrations before chlorination. An  attempt was made to
follow the InstTHM and TermTHM concentrations in a plug of water from the
source through the clearwell, but not into the distribution system.
  In each of these three locations, the removal of trihalomethane precursor occurred
during the first unit process where a coagulant was added (Table 28, page 97). Little,
if any, further removal occurred in the remaining unit processes in the treatment
plant.
  The Cincinnati, OH, results of moving the point of chlorination to later in the
treatment train (Figure 57, page 97) show that a significant difference in source water
precursor  levels was observed between the two treatment periods (routine and
modified, or delayed chlorination). At least a 39-perceni'deerease  in TTHM's was
noted for the source water during modified treatment. In this study, the fraction
B/( A + B + C) (Figure55) during routine operation was at least 0.34, and the fraction
C/(C + A) was 0.26 in the settled water (Figure 57), These data show that a slightly
higher percentage of the source water TermTHM concentration was present in the
finished water during the modified mode of treatment, indicating  that moving the
point of chlorination  from the off-stream reservoir effluent to the settling basin

94  Treatment Techniques for .Controlling Trihalomethanes in Drinking Water

-------
                            TABLE 27. SUMMARY OF PRECURSOR REMOVAL DATA AT
                                       FULL-SCALE TREATMENT PLANTS18
>»*
1.
§
^
a
a
a
3
51
n
f
t
8
s
8
3
o
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2
8.
3
»
3-
a>
-o
-^
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o
(~
Location
Huntington. WV

Fox Chapel. PA


Wilkinsburg-
Pennsylvania
Joint Water
Authority, PA
Evansville, IN


Pittsburgh. PA

Western Pennsylvania
Water Co., Hays Mine
Plant
Beaver Falls, PA


Wheeling, WV
Treatment
Coagulation, sedimentation.
2- to 3-yr-old GAC
Coagulation, 2-stage
sedimentation, filtration

Coagulation, 2-stage
sedimentation, filtration


Coagulation, sedimentation.
filtration

Coagulation, 2-stage
sedimentation, filtration
Coagulation, 2-stage
sedimentation, 2- to 3-yr-old
GAC
Coagulation, 2-stage
. sedimentation, filtration

Gravity sedimentation.
Mean* fraction of
precursor removal
BY(A + B + CJt
during routine treatment

0.29

0.49


0.38



0.36


0.38


0.35

0.33


Number
of
tests

10

12


10



11


11


8

10


                                   coagulation, sedimentation,
                                   filtration
                                                        0.30
to
cn
Continued

-------
 to
 O)
 s

 i?
 o
 o
 a
                     TABLE 27.  (Continued)
Location
Cincinnati, OH
Louisville, KY
Treatment
48-hr reservoir settling
w/alum, coagulation,
sedimentation, filtration
22-hr reservoir settling.
Mean* fraction of
precursor removal
BV(A + B + C)t
during routine treatment
0,51
Number
of
tests
10
                                                   coagulation, 2-stage

                                                   sedimentation, filtration
0.28
11
I
ro
if,

3'
S-'

I'
                      "Monthly raw and finlihsd samples.

                      tFrom Figure 56. Storage conditions: Buffer to finished water pH, 16 mg/L chlorine added, 7-day storage.

-------
TABLE 28. SUMMARY OF PRECURSOR REMOVAL THROUGH THREE
                     WATER TREATMENT PLANTS18


                                                             Mean*
                                                          % removal of
                                                        TermTHMf from
                                                        source to effluent
Location
Cincinnati, OH



Pittsburgh, PA


Wheeling, WV


Treatment
48-hr reservoir
settling with alum
Coagulation, settling
Sand filtration
Coagulation, clarification
Settling
Sand filtration
1-hr gravity settling
Coagulation, settling
Sand filtration
of given treatment

32
43$
30
29
19*
27
0
18
18
Two-week study.
f Buff or to fini«hfld water pH, IS mg/L chlorine added, 7-day storage, ambient temperature.
{May have been influenced by analytic error.
, 	 Routine (?;•»* . . TTLtKA Routine
O Treatment • lnst TTHM Treatment




L-






£508 . f— ] THMFP !>66% of Control)
CMH Term TTHM 338
Modified


— *-»






Treatment Routine
>309 Treatment
291
"o
8

77


~


=

I
i
Modified .
Treatment
(~

106






rr



W
w
^




232





i
tzZz




65


Rot
SOURCE
WATER
jtine

1
RESERVOIR
SETTLED
WATiB


r
SETTLED
WATER



FILTERED
WATER



FINISHED
WATiR

Treatment 48 mg/L PAC a 8 mg/L PAC
i 3,6 rag/L CI,
     Modified     |
     Treatment 4.8 mj/L PAC
                           4_8 mg/L PAC
                                        3,3 mg/L CI,
         Figure 57.  Trihalorhethane  formation (mean values)  during
                     routine and modified  (delayed chlorination) treat-
                     ment at the Cincinnati Water Works (OH), (October
                     1977, 560,000-mVday[150-mgd]capacity,}THMFP
                     conditions: pH 8.4; 19  to 25°C (66 to 77°F); storage
                     time, 7 days."

      Section VII. Treatment Techniques to Remove Trihalomethane Precursors  97

-------
effluent had little influence. On the other hand, the finished water InstTHM concen-
tration declined 41  pg/L (39 percent), partly because the lower concentration of
precursor at the time of the experiment was slowing the reaction rate. This decline
benefited consumers  near the water treatment plant, but  additional precursor
removal did not occur.
  In the Pittsburgh, PA, study, the fraction B/(A + B + C) (Figure 55) during
routine  operation  was 0.26, and the  fraction C/(C + A)  was  0.05  in the
coagulated/clarified effluent (Figure  58). The data in Figure 58 show  that the
finished  water TermTHM concentration did not decline, but actually rose about 2
percent during the  test  period. The InstTHM concentration in the finished water
declined 30 pg/ L (54 percent), however—a benefit to nearby consumers. The benefit
of  additional  precursor  removal did not  occur  as a  result of  changing the
chlorination  point. Note  that  in  this  study, the source water  TermTHM
concentration declined very little (about 6 percent)  during the period of modified
operation in contrast to the Cincinnati, OH,  results reported above. So in this case,
the decline in InstTHM concentration cannot be attributed to a lower source water
precursor concentration.
  The Wheeling, WV, study used the same  technique as described above. During
routine  operation,  the  fraction  of TermTHM   that  was  removed  in the
coagulation/settling basin wasO. 18, and the fraction of THMFP that was converted
to  InstTHM during  that unit  process was 0.23  (Figure 59). During  modified
       275
           Routine
           Treatment
              Modified
              Treatment
                                O+i
gUJ InstTHM

I   I THMFP

    TermTHM
                    196 Routine
                       Treatment
Modified
Treatment
(81% of Control!
                        203
                                                   Routine
                                                   Treatment
                                                   (74% of Control!
                                                             56
                        10
                                                                      26


SOURCE
WATER

r
COAGULATED AND
CLARIFIED WATER


SETTLED
WATER


FILTERED
WATER

i
1
Routine 1
TrBstment i .2 ma't ci,

FINISHED
WATER



0,4 my/I PAC 2A mg/L CI,
    Modified
    Treatment  4,3 mg/L PAC
                            0.5 mg/LCI,
                                                       2.7 mg/L CI,
         Figure 88.   Trihalomethane formation (mean  values) during
                     routine and modified {delayed chlorination) treat-
                     ment at the Pittsburgh Department of Water (PA).
                     (October  1978,  228,000-mVd [60-mgd] capacity.)
                     THMFP conditions: pH 8.3; 17 to 23°C (63 to 73°F);
                     storage time, 7 days.18

 98  Treatment Techniques for Controlling Trihatomethanes in Drinking Water

-------






_l
%
.
o
o
o
5
X
J™.
zr
s
s


369 Routine lili InstTHM Modified
325









^—~ J





^









«^x—





x Treatment i 	 i TMMPP Treatment
1 	 ' lnnnrr (88% of Control]
CZH-H TermTHM
Modified
Treatment 273
265








o
1
61






*•*. -j



j^?
1
Routine
Treatment
Routine
Treatment
(84% of Control)



152








•— *—


I
^g
1
324












I

1












104




SOURCE
WATSR
Routine
Treatment
fc ORAVITY-
SETTLED



t'

COAQULATED
& SETTLED *"


4.7 mg/L Cl,
1 .0 mg/L PAC
Modified
Tre
atment
1.2
t t
Tig/L KMnO* 4.O mg/L C
1 ,0 mg/L PAC ,
FILTERED .
WATER ,


i

FINISHED
WATER

1.7 ma/LCI,
O.2 mg/L CIO,
'
I, 2,6 m
0.2 mg

B/LC
/LCI

t
3.
         Figure 59.  Trihalomethane formation (mean  values) during
                     routine and modified (delayed chlorination) treat-
                     ment at  the Wheeling Water  Department (WV). "  .
                     (November 1978,  18,000-mVday [10-mgd] capa-
                     city.) THMFP conditions: pH 9.2; 9 to  13°C (48 to
                     55°F); storage time, 7 days.1"

treatment, the TermTHM found in the finished water had increased slightly from 84
percent (during routine treatment) to 88 percent of the source water TermTHM,
indicating that moving the chlorination point had little effect on this measurement.
A  decline of 48'/ig/L  (32 percent) did occur in the finished water InstTHM
concentration, however; so moving the chlorination point did  have a beneficial effect
to  some consumers, but this change did not increase precursor removal. Finally,
these three studies also confirmed the findings shqwn.in Figure 54 that  the ratio of
chlorine to bromine in the the trihalomethanes found in the clearwell decreases as
precursor is removed. These results indicate again that the conversion of bromide to
an active bromine species followed by reaction with precursor, materials is a more
rapid reaction than  the reaction  of chlorine with precursors.

  Contra Costa, CA, Results—Lange and Kawczynski reported on  a full-scale
experiment at the Contra Costa Water  District to determine the ability of alum
coagulation to  remove trihalomethane  precursors.20  At this location, the source
water is chlorinated during routine treatment to just beyond breakpoint, then
coagulated with alum, reducing the pH from 8.2 to 6,9, Lime is added, to the settled
water to raise the pH to 7.2 before filtering. Following filtration, the pH is adjusted
to 8.2,  and  the water flows into a 1.5  X 10s m3 (40-million-gal) clearwell.  The
InstTHM concentrations were determined at this point.
      Section VII. Treatment Techniques to Remove Trihalomethane Precursors  99

-------
  When the test began, the plant was operating as noted above, using a coagulant
dose of 50 mg/ L. The TTHM concentration in the effluent of the clearwell at this
time was  273 ng/L. Because source water TermTHM concentrations were not
measured  in this study, the influence of routine treatment on trihalomethane
precursors could not be determined. But a modification to provide chlorination of
the settled water lowered the InstTHM concentration in the clearwell effluent from
23 to 37 percent. This result assumes that the 8/15/77 data can be used as a control
for the entire experiment (Table 29). Because of the number of variables, exact
interpretation of these results is difficult. The increased  removal may have been
caused by at least three factors, possibly acting together; 1) shorter chlorine contact
time before the clearwell sampling point, 2) improved precursor removal prior to
chlorination (the purpose of the experiment), and 3) an increase in alum dose from 50
to 80 mg/ L over the presumed control. In this study, increasing the coagulant dose
did not improve the removal of precursors, as the InstTHM concentrations did not
decrease with increasing alum dose in this  range.

  TABLE 29. INFLUENCE OF SETTLED WATER CHLORINATION  ON
         InstTTHM IN CLEARWELL AT CONTRA COSTA, CA*°
Data
8/1S/77t
8/22
8/23
9/8
8/25
8/29
8/31
9/13
9/1
Alum dose,
mfl/L
60
80
80
80
103
120
120
130
148
InstTTHM,*
P9/L
273
171
193
231
190
180
185
203
213
Percent
InstTTHM
reduction
—
37
29
15
30
34
32
26
23
•Simplti eolt*ct«d *ft*r ctuirwoll.
fControl {lourc* water chlorlnitlon).

  Bristol County Water Company, Rl, Results—Blanck reported on the removal of
trihalomethane precursors at the Warren Filter Plant of the Bristol County (RI)
Water Company.*4 Here, reservoir water receives alum and a coagulant aid before
entering a clarifier/flocculator. PAC is then added before the water enters a settling
basin. The settling basin effluent receives lime treatment before filtration. Removal
of trihalomethane precursors in the settling basin was demonstrated by a decrease in
TTHM  concentration from 209 to 51 ftg/L when chlorination was moved from
between the clarifier/flocculator and the settling basin to after the settling basin.
This  reduction represented a decline of 75 percent. The author  did  not state,
however, where the TTHM samples were collected, or whether they were InstTHM
or TermTHM concentrations. In a way similar to the Contra Costa results discussed
above, these results are difficult to interpret for cause and effect relationships.
Insufficient sampling information is given to control for the influence of a shorter
chlorine contact time on the observed results.

  Metropolitan  Water District of Southern California Results—As reported by
Cohen et al., one portion of the Metropolitan Water District of Southern California
(MWDSC) system consists of a long transmission line from Lake Mathews to the
R.B.  Diemer filtration plant, followed by a feeder line to the San Joaquin Reservoir
(Figure 60).*° To assess the ability of the Diemer plant to remove trihalomethane
precursors, the trihalomethane concentrations at seven distribution sampling points

100  Treatment  Techniques for Controlling Trihalomethanes in Drinking Water

-------
    R.B. DIEMER
    FILTRATION
       PLANT
  SCALE IN KILOMETERS

0      6      10
                                  012345678
                                      SCALE IN MILES
           Olmda
           P.C.S.
                                 Lower Feeder
                                 *•»

       •East Orange County Feeder No. 2
       A-6

       OC-40
                                Station 525 • 58
                                                             Lake Mathews
                        Cl,
                     I POINT 2,
                                     SOURCE WATER
                                     COAGULATION
         OC-43
                                     FLOCCULATION
                                    SEDIMENTATION
                                      FILTRATION
                                                            Cl,
                                                          POINT 3 ,
                                    FINISHED WATER
                                      RESERVOIR
                                    FINISHED WATER

         Figure 60.  Sampling and chlorination locations. Metropolitan
                     Water District of Southern California.80 (Adapted
                     from JOURNAL American Water Works Association,
                     Volume 73, No. 2 [February 1981] by permission.
                     Copyright 1981, the American Water Works Asso-
                     ciation.)

beyond the Diemer plant shown in Figure 60 were determined. These sampling
points were monitored as the point of chlorination was changed in three steps from
just after Lake Mathews (point 1, Figure 60) to the filtered water at the Diemer plant
(point 4, Figure 60).
  Interpretation of the data from this study is complicated by two factors': (1) the two
controls, 23 days apart, produced different THM concentrations at the respective
sampling points, and (2) chlorine contact times before each sampling point are
different for each of the experimental runs, although for this water, THM concen-
trations reach their maximum concentration  in contact times shorter than those
experienced during  any  of the experiments. These facto'rs make comparison of the
resulting TTHM data difficult. For this analysis of the data (Table 30), sample point
CM-10 was selected, the InstTHM concentrations were assumed to have reached
maximum  (TermTHM) concentrations,  and the control data for  2/8/78 were
considered to be correct for  comparison with experimental runs 2-4. With these
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  101

-------
 s1
 0)
 re

 I
5'
 I
3*
tt
I
I
g
I
TABLE 30. REMOVAL OF TRIHALOMETHANE PRECURSORS BY THE R.B. DIEMER FILTRATION
     PLANT IN THE METROPOLITAN WATER DISTRICT OF SOUTHERN CALIFORNIA80 *



Chlorination

Date
1/16/78
1/24/78
1/27/78
2/1/78
2/8/78
point on
Figure 60
H
2
3
4
1§
Contact time.
hr
19.6
13.2
10.7
10.0
18.7
Free
c\,
residual.
mg/L
0.8
0.4
0.6
0.6
0.9






TermTrihnlomethanes.t
CHCI3
6
9
11
8
15
CHBrCI,
12
15
12
14
19
CHBr,CI
10
12
10
13
13


tig/L
CHBr,
<1
4
<2
6
3

Term
TTHM,
Mfl/L
28+
40
33+
41
50

Percent
TarmTTHM
removal^:
—
20
33
18
—
•All data are from sampling point CM-10. Figuia 60.
t Assumed to be TemtTHM concsntralions.
JBasod on 2/8/78 data.
jConlrol.

-------
assumptions, moving the point of chlorination was determined to result in a 20 to 33
percent reduction  in TTHM concentrations caused  by equivalent removals of
precursors in the Diemer plant.
  Different assumptions, however, lead to opposite interpretations. For example,
selection of the 1/16/78  data  for control purposes leads to the conclusion  that
TTHM's increased as a result of treatment. This demonstrates the difficulty of
controlling experiments  in  real plant situations.  Indeed,  the investigators of
MWDSC concluded that the Diemer plant did not remove precursors and that the
change in chlorine application point had no effect on formation of trihalomethanes.

  New Orleans, LA, and Evansville, IN, Results—Although control of finished water
TermTHM concentrations by removal of precursor during clarification was not the
major objective of studies at these two locations, data on the change in TermTHM
concentrations through the treatment plant were collected.63"81  These data (Table 31)
show that 40 percent of the trihalomethane precursors were removed by sedimen-
tation  in New  Orleans,  LA, and 31  percent  by the entire treatment plant in
Evansville,  IN.

 TABLE 31. PRECURSOR REMOVAL BY COAGULATION/SEDIMEN-
         TATION AT TWO FULL-SCALE TREATMENT PLANTS



Location
New Orleans, LA

Evansville, IN

Mean
fraction of
precursor
removed
B/(A + B + C)'
0.40
B'/(A + B +• C)*
0.31
Mean
fraction
converted
to InstTHM,
C/(C -»- A)"

0.28

0.54


Number of
tests

2

12



Reference

81

63
•Figure 66.
  Three studies focused almost exclusively on the impact of moving the point of
chlorination on finished water InstTHM and TermTHM concentrations rather than
on the removal of precursor by clarification. Because their results are closely related
to those previously reported in this subsection, they are reported in the following
three subsections.

  USEPA  In-house  Results—USEPA pilot  plant studies where chlorine  was
applied continuously at various points within the treatment train demonstrated the
importance  of the  point of chlorination  in causing reduced trihalomethane
concentrations in treated water. In one series of experiments, river water was
chlorinated (Figure 61, point 1) then held for 2 days to simulate off-stream storage.
The  water  then received either alum or ferric sulfate coagulation, floeculation,
sedimentation, and filtration through  dual media.  A finished water sample was
collected and stored for 2 days at 25°C (77° F) before analysis for chloroform. The
source water chlorine dose  (10 mg/L) was sufficient to maintain a free chlorine
residual in the finished water sample for the 2-day contact time.
  After 3 days of operation in this mode of treatment, the point of chlorination was
moved to the rapid mix, just before the coagulation/floeculation basin (Figure 61,
point 2).  In the next phase of the study, chlorine was added  to the settled water
(Figure 61, point 3) to determine whether or not coagulation and precipitation in the
settling basin would further reduce the precursor concentration. In the final phase of
the study, filtered water (Figure 61, point 4) was chlorinated to determine whether or

     Section VII,  Treatment Techniques to Remove Trihalomethane Precursors  103

-------
o
a.
"J 1.0 - -
a.
5
U)
5075
u
z
o
u
ia5
u
    ' 0,25--
                                               Ferric Sulfale Coagulant

                                               Aluminum Sulfale Coagulant
2
I
2-OAY SOURCE
WATER
STORAGE

t

COAGULATION,
FLOCCUUATION.
SETTUNG
5
3
-t
SAMPLING POINT
AFTER SIMULATED
2 DAYS IN
DISTRIBUTION SYSTEM
4
^l
FILTRATION | — *-»



DISTRIBUTION
SYSTEM



          Figure 61.  Chloroform in distributed water relative to point of
                     chlorination {pilot plant studies).
not the additional clarification during filtration would further influence the trihalo-
methane precursor concentration. The last three phases of the study were conducted
using ferric sulfate as a coagulant in one case and alum as the coagulant in the other.
In each case, the filtered water was stored in bottles at 25°C (77° F) for 2 days to
simulate reaching point 5 (Figure 61). This step allowed a comparison of the chloro-
form concentration theoretically reaching the consumer (TermCHClj) for the four
treatment approaches. Note that routine monitoring of the Ohio River during this
period indicated that the TermTHM concentration in the source water did not
change significantly during this experiment.
  Because a TermCHClj concentration was not determined on the actual source
water  used in this study,  the  influence of clarification during source  water
chlorination could not be evaluated; however, the data in Figure 61 do show that if
the terminal chloroform concentration during the study of chlorination at point 1  is
taken as unity, the removal of chloroform precursor during plain sedimentation,
coagulation,  and  filtration  is  apparent.  This  removal  is  evidenced  by  the
proportionately lower concentration  of terminal chloroform resulting when the
point of chlorine application was moved from the raw water to the rapid mix (25
percent decline), then to the settled water (40 percent decline), and finally to the
filtered water (50  percent decline). Also shown in Figure 61  is the improved
effectiveness of ferric sulfate, as opposed to alum, as a coagulant (at least in this
water).
  The improved effectiveness of ferric sulfate as a coagulant is shown in the last three
bars in Figure 61. The differences in the two  sets of data occur because, even when
chlorine was added at the rapid mix, precursor began to settle in the settling basin
and was removed from intimate contact with the free chlorine. Thus even when water
JO4  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
is chlorinated at the rapid mix (and all other conditions are equal), a better coagulant
will produce a lower terminal chloroform concentration because the separation of
chlorine and precursor in the sedimentation basin is hastened,

  Cincinnati, OH, Results—Theearly USEPA experimental results presented in the
preceding subsection encouraged the water utility personnel of Cincinnati, OH, to
attempt to lower the trihalomethans content in their finished water by moving the
point of chlorination from the source water to the clarified water.82"83 Figure 62 is a
schematic diagram of the Cincinnati Water Works. The water is pumped from the
Ohio River into two large uncovered reservoirs and  retained for approximately 2
days. For several  years before this study, the practice had been to add alum to the
water going to these reservoirs, along with sufficient chlorine to carry a free residual
through the reservoirs, the treatment plant, and the extremities of the distribution
system. In mid-July 1975, the point of chlorination was moved from point A to the
headworks of the  treatment plant (point B, Figure 62). The coagulant (added to the
source water) entering the off-stream storage reservoirs (point A) at the time of the
study reduced the  source water turbidity from approximately 11 to 2 ntu as the water
entered the treatment plant.
  A  sharp decline in tap  water chloroform  concentration was measured in the
distribution system following the movement of chlorine application from point A to
point B  in mid-July (Figure 63).  This decline is  attributed  to the change in
                                                   COAGULANT
                     OFF-STREAM STORAGE RESERVOIRS
                        (RETENTION TIME. TWO DAYS)
                                                   COAGULANT & OTHER
                                                       TREATMENT
                                                       CHEMICALS
                                                    WATER
                                                 - TREATMENT
                                                     PLANT
                          DISTRIBUTION SYSTEM

         Figure 62.  Schematic diagram of Cincinnati Water Works (OH).39

     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  105

-------
      260 -Jr
     220 --
    Found
             Chlorination Moved
             From Point A to
             Point B (Fig. 62)   £1
             July 14, 1975
                     I     I    1     I

                   Terminal Chlorolornn
                   Concentrations For
                   Chlorinated Source
                   Water Stored:
                    O 3 days
                    D 4 days
                      6 days
                                                                 O  -
         JUL      SEP
         1975
NOV       JAN      MAR

  DATE OF SAMPLING
MAY     JUL
         1976
         Figure 63.  Trihalomethane concentrations in Cincinnati, OH,
                     tap water.1*

chlorination practice. To determine whether or not changes in the source water had
occurred during this time period to account for this decline in chloroform concen-
tration, THMFP determinations were made on the source water at various times
during the test period (the recommended control procedure). Although these data
are somewhat scattered, they do indicate that the decline in the distributed water
chloroform concentration was not caused by a change in the precursor content of the
raw river water.
  Note that in this case, the ratio of InstTHM to TermTH M in the storage reservoir
effluent [the C/(C + A) fraction as shown in Figure 55] was0.63. Unfortunately, the
precursor removal in these off-stream storage reservoirs [the B/( A + B + C) fraction]
was not obtained  during this study;  but  a few days  before the change, the
TermCHCb concentration was 260 pg/L in the river and  210 /ag/L in the finished
water, indicating a 19-percent reduction by the entire treatment process. Note that
most  of this removal occurred in  the storage reservoirs (Table 28). Note also that
although a sharp decline in distributed water chloroform concentration occurred, a
similar decline in the concentration of the bromine-containing trihalomethanes did
not. The reason, as  noted previously, is that these materials are  formed faster than
chloroform and therefore  will be  formed first from any precursor that remains.

  Durham,  NC,   Results—Young  and  Singer investigated  the removal  of
trihalomethane  precursor  at  the Durham, NC, Water  Treatment  Plant,84 On
September 7,1976, they determined that the chloroform concentration in the source

10S  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
water, Lake Michie, was about 110 ^ig/ L after 2.5 hours of contact with free chlorine.
They sampled the clearwell at the water treatment plant 10.35 hours after chlorine
was  added at the  rapid mix on October  16, 1978, and obtained an InstCHCb
concentration of 100 jig/ L. Because terminal concentrations were not determined on
the source and filtered water, the removal of precursor by the treatment plant could
not be calculated.
  In early January 1977, source water chlorination was stopped,  and chlorine was
added to the settling basin effluent just before dual-media filtration, 6.25 hours
before the sampling point. Before the change, the InstCHCb concentrations in the
finished water were about 125 j*g/ L; immediately after the change, they declined to
75 to 90 /*g/ L. Because TermCHClj concentrations were not determined, the decline-
in theTermTHM concentrations, if any, could not be calculated. A 28-to 40-percent
reduction in InstCHClj concentration in the clearwell (a benefit to consumers near
the plant) did occur, however.

  Precipitative Softening—Daytona Beach, FL, Results—Another example of the •
use of clarification for the removal of precursor was a USEP A sponsored study at a
softening plant in Daytona Beach, FL.*5*8* Figure 64 is a schematic diagram of the
Daytona Beach Water Treatment Plant and shows  the two alternative points of
application of chlorine during the first two of three modifications. In this system,
analyses for InstTH M and TermTH M concentrations were performed on the source
water and several hours after filtration (sample point 5).
                                                         Cl, #1
                                                         POLVMiR.
                                                         NALCOLY7E»8174
                                                         SLAKED LIME"
                                                         Cl, #3
                                     TO
                                DISTRIBUTION
                                   SYSTEM
         Figure 64.  Flow diagram of the Ralph F. Brennan Water Plant,
                     Daytona Beach (FL).aB'8»
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  107

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  Normal practice consisted of addition of lime and coagulant aid to the upflow
softener/clarifier (90-min detention) to increase the pH to about 9.4, followed by
recarbonation (when necessary), filtration, and storage in the clearwell. For the third
modification of this study, alum (20 to 30 mg/ L) was also added at the same point as
the lime, and chlorine was added at the clearwell. The TermTHM  samples were
stored for 2 days at  pH 7.2 to 9.6 and a temperature of 25° C (77° F). The large
variation in pH  makes complete interpretation of the TermTHM data difficult.
  During the three treatment modifications, the mean TermTHM concentration of
the raw water only changed from minus 7 percent to plus 10 percent of the value
measured  during routine operation (Figure 65). Comparison of the TermTHM
concentration in the source water with that in the finished water revealed a 41-
percent decline  caused by  the  precipitative softening and  filtration processes.
Moving the chlorination point to the recarbonation basin resulted in virtually no
change in the percent  of source water TermTH M present at sample point 5 (59
percent versus 63 percent). Chlorinating the filtered water did, however, cause a
substantial change: Sufficient precursor was  removed by filtration to  cause an
       CONTROL
CO
8r^-i *Percent of Control o
in
I-*.
CO


a*
3
O
CC

1

c
.9
«i
1



ication
2nd Modi



SUPPLY
W6U.S


§
1
1
•2


^ InstTTHM g
r~\ THMFP § 1 c
	 ._ 0 o
LZ]+^ TermTTHM o * S
cc «i .H
O) CO ^
a ss. -o
o o £
CM CM "
CN CM jj




•j—J SOFTENING U HECAR1ONAT1ON U FILTRATION W CLEARWiLL

1
I

m
1
n
V
o
1


c
0
to
1
T3
co
eo
o
to
1

U STORAGE 1
   Routine       ci,

   1 st Modification

   2nd Modification

   3rd Modification
UMI
NALCOLYTE*8t74

LIME          CI,
NALC0LYTES8174
 +
LIME
NALCOLYTES8174

LIME
NALCOLYTE*8174
ALUM
Ci,


CI,
         Figure 6B.   Influence of three treatment modifications  to re-
                     move trihalomethane precursors at Daytona Beach.
                     FL. THMFP conditions: pH 9.0; 20°C (68°F); storage
                     time, 2 days.88-"
108  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
additional 16 percent drop in the TermTH M concentration remaining in the finished
water.  Finally, the addition of alum to the clarifier did not improve the treatment
significantly (a 4-percent decrease in source water TermTH M concentration was
found  in the filtered  water). Note that  a 33-percent decline  in InstTHM
concentrations occurred during the second and third modifications (a benefit to con-
sumers near the treatment plant).
  In this study, TermTHM concentrations were not measured at the  intermediate
treatment points, so calculations of the fractions C/(C + A) and B/(A + B + C)
(Figure 55) could not be made. But because the high pH (9.3 to 9.5) would increase
the formation rate of trihalomethanes, a rather high fraction of source water
THMFP would  be expected to be converted to InstTHM through the treatment
plant [C/(C + A), Figure 55].

  Jefferson Parish, LA, and Miami, FL, Results—Although precursor removal by
clarification was not the  primary  objective at these locations, these  USEPA
sponsored projects evaluated the precipitative softening unit process.14*87 As was the
case in Daytona Beach, these data (Table 32) show the removal of precursor by lime
softening in spite of the higher operational pH for this unit process.

TABLE 32. PRECURSOR REMOVAL BY SOFTENING UNIT PROCESSES
              AT TWO FULL-SCALE SOFTENING PLANTS



Location
Jefferson Parish,
LA
Jefferson Parish,
LA
Miami, FL
Mean
fraction
precursor
removal.
B/(A + B + C)*
0.16

0.25

0.29
Fraction
converted
to
InstTHM,
C/(C + A)*
0.02f

0.04f

0.01$


Number
of tests
3

4

4



Reference
14

14

87
•Figur* 55.
tCombinad chlorine r*»idua! maintained through treatment plant; therefore fraction IB low.
{Chlorlno finrt added to tattling baitn effluent; therefore fraction i> low.


  Direct Filtration—USEPA In-house Study—The primary objective of this in-
house research performed at the USEPA pilot plant facility was to demonstrate the
feasibility of direct filtration for the removal of  humic substances  from water
supplies, including their associated total THMFP.88 In this research,  a gravel pit
water spiked with  humic acid and an algae-laden lake water were used in direct
filtration pilot plant studies in which a cationic polyelectrolyte was  used as the
primary coagulant. Characteristics of the surface waters used are shown in Table 33.
Filtration performance was evaluated using classic measures of color, turbidity, and
head loss development. In addition, the removal of trihalomethane precursors was
evaluated by measuring the THMFP in the raw and filtered  waters.
  The humic material used in  this study was extracted from  Michigan peal  by
soaking it in 0.1 N  NaOH for 24 hours and recovering it by using the procedure of
Hall and Packham." The formation  of trihalomethanes from this humic material
was evaluated  by  chlorinating three different solutions with dry-weight  humic
material concentrations of 2.5,5, and 8 ing/ L, measured as weight on evaporation to
dryness. This chlorination was performed in buffered, distilled water using NaHCOj
(12 fimo\/L) so that the pH remained approximately constant (8.0 to 8.1). The
chloroform yield of 1.3 percent, based on organic carbon (TOC), agreed with the
yields generally reported  in the literature for humic acid."*79189

      Section VII. Treatment Techniques to Remove Trihalomethane Precursors 109

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  TABLE 33. WATER QUALITY CHARACTERISTICS OF GRAVEL PIT
               WATERS AND STONELICK LAKE WATER
Watar quality
parameter
Unspiked gravel   Spiked humic acid-   Stonelick
   pit water*	gravel pit water   Lake waterf
pH                               8.2
Turbidity, ntu                     1.6
Alkalinity, mg/L as CaCO,       129
Hardness, mg/L as CaCO3       133
TOC, mg/L                      5.4
Sutpnnded solids, mg/LJ          NM
Apparent color,
  Pt-Co unit*                     NM
                        8.2
                        4.0
                        NM§
                        NM
                        6.9
                        NM
                      100
  8.0
 25
 67
110
  7.3
 11.2

340
•ColllCUd 5/18/78.
fColl.o.d 7/11/78.
ilMlltuild 7/26/78.
|Not m«i»ured.
   The humic material, about 3.3 mg/ L by weight, was added to the gravel pit water
 for use in the direct filtration pilot plant studies. The gravel pit water was used in this
 study because it was a low-turbidity water. The unspiked gravel pit water contained
 5.4 mg/L of TOC and had a 5-day THMFP concentration of approximately 190
      at pH 8.3 and 25°C (77° F) (Figure 66).
       600
                   20
                                    60       80

                                 REACTION TIME, hr
                                                     100
                                                             120
                                                                      140
          Figure 66.   TTHMformationcurvesfor unspikedgravelpitwater
                      and spiked humic acid-gravel pit water. pH 8.3; 25°C
                      (77°F)."

   Jar tests were used to screen cationic polyelectrolytes and to select the dose to be
 used in direct filtration. The jar tests studied the gravel pit water containing humic
 materials at approximately the same concentration as  was ultimately used in the
 direct filtration pilot plant studies. Based on the jar test results for pH 6, a dose of 6
 mg/L of polyclectrolyte Betz® 1190* was selected as the optimum for^stabilization
 (Figure 67). This dose was used in the direct filtration tests, and the results demon-
 •Mgnufactured by Bc« laboratories. T»evosc. PA 19047.
 7 JO  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
          120
                                8       12       16

                               POLYMER DOSE,mg/L
          Figure 67.   Turbidity and color jar test data for humic acid using
                      Betz® 1190. 5 mg/L humic acid added to gravel pit
                      water; source water color 100 Pt-Co units, pH 6.0;
                      turbidity 1.0 ntu.ra

 strated that jar tests can be used to choose coagulant dosages, even when cationic
 polymer  is  the  primary coagulant.  The  cationic  polymer selected showed a
 stoichiometric relationship  with  respect to doses required  to coagulate various
 concentrations of humic material (Figure 68).
•  • The pilot plant studies using gravel pit water spiked with humic acid demonstrated
 that direct filtration was effective for turbidity removal (Figure 69), All THMFP
 analyses were performed at pH 8.3 and 25°C (77° F). The spiked source water had a
 THMFP concentration of  400  to 470  ng/L; however,  as  previously  noted,
 approximately 200 pg/L of this was caused by organic compounds that were
 originally present in the gravel pit water.

      Section VII. Treatment Techniques to Remove Trihalomethane Precursors  1)1

-------
      150
      140
  Initial Humic Acid Cone
D 2,5 mg/L
O 5.0 mg/L Dry Weight
» 10.0 mg/L
                            8       12       16      20

                              POLYMER DOSE, mg/L

         Figure 68.  Stoichtometry of coagulation of humic acid with
                     Betz® 1190. Humic acid added to gravel pit water;
                     pH 6.0.«a

  The results  of direct  filtration runs  at  pH 6  showed  that the THMFP
concentration could be reduced  to approximately 200 fig/ L—the background level
of the gravel pit water (Figure 70)—thus demonstrating that humic acid precursors
could be removed by direct filtration. As a control, unspiked gravel pit water was
filtered at pH 6.  In this case, only an average of 9 percent of the trihalomethane
precursor material was removed throughout the run, indicating that these materials
were very different in character from the spiked humic materials. Furthermore, other
tests showed that based on TOC, the chloroform yield of the unspiked gravel pit
water was 0.3 percent, again indicating the difference between those precursors and
those in the humic materials used for spiking. Finally, the effluent from the filtration
test (Figure 70) was evaluated  for chloroform yield as a method of organic character-
ization. Samples collected at 90 minutes and 6 and 10 hours into the filtration test
averaged a chloroform yield of 0.4 percent on a TOC basis after 5 days at pH 8.3.
Thus the trihalomethane precursors that were not removed in this test were likely to
be the same materials that were in the unspiked water. Other treatment processes
would therefore be required to remove the organics originally present in the gravel
pit water. Note that the data in Figure  71 (page 115) show that  better color and
THMFP removal occurred at pH 6, in contrast to pH  8.3,

/12  Treatment Techniques for Controlling Trihalomethanes in Drinking  Water

-------
             1.6
   1.2
3
c

E  0.8
Q
CD
tr
             0.4
          q
          x*
          "S
          c
    20
                        Control
                                                        q
                                                        X
          O  10
          Q
          iS
          3:
                  02468
                           TIME IN OPERATION, hr

          Figure 69.   Turbidity and head loss data for spiked humic acid-
                      gravel  pit water.  Pilot plant operated at pH 6.0;
                      source water turbidity 3.8-4 ntu.*8

  In another phase of the research, water was collected from Stonelick Lake and was
used in a brief direct filtration study. This water was  selected  because  of its high
apparent color (340 Pt-Co units) and relatively high turbidity (25 ntu). In addition,
the trihalomethane precursors in this water represented another type  of natural
organic material. The organic precursors were assumed to be autochthonous (i.e.,
produced within the lake  from algal activity or from aquatic plants in the littoral
zone of the lake). The THMFP for a 5-day contact period at pH 8.3 was 634 /tg/ L.
  Direct filtration using Betz® 1190 as a primary coagulant was effective in terms of
color and turbidity removal: Effluent turbidity was generally less than 0,4 ntu, and
effluent color was less than  15 units (Pt-Co). Polymer doses  required for direct
filtration were high because of the high color and turbidity of  the raw water. The
THMFP data showed that some reduction of the precursors could be achieved by
direct filtration (33 to 55 percent reduction  in the 5-day THMFP), but the  filter
effluent THMFP's were still high (Figure 72, page 116).

  East  Bay  Municipal  Utility District  Results—Cams and Stinson  investigated
direct filtration following alum coagulation and flocculation at the Walnut Creek
Filter Plant of the East Bay Municipal Utility District." In this study, chlorinated
water from the Pardee Reservoir arrived at the filter plant containing both InstTH M
as well as THMFP. Two test situations were  compared With the routine operation.
At this plant, alum (17 fig/ L) and chlorine are added at the rapid mix, and lime (5
mg/L) is  added after the filters. The two test conditions  varied from the routine
operation by: 1) moving chlorination from the rapid  mix to after the filters and, 2)
reducing chlorine dose at Pardee Reservoir and chlorination after the filters.
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  113

-------
      w  40
      o
      U
      CC  20-
      3
      o
      o
      LU
      K

      I 400
        300 •
      X
      O>
      a.
        200-
      5
      I
        100-
                  T
                                     > 6 mg/L Polymer, No Precoat
Source water 423 jjg/L
                           Effluent
                            4       6       8       10

                             TIME IN OPERATION, hr
                                                           12
         Figure 70,   Apparent color and THMFP data for spiked humic
                     acid-gravel pit water. Pilot plant operated at pH 6.0;
                     source water color 85 Pt~Go units. THMFP condi-
                     tions: pH 8.3; 25°C (77°F); storage time, 6 days."

   In  this case, during routine operation, the fraction of decline of TermTHM
concentration, B'/(A -f- B + C), was 0.13 during direct filtration. Furthermore the
fraction of the THMFP unremoved  by direct  filtration  that was converted to
InstTHM during flocculation and direct filtration was 0.25. The data in Table 34
(page 1 17) show that little change in TermTHM concentration occurred when the
chlorination point was moved to after the filter. Also, little effect of change to the
"Test 2"conditions was observed. Similarly, in this case, the finished water InstTHM
concentration did not decline during either of the test conditions.

   Los Angeles, CA, Results — McBride of the Los Angeles Department of Water
and Power reported  on  a  pilot plant  study in which the 1-hour TermCHCb
concentration in the source water was compared with the same value after direct
filtration." In this case, the TermCHClj concentration after 60 minutes was
in the source water, and  10 Mg/L after direct filtration. This 47-percent decline in
TermCHCb thus indicates removal of chloroform precursors during clarification.

   Bridgeport, CT, Results — To determine the best technique for treating water in
Bridgeport, CT, the Bridgeport Hydraulic Company studied various  pilot plant
arrangements." Two runs were made with each of these configurations, and the
resulting mean TermTHM concentration, turbidity, and color in the finished water
were determined  (Table 35, page  118).  These data show the benefits of precursor
removal before  disinfection. Compared with the other data presented in  this
subsection, these removals were high.

7 14  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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              0!
              To  60
              o
              VI

              8
              C  40	
              oc
              O

              O   20
              iu
              cc

              I
                300 •
              X200
                100
        III
           Figure 71.
       2488
         TIME IN OPERATION, hr

Apparent color and THMFP data for spiked humic
acid-gravel pit water. Pilot plant operated at pH con-
ditions indicated; source water color 50-100 Pt-Co
units;  hydraulic  loading,  12  rrt/hr  (5 gpm/fta).
THMFP conditions: pH  8,3; 25°C <77°F);  storage
time, 4 days.*8
Discussion—
 •  Data from 28 different studies discussed in this subsection have demonstrated the
potential  for removing  trihalomethane  precursors  by  clarification.  Because
precursors are not defined organic chemicals, but a mixture of compounds  that
varies  from location to location,  the potential for removing these  materials by
clarification also varies from location to location.
   Table 36 (page  119) summarizes the data on trihalomethane precursor removal
from all the studies presented in  this subsection. Although experimental design
problems or incomplete data reporting made some interpretations difficult, for 24 of
the 28 studies, calculations could be made indicating the effectiveness of the clarifica-
tion process. Trihalomethane precursor removals varied from 16 to 51 percent for
coagulation/sedimentation plants, from 16 to 41 percent for precipitative softening
plants, and from 13  to 100 percent for direct filtration plants. In each case, these
removals quantify the decline in TermTH M concentrations that could be attributed
to the presence of a given treatment plant or unit process. 1 f the water had not been so
treated, consumers would have had higher trihalomethane concentrations in their
drinking water.
   Because clarification  processes can  remove trihalomethane  precursors, the
possibility exists  for  lowering trihalomethane concentrations even further by
chlorinating after the clarification  processes. By determining the concentrations of
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  11S

-------
   £
   ta
   u
   V)
   0300-
   O200-
   O
   O
   gioo-
   oc

   I.
     600-
   D>
   a.
   a."
   u.
400-
     200-
            ' No Polymer  {Filter *6) •
                             - 10 mg/L.-
                             (Filter 86)
12 mg/L	15,2 mg/L —
                                              (Filter #6)
          (Filter S 6)
                                      ft   I  ft  ft  ft-i-ft
                                             Source Water THMFP
                                                  Filter #6
                                6       8      10
                             TIME IN OPERATION, hr
                                                      12
                                                              14
                                                                      16
          Fiflure 72,  Apparent color and THMFP data for Stonelick Lake
                     water. Pilot plant operated at pH 6.0, filter 4, polymer
                     dose of 17.9 mg/L; filter 6, polymer dose indicated
                     between  arrows;  source  water color 225  Pt-Co
                     units; hydraulic loading 5 m/hr (2 gpm/ft2). THMFP
                     conditions: pH 8.3; 25°C (77°F); storage time, 8 days,88
TermTHM and  InstTHM and calculating  the THMFP at various points in a
treatment plant,  predictions for the potential success of lowering trihalomethane
concentrations by moving the point of chlorination in that location can be made. The
chance  of success is enhanced  if the fraction of TermTHM  removed in the
clarification or precipitative softening step and the fraction of precursor converted to
InstTHM through  the  unit  process  is  high.  Under such circumstances, the
TermTHM concentrations in the finished water are likely to be lowered if the
chlorination point is located after the unit process under study. In  nine of the 28
studies reported  in Table  36, the fraction C/(C + A) from Figure 55 could be
calculated and compared with the  observed change in TermTHM  concentration
when the chlorination point was moved. In the seven of those nine cases where source
water was chlorinated to produce a free residual, this fraction ranged from 0.05 to
0,63. Only when C/(C + A) was 0.63 did a significant decline in finished water
TermTHM occur when the chlorination point was moved. This result verifies that
this fraction must be high through a unit process to lower TermTHM concentrations
successfully when  chlorination is moved to a  point  after that   unit process.
Unfortunately, insufficient data are available to make a numerical judgment about

116 Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
 ?
Ol
                TABLE 34. REMOVAL OF TRIHALOMETHANE PRECURSORS BY COAGULATION AND DIRECT
                FILTRATION AT THE WALNUT CREEK PLANT OF THE EAST BAY MUNICIPAL UTILITY DISTRICT86
I
4'

I
o
ai

I
§

2.               -2 days. pH 9.Z.
j&                tFilfaied water chlorination,
o"               ^Reduced chlorinatton at Pardae Rssarvolr and f iltared water chlorination.
^t
K

a
3
Source water from Pardae Reservoir
Test
Control
Test It
Test 2%
Cl, residual,
mg/L
QM
0.21
0.14
InstTHM,
rti/L
84
95
84
THMFP."
Mfl/L
63
B2
65
TermTHM"
Mfl/L
147
147
149
Cleat-well water
InstTHM.
MB/L
95
93
94
THMFP.*
MI/L
33
35
16
TermTHM/
MJ/L
•(28
128
110

-------
 TABLE 35. INFLUENCE OF VARIOUS CLARIFICATION TECHNIQUES
         ON TRIHALOMETHANE PRECURSOR REMOVAL AT
                           BRIDGEPORT, CT"
                                                Percent removal
  Treatment
                                          Mean
                                        TermTHM*
           Turbidity    Color
Chlorine, limo,
  fluoride, Virchem® (control)
Direct filtration, post-chlorination:
      Run 1
      Run 2
Conventional treatment,
  pott-chlorination:
      Run 1
      Run 2
Oj/diatomacoous earth filtration,
  post-chlorination:
      Run 1
      Run 2
36
54
54
54
64
73
86
88
86
88
87
75
21

89
93
89
94
81
80
•Slona* condition! not tptctliad,                                   •                 '

 the size of the fraction C/(C + A) needed to lower TermTHM concentrations'
 following a chlorination move. This is also true regarding the fraction B/( A 4- B 4- C)
 or B'/(A + B + C).
   Also, if the rate of formation of trihalomethanes is favorable in a specific location,
 shortening the time elapsed between chlorination and the finished water by moving
 the chlorination point downstream in the treatment plant will probably lower the
 InstTHM concentration in the finished water, thereby benefiting consumers (espe-
 cially those near the treatment plant) (Figure 56). As shown in Table 36,10 locations
 attempted  to control trihalomethane concentrations by moving the chlorination
 point. Seven produced  a  positive reduction of 2 to  75 percent in finished water'
 InstTHM concentration.
   As noted in Section V, studies such as these should involve sufficient samples to
 monitor changes in source water precursor concentrations and to  ensure  that
 apparent changes in precursor concentration cannot be attributed  to analytic
 imprecision. Composite sampling may also prove to be beneficial toward this end.
 Although some of the 28 studies discussed may have been based on fewer samples •
 than desirable, taken together they demonstrate well the partial removal of precursor
 by clarification. Additionally, the studies described were generally performed over a
 short time. Studies should be performed over at least a l-year period to determine
 seasonal effects on precursor concentration, nature of the precursor, and effects of
 seasonally  varying reaction conditions (if not held constant) on the results observed.
   Finally,  if precursor is removed  by clarification or  precipitative softening,
 bromine-containing trihalomethane concentrations will .be influenced less than the
 chloroform concentration. The reason is  that chlorine  reacts quickly with any
 bromide present in the water to produce active  bromine species that effectively
 compete for whatever precursor remains after treatment. This effect will be most
 pronounced early in the chlorine/precursor reaction, declining as time passes and
 more chloroform is formed, until precursor is exhausted.
   Note that for several of the 10 utilities that moved the point of chlorination in an
 attempt to lower trihalomethane concentrations (Table 36),  data on the resulting
 bacteriologic quality of the finished water were  also collected. Where available,
 these data  will  be discussed in Section IX.
 118  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
          TABLE 36. SUMMARY OF DATA ON REMOVAL OF TRi HALO METHANE PRECURSORS BY CLARIFICATION
CO
S1
3-
3
•§'
§
0)
3-'
0!
8"
3
33*




26"

16"

*
t

Percent increased*
Fraction InstTHM TermTHM
C/(C + AJf reduction reduction • Remarks Reference


• t
t

t
t
t

t
t
t
%
t
0.26




0.05

0,23

t
t



§
' §

§
S
§

§
§
S
§
§
39M




54b

32b

23 to 37"
75»,b



§
§

§
§
§

§
§
S
§
§
Ob




Ob

ob

t
t



"Fraction B"/(A + B + C) from Figure SB
"Fraction B'/(A + B + Cj from Figure 55

"Fraction B'/(A + B + C) from Figure 55
'Fraction BV(A + B + C) from Figure 55
"Fraction B'/(A + B + C) from Figure 55

'Fraction B'/{A + B + C) from Figure 55
"Fraction B'/(A + B + C) from Figure 55
"Fraction B'/(A + B + C) from Figure 55
"Fraction BV(A + B + C) from Figure 55
•Fraction B'/JA + B + C) from Figure 55
"Fraction BY (A + B + C) from Figure 55
^Chlorine moved to settled water;
cMay have been influenced by a sharp
decline in source water precursor
during the study period
•Fraction B'/(A> B> C) from Figure 55
bChlorine moved to settled water
•Fraction B'/(A t B + C) from Figure 55
''Chlorine moved to settled water
"Chlorine moved to settled water
•Chlorine moved to settled water
bOata assumed to be InstTHM concentrations


18
18

18
18
18

18
18
18
18
18
18




18

18

20
66

    Continued

-------
 TABLE 36. (Continued)
s1
3>
GJ
I
I
~i
«
n
I
C
w
t
O
o
a
5
§:
1'
•?
3-'
0)
5"
3
*
5-
0)
3
*?
3"
5*
3'
a'
«s
I

""*




Influence
of moving


chlorination to later


Treatment
and
location
Metropolitan Water District
of Southern California

New Orleans, LA
Evansville, IN
USEPA Pilot Plant
Cincinnati, OH


Durham, NC

Precipitative softening:
Daytona Beach, FL




Jefferson Parish, LA

Miami, FL

Direct Filtration:
USEPA Pilot Plant

East Bay MUD, CA
Percent
TermTHM
reduction
during
clarification

20"

40"
31"
t
19"


t


41"




1 6 to 25«

29"


3S to 100"'b

13"
pointin treatment train



Percent
Fraction InstTHM
C/{C +

t

0.28
0.54
1
0.63


|


j




A)f reduction

j



t
t


28 to 30"


1Qb, 33s-d




0.02to0.04b §

0.01 b


*

0.25

§


§

2b
Percent
increased*
TermTHM
reduction Remarks

Ob "Fraction BV(A + B + C) from Figure 55
bChlorine moved to filtered water
"Fraction B/(A + B + C} from Figure 55
•Fraction B'/(A + B + C) from Figure 65
40* "Chlorine moved to settled water
86b "Fraction B'/|A + B + C) from Figure SS
^HCI] only; chlorine moved to off-stream
reservoir effluent
$ "Chlorine moved to settled water


Ob, 23c«d 'Fraction BV(A + B + C) from Figure 55
bChlorine moved to settled water
°Chlorine moved to filtered water
'Varying pH storage conditions influenced
results
§ "Fraction B/(A + B + C) from Figure 55
bChloramine residual
§ "Fraction B/(A + B + C) from Figure 55
bChlorine routinely added to settled water

§ "Spiked water reduced to starting concentration
^Fraction B'/JA + B + C) from Figure 55
Ob "Fraction B'/(A + B + CJ from Figure 55






Reference

80

81
63

82,


84


85,




14

87


88

55






83





86












Continued
                                                                  bChlorine moved to filtered water

-------
IS
?
&
g
s
%
S

1
o
g
IHBLC jo, (Continue*




Treatment
and
location

Los Angeles, CA
Bridgeport, CT
V


Percent
TermTHM
reduction
during
clarification

47*
36 to 54«

Influence of moving
chlorination to later
point in treatment train
Percent
Percent increased*
Fraction InstTHM TermTHM
C/(C + A)f reduction reduction Remarks

£ § § * Fraction BV(A + B + C) from Figure 5S
$ § § * Fraction B'/{A + B + C) from Figure 5S







Reference

90
91
'Increase compared! with reduction that occurrtd with routine operation.
tFram..FiBur8 BB.
^Unknown.
§Nst attempted.

-------
Control of Precursors at the Source

General Considerations—
  When possible, water utilities should examine the quality of their source water to
determine whether or not operational changes could be made to improve the quality
and thereby lower the concentration of trihalomethane precursors. Some examples
of this technique will be given in the following subsections.

Experimental Results—
  Selective  Withdrawal from  Reservoirs—Barnett and Trussell reported on the
experiences of the Casitas Municipal Water District.*2 This water district uses Lake
Casitas as its source, with a maximum  depth at the intake  of 59 m (194 ft) and a
volume of 308 X  106 m5 (254,000 acre-ft). Water can be withdrawn from the lake
through any one of nine hydraulically operated intake gates that are separated by
depth intervals of 7.3 m (24 ft). During the period August 1977 to March 1978, the
organic content of the lake waters was measured at the surface and at 23,46, and 58
m (75, ISO, and 191 ft).  Samples were analyzed for TOC concentrations and 100-
hour THMFP; temperature and pH were not reported. Analyses completed during
that period indicate that both concentrations for TOC and total TH M FP at a given
depth in the lake vary significantly from time to time during the year. Several factors
have  been identified  that  appear to influence these  concentrations. These are
summarized as follows:
   1. Natural conditions that cause thermal and dissolved oxygen stratification and
turnover of the lake. Data collected during January and February 1977 indicate that
upwelling of a very small zone of anaerobic water during turnover caused a major
increase in total organic content of the source water. A TOC concentration of 9.3
mg/L  was  found during this  period—a  higher  concentration than occurred
previously.
   2. The Lake Casitas aeration system that is in operation during the period April to
October of each year. This system significantly influences  thermal and dissolved
oxygen stratification patterns.
   3. Algal blooms.
   4. Unusually large quantities of inflow to the lake from  the Casitas watershed,
resulting in  inundation of areas that have not been previously covered by water.
   Figure 73 illustrates the importance of these factors. The organic profile collected
on August 25, 1977, showed that (at least in this case) significantly lower concen-
trations of trihalomethane precursors existed in the zone of the lake from a depth of
30 to 50 m (100 to 165 ft). Water drawn from this zone would be expected to have
considerably lower TermTHM concentrations upon chlorination  than if source
water had been drawn from other levels in the  lake. This experience  illustrates a
practical technique that a  water utility may have at its disposal for controlling
trihalomethane precursors in their source water.

   Plankton Control—Recently, investigators have been studying the possibility that
algae (either themselves or their extracellular products) can act as trihalomethane
precursors. Experiments in  1976 and 1977 showed that constituents of both centri-
fuged cells and the noncentrifugeable extracellular products from a culture of the
blue-green algae  Anabaena flos-aquae and the green  algae Panadorina morum
served   as trihalomethane  precursors  when  these materials  were   chlorinated
(Unpublished report. R. Daum, USEPA, Cincinnati,OH, 1979). Later, Hoehnetal.
conducted a laboratory  study of the trihalomethane yield  capacity (a version of
THMFP) of algal-produced organic carbon." This study was undertaken after a
possible causal relationship was observed in  1975  between the trihalomethane
concentrations in  the finished water of the Fairfax County Water Authority and
ehlorophyll-a concentrations in the source water for that utility. From this study, the
authors concluded:

122  Treatment Techniques tor Controlling Trihalomethanes in Drinking Water

-------
      200
                   1O
                            20      30       ,40
                             WATER DEPTH, m
                                                               60
                   33      .66       94      131
                              WATER DEPTH, ft
                                                      164
                                                              197
          Figure 73.   Lake Casitas  organic profile, August. 25, 1977,
                      Casitas Municipal Water District (CA).9Z (Adapted
                      from JOURNAL American Water Works Association,
                      Volume 70, No. 11 [November 1978] by permission.
                      Copyright 1978, the American Water Works Asso-
                      ciation),
   I. Both green algae and.blue-green algae produce extracellular products that upon
 chlorination yield at least as much chloroform per unit of organic carbon as has been
 reported from chlorination of humic and fulvic acids.
   2, The algal extracellular products generally produce greater yields of chloroform
 from the available TOC than does the algal biomass.
   3.  Though  not  yet  fully  confirmed, indications  are  that  high-yielding
 trihalomethane precursors are liberated from algae in greater abundance near the
 end of the exponential phase of growth than at any other time during their life cycle.
   4.  Data collected during 1976 and 1977 do not  confirm the apparent causal
 relationship observed in 1975 between finished water trihalomethane concentrations
 and reservoir chlorophyll-a concentrations.

   Finally,  work  by  Briley  et /al.  confirmed  that  high  concentrations  of
 trihalomethane are produced from algal biomass and algal metabolites.94 They also
'found that both algae and extracellular products derived from algae growth
 produced trihalomethane concentrations that are comparable to yields observed
 from humic and fulvic acids. In contrast to the work of Hoehn et al.," Briley et al.94
 suggest that maximum levels of trihalomethanes appear to be produced during the
 entire exponential growth phase of Anabaena.
   The significance  of these  results is that a reduction of trihalomethane concen-
 trations may be partially accomplished by controlling the natural phytoplankton
 communities in the water  source, particularly  if source  water chlorination is
 practiced. Several techniques, the most popular of which is treatment with copper
 sulfate, are available for controlling algal populations in lake and reservoir waters.

   Prevention of Salt Water Intrusion—The data from Lange and Kawczynski show
 that in Contra Costa, CA, sea water intrusion during a drought caused the bromide

     Section VII.  Treatment Techniques to Remove Trihalomethane Precursors  123

-------
content of the source water to increase.30 This increase in bromide content caused
consistently higher yields of trihalomethanes (Figure 5, Section III) and aggravated
attempts to control trihalomethanes  because of the  faster formation rates of
bromine-containing trihalomethanes. Although in this case the end of the drought
caused the source water quality to return to normal, water utility personnel faced,
with a  continually increasing sea  water intrusion problem might consider the
development of an underground fresh water barrier created by injection wells or
spreading basins as one technique to reduce the type and concentration of TTH M's
in their chlorinated finished water.

Discussion-
   Utility managers should carefully consider the potential for altering the quality of
their source water to lower trihalomethane precursor concentrations reaching the
treatment plant. Periodic determinations of source water trihalomethane precursor
concentrations (THMFP) may reveal control measures  that could be taken to
minimize these concentrations.  These measures may include control of algae,
prevention of salt water intrusion,  or selected uses of alternative sources. When
alternative sources  of water  are considered, THMFP determinations should be
carried out over the range of conditions likely to be present in the distribution system
to verify conclusions drawn about effect of changes in source water quality on the
ultimate trihalomethane content of distributed water.

Aeration

General Considerations—
   Because the primary trihalomethane precursors are now understood to be high-
molecular-weight humic and fulvic acids, aeration would not be expected to be
effective for precursor removal. Nevertheless, aeration was  briefly evaluated in-
house by USEPA for reducing THMFP in Ohio River water.

 Experimental Results—
  With the use of the diffused-air aerator described  in  Section VI, Subsection
Aeration (Experimental Results),  river water was aerated  at varying air/water
ratios,  then chlorinated and stored at 25°C (77°F) for 2 days in sealed vessels. A
companion river water sample was chlorinated and stored under the same conditions
without being aerated. The  data in Table 37 show the influence of aeration on
TH M FP to be insignificant (less than 10 percent), even at an air/ water ratio of 20/1.
As shown earlier in Figure 52, the chloroform formation potential also remained in
an aerated tap water sample.

Discussion—
   As would be expected, this technique is not effective for trihalomethane precursor
removal.

Oxidation

General Considerations-
   Several oxidants have been investigated by USEPA and others to determine
whether or not they would be effective in oxidizing precursor material and  thereby
reducing the trihalomethane concentration after chlorination. The oxidants studied
were ozone,  chlorine  dioxide,   potassium   permanganate, ozone/ultra-violet
radiation, and hydrogen peroxide.
   Two goals are desirable when these oxidants are applied: 1) the stated objective of
lowering THMFP by chemically altering the precursor materials, and 2) complete
chemical oxidation of the precursors (to carbon dioxide) to eliminate the potential
problem of the presence after treatment of oxidation byproducts possibly more

124 Treotmant Techniques for Controlling Trihalomethanes in Drinking Water

-------
   TABLE 37. EFFECT OF AERATION (10-MINUTE CONTACT TIME)
                         ON REDUCING THMFP

                                  Trihalomethanes, ng/L after 2-
                       Air/water  day contact time at 25°C <77°F)TermTTHM,
Type of water ratio (V/V> CHCI,
Ohio River water
Ohio River water with
1 3 mg/L CI2 (control)
Aeratedf Ohio Riverwater
Aerated Ohio River water
Aerated Ohio Riverwater
Aerated Ohio Riverwater
Aerated Ohio River water
Aerated Ohio Riverwater
—

—
1:1
4:1
6:1
8:1
10:1
20:1
NF"

66
66
64
62
62
59
61
CHBrCI,
NF

28.0
27.8
26.8
25.8
26.8
25.6
26.0
CHBraCI CHBr, M9/L
NF NF NF

8.0 <0
8.0 <0
6.6 <0
7,6 <0
7.8 <0
7.7 <0
8.0 <0

.1 102
.1 102
.1 97
.1 95
.1 97
.1 92
.1 95
*None found.
tActlvated-carbon-filterod air.

harmful than the trihalomethanes. As will be seen below, the first of these goals is
accomplished to some degree in some cases. The second goal is  not usually
accomplished, which indicates that oxidation byproducts remain in the treated
water. Comparatively little is now known about the nature of these materials, but
this information can  be found summarized  later in  Section VUI, Alternative
Disinfectants.
  The  results summarized below mainly  indicate the potential of oxidation
techniques for achieving the goal of lowering THMFP.

Experimental Results—
   Ozone—The  USEPA in-house  studies used the  ozone contactor described  in
Section VI, Subsection Oxidation. In the continuous-flow studies, unchlorinated
Ohio  River water  was coagulated, settled,  and  filtered before ozonation. Three
different applied ozone doses were used at a constant 5- to 6-minute contact time.
Following ozonation, the samples were  chlorinated and stored for 6 days at 25°C
(77° F).
  Ozonating  for a few minutes'  contact time with small dosages followed by
chlorination  produced  slightly  more  chloroform  and  TTHM's than with
chlorination alone (Table 38). This means that theTH MFP was not reduced by low-
level ozonation, and subsequent chlorination to produce a disinfectant residual in
the distribution system would result in trihalomethane production. The reason that
low-level ozonation plus chlorine produced more chloroform than chlorination
alone is not known, but the effect has been seen by others. Possibly because the ozone
satisfies some of the oxidant demand, more chlorine is available for the trihalo-
methane reaction.  But because of the high chlorine dose  used  (8  mg/L), this
explanation does not seem likely, and a change in the organic precursors must be
assumed. The reduction in bromine-containing trihalomethanes is probably caused
by  oxidation of bromide to some nonreactive species (possibly bromate)  by the
ozone.24*25 The applied ozone dose of 227 mg/ L may have completely oxidized some
of the trihalomethane precursors, thereby reducing the  chloroform formation
potential from 91 to 62 jig/L (32 percent), and the TermTTHM by 43 percent.
  To observe the effect of longer contact times and generally higher ozone doses, the
ozone  contactor was  used as a  batch  reactor in a second test rather than a
continuous, countercurrent reactor, as in previous runs. The THMFP of Ohio River
water can be reduced  by ozone (Figure 74), but  the contact time is probably un-
realistic for water  treatment (several hours). The ozone application rate for this
batch study was 43.5 mgO3/ minute applied to approximately 13 liters of river water,

     Section  VII. Treatment Techniques to Remove Trihalomethane Precursors  125

-------
            TABLE 38. EFFECT OF OZONATION ON THMFP»
                Chlorine
    Appliedf  dose after
      j dose,  O, treatment.
Trihalomethanes, ng/L
 Term   Percent
TTHM, TermTTHM
Fast
1

2

3

t mg/L
0*
0.7
0$
18.6
0*
227
mg/L
8
8
8
8
8
8
CHCI3
6
15
12
14
91
62
CHBrCI,
14
8
9
8
26
7
CHBr2CI
4
3
2
8
6
1
CHBra
NF§
NF
NF
NF
NF
NF
^g/L
24
26
23
30
123
70
removal
— . •
-8
— .
-30
—
43
'Stored for 8 day* at 26°C (77°F). Duil-modla filttr affluant; continuout-flow itudias; 5- to S-minuta contact
 t!m*.
        oM, contintiou*-f1ow itudtas, mg/L =
         mg Oj _   standard Htar* ofnaM CO| *nOal       minuta
 standard Ktar of gas {Oa •*• Os|

 t Control.
 JNono found.
                                   minute
                                                    liters of water
              90
              80
              70
              60-
              50
            .
           x 10 •
             30
             20
              10
                 0       1       2      3       456       7
                                OZONE REACTION TIME, hr

          Figure 74.   Batch treatment of Ohio River water with .ozone.
                       13-L batch reactor; 3,3 mgOi/L/min.THMFPcondi-
                       tions: pH not reported; 25°C (77°F); storage time, 6
                       days.
 726  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
or about 3.3 mg Oj/ L per minute. In this batch test, the calculated gas/water ratio
for the 6-hour contact time is approximately 14:1; therefore, the observed effect was
caused by ozone oxidation and not merely gas stripping, as aeration alone at a 20:1
air/water ratio was ineffective for reducing the THMFP concentration (Table 37).
  Glaze  et al. studied the potential of ozone  for oxidation of trihalomethane
precursors in Texas lake water.40 An example of their findings using a 22-liter batch
reactor and three different  ozone doses is shown in Figure 75: With sufficient
exposure to ozone, substantial removal of trihalomethane precursor occurred. As in
the USER A in-house study (Table 38), an initial drop in precursor concentration was
followed by an increase with a small additional amount of ozonation,  which was
followed by a further decline when more ozone was applied.
                    30
                              60       90        120

                           OZONE REACTION TIME, min
                                                          150
                                                                    180
         Figure 75,   Ozone destruction of trihalomethane precursors in
                     Caddo Lake, TX, water. THMFP conditions: pH 6.5;
                     26°C (79°R; storage time, 3 days.40

  To confirm these results, Glaze  et al.  assumed the initial  rate of precursor
disappearance to be exponential and subtracted this projected decay curve from the
actual data. The plot of this difference showed the appearance and then destruction
of a material called "byproduct precursor" by these workers (Figure 76). A similar
result was shown by Riley et al.  (Figure 77), but because their samples were stored
for the determination of TermTHM concentrations at different pH  values, their
results are difficult to interpret' precisely.
  To determine what success other investigators have had in oxidizing trihalo-
methane precursors, Trussell" and Trussel and Umphres" reviewed the literature
and found eight references to this type of work. These data (Table 39) show great
variation in performance, but  this is not surprising because of the variations in

     Section VII, Treatment Techniques to Remove Trihalomethane Precursors   127

-------
                                 Curve A: 0.14 mg Oj/L-mln

                                 Curve 8: 0.28 mg Oa/L-min

                                 Curve C: 0,42 mg Oj/L-min
                                 Exponential decay of initial trihalomethane
                                 precursor
                                 Residual curve for formation and
                                 decay of byproduct precursor
                               60       90       120

                          OZONE REACTION TIME, min
                                     150
                                               180
          Figure 76.
Analysis of THMFP destruction curves for Caddo
Lake, TX, water.40
experimental conditions among these studies—not the least of which are  the
conditions under  which TermTHM's are measured. Taken in the aggregate,
however, the data do indicate the potential of trihalomethane precursor oxidation by
ozone for prevention of formation of trihalomethanes even though ozone doses and
contact times much higher than those used for disinfection  may be required.

  Chlorine  Dioxide—Miltner  investigated  the effect  of  chlorine  dioxide  on
trihalomethane precursors with both raw Ohio River water and prepared humicacid
mixtures." In the first part of the study, raw Ohio River water was divided into two
samples, one of which was treated with 2 to 3 mg/L chlorine dioxide generated by the
method of Granstrom and  Lee." Both samples were stored for 48 hours, after which
aqueous chlorine was added to both samples. During the 48-hour storage period, the
chlorine dioxide was consumed by the raw water.
  The results of this experiment  show that chlorine dioxide was  altering  the
precursor, because chlorination of the chlorine dioxide-treated water resulted in

128   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
        1,6
   Q
   LJJ
   O
   3
   Q
   O
   K
   Q.

   O

   O
           O     2     4      6      8    10    12     14    16    18    20

                       OZONE/HUMIC ACID CARBON,  mol/mol

          Figure 77,   The influence of ozonation on trihalornethane pre-
                      cursors at various pH's. THMFP conditions: pH as
                      noted; temperature not given; storage time, 4 hr,95

lower TTHM concentrations than did chlorination of untreated water (Figures 78
and  79). On  the other hand,  the data in Table 40 (page 133) show that in some in-
stances, higher concentrations of bromodichloromethane and dibromochlorometh-
ane  were formed when the water was treated with chlorine dioxide. The  reason for
these results  is unknown and may even be analytic error.
   In the second  phase of the Miltner study,  two 5 mg/ L humic acid mixtures were
prepared.*'*  One  sample was  treated with  2 to 3 mg/L  of laboratory-generated
chlorine dioxide, and both samples were stored for 48 hours, during which time the
chlorine dioxide in the treated sample was consumed. Both mixtures  were then
chlorinated.  Again,  chlorine  dioxide  was  reacting  to reduce  the  precursor
concentration, as shown by the reduction in chloroform concentration (Figure 80,
page 134). In this case, chloroform was the only trihalomethane produced. Although
this  work does demonstrate the ability of chlorine dioxide to alter precursor materi-
als so that it  does not participate in the trihalomethane formation reaction, as with
ozone, the conditions used here are not typical of water treatment practice. The use
of chlorine dioxide in a more typical  manner  will be reported in  Section VIII.

   Potassium  Permanganate—A speculation by  Rook21 that  the  reaction of
precursors   to  form  trihalomethanes  was  characteristic  of those  of  m-
dihydroxyphenyl  moieties led  to  some unpublished  USEPA  experiments on
treatment of resorcinol and  m-dihydroxybenzoie acid solutions with  potassium
permanganate at low dosages.  As expected, this treatment was nearly 100 percent
•The humic acid solution was made using 5 mg of humic acid (Aldrich Chemical Company) mixed in I liter of distilled water
 that had been passed through a Super-QJMilKporc Filter Co.) filler and redistilled in glass; thepH was then adjusted to 10.
 After mixing, this solution was adjusted to pH 7 and mixed  for several hours.
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors   129

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      TABLE 39. TRIMALOMETHANE PRECURSOR REDUCTION
                            WITH OZONE2««2B
Location
Owens River
Lake Casitas
Columbia River
Columbia River
Columbia River
Columbia River
Ohio River (Louisville}
Ohio River (Louisville]
Ohio River (Louisville)
Ohio River (Louisville)
Ohio River (Louisville)
Bay Bull's Big Pond
Bay Bull's Big Pond
Bay Bull's Big Pond
Mokelumne Aqueduct No. 2
Mokelumne Aqueduct No. 2
Mokelumne Aqueduct No. 2
Mokeiumne Aqueduct No. 2
Middle River
Middle River
Middle River
Middle River
Middle River
Rotterdam
Rotterdam
Orange County
Ozone
dose,
mg/L
1.0
2.0
0.5
1.0
2.0
4.0
1.0
2.0
4.0
6.0
8.0
1.0
2.0
3.0
2.0
3.4
4.5
6.0
2.6
2,8
5.5
10
11
2
8
1.0
Percent
TermTHM-
reduction
78
6
8
14
16
16
6
22
30
46
46
13
19
27
62
59
59
53
-13
-3
32
7
22
60
50
7
*M*»iurem*nt condition* not specified.


effective in preventing the formation of trihalomethanes upon later chlorination of
these  substances.  To  investigate whether or  not treatment  by  potassjum
permanganate would remove trihalomethane precursors, Ohio River water was
dosed  with  potassium  permanganate,  stored, and subsequently chlorinated.
Chlorination in these experiments was carried out in the presence of the precipitated
manganese dioxide as well as excess, unreacted potassium permanganate. Therefore,
apparent lower precursor concentrations after treatment cannot be attributed to
precipitation and therefore are  likely to be the result of the  oxidation process.
Selected data from this experiment (Table 41, page 134) indicate limited success in
removing trihalomethane precursors from Ohio River water. The results were variable,
depending on conditions of both potassium permanganate and chlorine treatment.
Note that when potassium permanganate treatment and chlorination are both
carried out at high pH (experiment 2,3), the treatment for precursors does not appear
to be as effective as when both are carried out at neutral pH (experiment 1,5). The
overall yields of trihalomethanes are also greater at high pH (not shown). The reverse
is true, however, when the chlorination pH is a constant  7.0 (experiment  1,6),
showing that potassium permanganate is a better oxidant for precursor removal at
high pH.
130  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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                                   8 mg/L chlorine *
                                   Untreated Water
                  8 mg/L chlorine * 2 to 3 rng/L CIO, Treated Water
                              20          30

                            REACTIONTIME.hr
     Figure 78,    TTHM concentration after chlorination of chlorine
                  dioxide treated and untreated.Ohio River water, pH
                  7.6; 25°C (77°F).»
Section VII. Treatment Techniques to Remove Trihatomethane Precursors  131

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                                                8 mg/L chlorine +
                                                Untreated Water
           	/  /  8 mg/L chlorine + 2 to 3 mg/L CIO, Treated Water
                                     20          30

                                  REACTION TIME, hr
          Figure 79.   TTHM concentration after chlorination of chlorine
                       dioxide treated and untreated Ohio River water, pM
                       6.8; 25°C (?7°F).39
132   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
to
n>
3-

t
:?
3=
8"
                      TABLE 40. EFFECT OF CHLORINE DIOXIDE ON TRIHALOMETHANE PRECURSOR
                                       CONCENTRATION IN OHIO RIVER WATER39

Type of
water
Raw water (control)
cio,-
treated water§
Raw water (control)
cio2-
treated water§


Free chlorine, mg/ L
Dose
8

8
8

8
Residual
Vest

Yes
3.9

4.7
Storage
time.
hours
24

24
47.5

47.5




Trihalomethanes, ftg/L
CHCI,
59

30
76

41
CHBrCIa
18.5

15
21.6

23
CHBr,CI
4

8
4

13
CHBr,
NFJ

NF
<0.4

NF
Term
TTHM,»
(tmol/L
0.628

0.382
0.765

0.547
Percent
reduction
TTHM
—

39
—

29
                'Tcmparatin*. 2S°C |77°F|; pH, 6,8, dorage lima as shown.
                fNot quantified,
                {Nona found.
                $2 mg/L CIO,.

-------
        120
        100
                       8 mg/L chlorine * 3 mg/L ClOj Treatad Humic Acid     	
                        10          20         30

                                REACTION TIME, hr
                                                        40
                                                                  50
          Figure 80.
Chloroform concentration  after  chlorination  of
chlorine dioxide treated and untreated humic acid
solutions. pH 7,0; 25°C {77°f).M
     TABLE 41. TRIHALOMETHANE PRECURSOR REMOVAL BY
       POTASSIUM PERMANGANATE IN OHIO RIVER WATER
            KMnO4 reaction
                                       Chlorine reaction
Expert- Amount Reaction
ment added, time.
No. mg/L hours pH
1

2

3

5

6

0
5
0
5
0
6
0
10
0
10
1.5
1.5
1.5
1.5
1.5
1.5
21
21
21
21
7.1
7.1
9.3
9.3
10.2
10.2
7.0
7.0
11.6
11.5
Cl,
added,
mg/L
10.5
10.5
10.5
10.5
10.5
10.5
8.9
8.9
8.9
8.9
Total
oxidant
residual,*
mg/L
9.3
13.5
9.1
13.3
9.1
13.5
6.0
14.7
6.0
12.9
Reaction Percent
time, TermTTHM
hours pH reduction
2
2
2
2
2
2
24
24
24
24
7.0
7.0
9.0
9.0
9.9
9.9
7.0
7.0
7.0
7.0

15.4

2.7

5.6

25.0

35.3
•Recorded *s mp/L Cl, and includes axcost unreacted KMnO4 {where applicable) at wall BI chlorine,

134  Treatment Techniques for Control/ing Trihalomethanes in Drinking Water

-------
  Singer et al. conducted similar experiments using the raw water supplies of Chapel
Hill and Durham, North Carolina," Both are surface supplies with high TH MFP.
These experiments also demonstrated greater effectiveness of potassium perman-
ganate treatment at high  pH values when chlorination  was carried out near
neutrality.  Removals of 30 to 40 percent were reported when potassium  perman-
ganate treatments of 10 nig/ L were carried out at pH 6.5 and 10.3, respectively.
Because these samples were filtered before chlorination, some of this removal is the
result of precursor precipitation with manganese dioxide, although this effect was
considered  by the authors to be much less than  that caused by the oxidation
mechanism. In their conclusions, the authors state that potassium permanganate can
decrease the chloroform formation potential of a water and that the extent of this
decrease is  related directly to the potassium permanganate dose. In addition, at the
pretreatrnent doses of potassium  permanganate normally employed (1.5 mg/L or
less), the effect of this treatment  is relatively small, and accordingly, if potassium
permanganate is to be used specifically for this purpose, much larger doses will be
required.

  Ozone—Ultra-violet  Radiation—To determine whether or not irradiating water
with ultra-violet light while treating it with ozone (Oj/UV) would enhance the
destruction of trihalomethane precursors, Glaze et al. treated a precursor-rich lake
water with Oj/UV.40 Although they did not examine ozone alone as a control in this
study, their data (Figure 81) do show that at a constant ozone dose, a 4-fold increase
in radiation intensity reduced the treatment time to reach 100 /ug/ Lof THMFP(3-
day, pH 6.5,  26°C [79° F]) from 40 to 21 minutes in the batch reactor. This result
shows that increased quantities of U V energy enhance the removal of precursor when
ozone is used.
      400
      380
                                          Ozone Dose    UV Intensity.
                                        Rate, mg/L-min     W/L
                                             4.00
                                             4.18
                                             4.09
0.096
0.196
0,40
                 10
                        20    30     40    50    60     70

                         OZONE/UV REACTION TIME,  min
                                                               80
                                                                     90
         Figure 81.  Destruction of trihalomethane precursors in Cross
                     Lake, TX, water by Oj/UV. THMFP conditions; pH
                     6.5; 26°C (79°F); storage time, 3 days.40
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  135

-------
  Hydrogen Peroxide—Hydrogen peroxide has been suggested as an oxidant that
could be used for the removal of trihalomethane precursors. This possibility has been
briefly studied by two investigators,98*9* but unfortunately, both used the unrealistic
direct aqueous injection method28  of  estimating precursor concentrations (see
Section IV). Conclusions on  the usefulness of hydrogen peroxide for precursor
oxidation therefore cannot  be made,

Discussion-
  Each of the oxidation techniques discussed in this subsection—ozone, chlorine
dioxide,  potassium permanganate,  and ozone/ultra-violet  radiation—had some
effect on THMFP concentrations. Doses of the oxidants were higher and contact
times longer, however, than normally used in disinfection practice to accomplish
significant lowering of THMFP. Further, although the precursor materials were
altered so that they no longer could participate in the trihalomethane formation
reaction, these studies did not determine the exact fate of these materials. Thus, the
possibility of creating undesirable byproducts from these oxidative reactions cannot
be ruled out at this time. This means that batch and pilot studies will be required on a
case-by-case basis to determine the ultimate applicability of oxidative techniques for
lowering THMFP. Oxidation  reactions of precursor materials are likely to be rather
complex, and byproducts obtained will vary significantly with reaction conditions,
as will removals of THMFP. Finally, waters high in bromide that produce high
concentrations of TTHM  might be treated  with  ozone to  retard or prevent the
formation of the bromine-containing trihalomethanes, thereby lowering theTTH M
concentrations. More work will be needed to investigate this possibility.

Adsorption

Powdered Activated Carbon (PAC)—
  General Considerations—Because trihalomethane precursors  are a mixture of
many organic chemicals, and this mixture varies from location to location, treating
adsorption of these substances in a theoretical manner is much more difficult than
treating the adsorption of  the individually identifiable and quantifiable trihalo-
methanes. Aquatic humic materials,  a major  contributor to trihalomethane
precursors, are not themselves a single substance. Unlike the individual trihalometh-
anes, the characters of these acidic materials are influenced  by numerous variable
factors that will influence  their adsorbability. These factors include  molecular
weight distribution, pH, inorganic  ions  present,  precursor source, and relative
fractions of humic and fulvic  acids.8*
  These variables are beyond  the influence of the physical-chemical characteristics
of the solution on the activated carbon surface itself (which, of course, will affect the
adsorption of even pure substances). Also, trihalomethane  precursors cannot be
measured directly, but only by  the  resulting   trihalomethanes formed upon
chlorination of a test sample. Furthermore, the quantity of trihalomethanes formed
depends on the test conditions selected, time of storage, temperature of storage, and
storage pH. The mixture of trihalomethanes formed as well  as their total quantity
will  depend  on the bromide concentration in   the water. Thus experimental
adsorption results seemed likely to be quite variable, depending on the water being
treated for precursor removal. Nevertheless, several studies have been conducted
that attempt to demonstrate how the TH MFP (in pmol/ L) is lowered by treatment
with various doses of PAC. These studies are reviewed  here.

  Experimental Results—An  in-house USEPA study assessed the effectiveness of
PAC on the removal of trihalomethane precursors from Ohio River water that had
been coagulated and settled. This water was dosed with varying concentrations of
PAC, mixed at 100 rpm for 2  minutes, and centrifuged for 20 minutes at 1,500 rpm
(480 gravities). The supernatant liquor was then decanted and chlorinated. These

136  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
samples were then stored for 2 days at 2S°C (77°F) (pH was not recorded). Four
studies were  made with three brands of PAC. Extrapolation from the  resulting
adsorption isotherms from three of the studies (Figure 82) show that about 43 mg/ L
of PAC would be required to reduce the TH M FP from 1 toO.5 jimol/ L in this water.
The adsorption isotherm for the Watercarb® material is atypical and indicates that it
would not be an effective adsorbent for trihalomethane precursors (Figure 82),
       0.02
       0.01
    o>
    E
   u
    m
    tr
    O
   z
   a
O  Oarco® M
•  Nuchar Aqua®

D  Walercarb®
       0.001
       0.0005 - -
            0.1
         Figure 82.
      0.2           0.4      0.6   0.8  1.0

      EQUILIBRIUM THMFP (Cf), nmol/L

  Adsorptjon isotherms from three studies using PAC
  to remove trihalomethane precursors from coagu-
  lated and settled Ohio River water. THMFP condi-
  tions: pH, not reported; 25°C (77DF); storage time, 2
  days. (Darco® M manufactured by ICI America. Inc.,
  Atlas Chemical  Division, Wilmington, DE 19899;
  Nuchar Aqua© manufactured by Westvaco Corpora-
  tion, Covington, VA 24426.)
    Section VII. Treatment Techniques to Remove Trihalomethane Precursors  137

-------
  A project at the New Orleans,  LA, water utility was reported by Lykins and
DeMarco.100 The adsorption isotherm from these data for raw Mississippi River
water (Figure 83) would indicate that about 77 mg/ L of PAC would be required
to reduce the THMFP concentration from 1 to 0.5

       0.1
                    I
    en
    N,
    ai
    M 0,01 --
    CC
    o
    V)
    o
    CD
    5
    §
     0.001
                         I
           0.1
         Figure 83.
                               0.5
                                         1.0
                                                             5.0
                                                                      10
                            EQUILIBRIUM THMFP (Cf).
                     Adsorption isotherm from New Orleans, LA, study
                     using PAC to remove  trihalomethane precursors
                     from Mississippi River water, THMFP conditions: pH
                     10; 29°C (85°F);-storage time, 5 days."50 (Hydro-
                     darco® 8 manufactured by ICI America, Inc., Atlas
                     Chemical Division, Wilmington, DE 19899.)

  Other studies have been reported in  the literature showing various degrees of
effectiveness for the removal of trihalomethane precursors by PAC,54'"" but the
above two examples seem to illustrate a range of applicability of this technique.
  Discussion—The results presented clearly indicate that the effectiveness of PAC at
any given location will be subject to wide variability because of the-factors outlined
under General Considerations  in this Section as well as the characteristics of the
selected  PAC  itself. Case-by-case studies will be required to determine the actual
effectiveness of this treatment technique. In general, doses of PAC much higher than
conventionally used in existing water treatment practices seem to be required to
obtain significant removals of trihalomethane precursors.
Granular Activated Carbon (GAC)—
  General Considerations—Section VI included a discussion of factors influencing
adsorption of pure materials (trihalomethanes) and a general description of the
performance characteristics of a typical dynamic adsorption system compared with
those of a theoretical plug flow system in which simple equilibrium calculations can
be used to estimate times to "exhaustion." The data that followed in that section
138  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
indicated that equilibrium calculations based on PAC isotherms were of marginal
utility in predicting performance of the GAC systems studied.  Kinetic  effects,
influencing the shape of the mass transfer zone, and other factors were important in
causing significant deviations between column  performance predicted solely from
isotherm data and actual experimental results. This was the case even when the
targets  of  treatment, were well-known  and reproducible  experiments  could  be
conducted.
   As discussed  above for PAC  adsorption  of precursors, many more  factors
influence  the  results  of adsorption  experiments  involving  trihalomethane
precursors.  Although  isotherm data may  prove to be useful to determine the
feasibility of using GAC adsorption for the removal of precursors under a given set
of circumstances, little is to be gained by attempting to estimate adsorber life in a
general sense because of the variables between systems.
   Furthermore,  as will be seen below, GAC adsorbers do not typically reach
"exhaustion" at all. The equilibrium state (influent equals effluent concentration)
rarely, occurs in practice, and a "steady state" condition prevails over a long period of
time.  Under  this condition,  the  effluent concentration of THMFP  remains
significantly below that of the influent. This is usually considered to be the result of
biologic activity within the bed, although other explanations have been proposed.102
   Therefore, because of these general considerations, no attempt  will be made to
predict dynamic  GAC adsorber  performance from a given set of equilibrium
(isotherm) data.  The following is a compilation of experimental results from pilot
and field studies that will be used to develop a general picture of the effectiveness of
the GAC adsorption technique for removal of precursors.

   Experimental Results—For the in-house USEPA studies, a pilot water treatment
plant was fabricated to provide a continuous supply of treated but unchlorinated
water' for trihalomethane precursor removal studies. To minimize contamination
from structural materials, the pilot plant was built almost entirely of stainless steel,
Teflon®, and glass,  and it  was  housed  in  a room kept  free from  organic
contamination in trie air. Through the assistance and cooperation of the Cincinnati
Water Works, Ohio River water was provided  as a source of raw water. The pilot
plant employed conventional alum coagulation, .flocculation,  and sedimentation;
the unchlorinated settled water was pumped through GAC adsorbers fabricated with
glass columns 3.7-cm (1.5-in) in diameter. For this st.udy, two depths of GAC were
used: A 76-cm (30-in) deep bed of coal-based GAC and a 150-cm (60-in) deep bed of
lignite-based GAC. The THMFP was evaluated by chlorinating influent and effluent
samples 'from  the  adsorber  and  comparing  the   resulting  trihalomethane
concentrations.
   The results from the 76-cm (30-in) deep coal-based GAC system with a 9-minute
EBCT (Figure 84) show three important points: (1) when fresh, this GAC adsorbed
nearly all of the trihalomethane precursors from this water, as shown by the low
concentrations of trihalomethanes  formed when  the fresh  GAC effluent was
chlorinated; (2) some trihalomethane precursor began" to pass the adsorber almost
immediately, as shown by the steady rise in the concentration of trihalomethanes
produced upon chlorination of the GAC effluent; and (3) because of the faster
reaction between bromine and precursor compared with chlorine and precursor, the
bromine-containing trihalomethanes wil! be formed first (if bromide is present in the
water) as the trihalomethane precursor begins to break through a GAC adsorber and
the effluent is chlorinated.
   For example,  in  Figure 84, the concentration of dibromochloromethane in^the
chlorinated  effluent sample equalled the concentration in a chlorinated influent
sample at 4 weeks, whereas the concentration of bromodichloromethane in the
chlorinated effluent sample did not equal the concentration in a chlorinated influent
sample until the 8th week. Furthermore, the concentration of chloroform in the"
chlorinated  adsorber  effluent  sample did  not equal the concentration  in  a
chlorinated influent sample until the 13th week. Thus, the first precursor to penetrate
      Section VII. Treatment Techniques to Remove Trihalomethane Precursors 139

-------
              Influent Chloroform Formation Potential
              (Chlorinated GAC Influents        x.
                                                  Chlorinated GAC Effluent
                       I          I           I          I
               Influent Bromodichloromethane Formation Potential
               (Chlorinated GAC Influent!
                                                  Chlorinated GAC Effluent
               Influent Dibromoehloromethane Formation
               Potential
              (Chlorinated GAC Influent)
                                                  Chlorinated GAC Effluent
        10
                                10         15        20
                                TIME IN OPERATION, wk
         Figure 84.   Removal of trihalomethane  precursors from Ohio
                      River water by coal-base GAC.  Test period, March-
                      October 1975; GAC type, Filtrasorb®200; beddepth,
                      76 cm (30 in); hydraulic loading, 5 m/hr (2 gpm/ft2);
                      EBCT, 9 min. THMFPconditions: pH 6.5; 20°C{68°F);
                      storage time, 4 days.
14O  Treatment Techniques for Controlling Trihatomethanes in Drinking Water

-------
the adsorption system reacted with the active bromine species to form dibromo-
chloromethane. Apparently insufficient bromide was present to cause formation of
the pure-halogen trihalomethane, CHBr3,
  These data would indicate that for  this adsorbent, exhaustion for precursor
removal occurred about the 13th week in this system with a 9-minute EBCT. The
influent to this system contained approximately 0.28 /itnol/L of THMFP,
  The data for the deeper lignite-based GAC adsorber with an 18-minute EBCT
(Figure 85) show the same results as noted above—good precursor removal at first,
bromine-containing trihalomethanes being formed as precursor materials begin to
break through, and a fairly rapid breakthrough of precursor. These data do show
one important difference, however. In this  case, some removal of trihalomethane
precursor was taking place even after 30 weeks of operation. This effect is shown
particularly by the difference in the concentrations of influent chloroform formation
potential and the chloroform formed upon chlorination of the adsorber effluent.
  The service time to exhaustion of the bed with an 18-minute EBCT might be
expected to be twice as long as that with 9 minutes even though different sources of
granular activated carbon were used, but removals continued much longer than
expected in the deeper bed. Although the GAC source is one explanation for this,
biodegradation of precursor within the bed is also considered to be a factor.
  A Huntington, WV, project18 and a Jefferson  Parish, LA, study14 confirmed the
results obtained in the pilot  plant  studies—good  removal of trihalomethane
precursors early in the test, fairly rapid  breakthrough of precursor materials,  and
lack of true exhaustion,  possibly because of biologic activity (Figures 86 and  87).
These two sets of data also show the predicted general relationship between EBCT
and time to reach steady-state operations  (defined  as the service time when the
percentage of trihalomethane precursor being removed is no longer declining). For
the Huntington, WV, system, this condition was reached at about 6 weeks for an
EBCT of 7.1  minutes; whereas for the Jefferson  Parish study, the time to reach
steady-state conditions was about 20 weeks  for a 23-minute EBCT. Table 42 (page
145) summarizes the data from the USEPA projects and from selected literature
citations on the performance of GAC adsorption as a unit process for removing
trihalomethane precursor. These data are ranked in ascending EBCT order to show
as far as possible the influence of longer EBCT's on the  rate of trihalomethane
breakthrough and the percent of precursor removed during steady-state operation.
Influent THMFP and sample storage conditions for the THMFP test are given to
assist  the reader in selecting examples of treatment conditions most appropriate for
comparison with a particular utility.
  With the data of Wood and DeMarco from Miami, FL," a bed-depth service time
plot68 was constructed for the removal of trihalomethane precursors at that location
(Figure 88, page 148). These data show that the minimum adsorber bed depth is
19 cm (7.5 in) to remove THMFP to 200 /ug/L and 32 cm (12.5 in)  to reach
100 pgl L from an average influent concentration of 434 /ag/ L. Of course, if a lower
target were chosen, the minimum bed depth would be correspondingly greater. Note
that because trihalomethane precursors are a mixture of compounds, they do not
behave as  pure substances behave.  For example, using additional data from  this
study, the bed-depth service time plots for target concentrations of 50 and 20 /ug/ L
were nonlinear, but they did indicate a thicker critical depth. This approach to
adsorber design may have only limited application here.

  Discussion—The data in Table 42 confirm the generalized conclusions drawn
from  Figures 84  through  87: (1) GAC adsorption is initially  very effective for
trihalomethane precursor  removal; (2)  in practice, the rate of  trihalomethane
precursor breakthrough is fairly high; and (3) exhaustion (defined as an effluent con-
centration equal to influent concentration) usually does not occur, but rather a
steady-state  develops during which  a  rather constant percentage of precursor
material continues to be removed, possibly because of biodegradation.

      Section VII. Treatment Techniques to Remove Trihalomethane Precursors  141

-------
       75
       50--
       25
             Influent Chloroform Formation Potential
             (Chlorinated GAC Influent;
       45
       BO-
    or
    U-
             Influent Bromodichloromethana Formation Potential
             (Chlorinated GAC Influent)
                                                                      r"
                                              0-" -o                  '
                                              /     \      O-O-O-o	0-0*
                                           Chlorinated GAC Effluent
                                           J       *  y
             	0^
-------
       300
                             10      15       20       25
                              TIME IN OPERATION, wk
                                                             30
          Figure 86.
Removal of trihalomethane precursors by GAG at
the Huntington Water Corp. (WV). GAC type, WVW
14 x 40; bed depth, 76 cm (30 in); hydraulic loading,
6.1  m/hr (2.6 gpm/ft2); EBCT, 7.1 min.THMFP con-
ditions: pH 8.3; ambient temperature; storage time,
7 days."*
  Although the data (Table 42) are quite scattered, because of being collected in
different locations and because of different sample storage conditions for THMFP
measurement, adsorbers  with  longer EBCT's  removed  precursor  longer  and
demonstrated a higher percentage removal at steady state conditions. Because of the
variability  of waters  being treated and  the necessity of varying THMFP test
conditions  to approximate reaction  conditions experienced at a given utility,
drawing more concise conclusions is difficult. Thus, continuous flow pilot studies
must be performed at each location to determine the breakthrough patterns and
potential long-term removals at steady state to be expected in practice. Finally, as
trihalomethane precursor materials begin to break through a GAC  adsorber, if
bromide is present, the bromine-containing trihalomethanes appear first upon chlo-
rination because of the rapid oxidation of bromide by chlorine to an active bromine
species that  then reacts quickly with whatever precursor material is present (Figure
84).
Synthetic Resins—
   General Considerations—Ambersorb® XE-340, which was shown to be effective
for trihalomethane  removal (Section  VI,  Subsection,  Synthetic  Resins)  was
evaluated  to  determine  whether  or  not  it  could also  effectively  adsorb
trihalomethane precursors.

     Sect fan VII. Treatment Techniques to Remove Trihalomethane Precursors  143

-------
•"
c
8
                                                            10      12     14      16

                                                             TIME IN OPERATION, wk
                                                 18
                                                         20
                                                                22
                                                                       24
                                                                             26
 '

I
Figure 87.  Removal of trihalomethane precursors by post filter
           GAC adsorber, Jefferson Parish, LA. GAG type, WVG
           12x40; bed depth, 71 cm (28 in); hydraulic loading,
           1.9 m/hr (0.75 gpm/ft2); EBCT, 23 min. THMFPcon-
           ditions: pH 10; 21 °C (70°F); storage time, 5 days.1*

-------
TABLE 42. SUMMARY OF PERFORMANCE DATA FOR REMOVAL OF TRIHALOMETHANE PRECURSORS BY VIRGIN GAC ADSORPTION
V)
I
o'
3
5
i
0)
1
a
~
n
1
•3°
c
8
8
20
1
O
*
31
S,
3
n
1
"o

o
i
o
3
x
ft
location

Cincinnati, OH
Cincinnati, OH
Evansville, III
Cincinnati, DH
ML Climens, Ml


Mt Clemens, Ml
Evansville, IH
HuntingUn, WV
Davanport IA
Cincinnati, OH

Cincinnati, OH
Cincinnati, OH
Cincinnati, OH
Cincinnati, OH
Cincinnati, OK

Cincinnati, OH
Cincinnati, OH
Evansvilli, IN
Cincinnati, OH
Beaver Falls, PA
Continued
Type of GAC

WVG 12x30
HD 10x30
HD 10x30
WVG 12x40
HD 3000*


HD 30001
HD 10x30
WVW 14x40
Fiitrawrb® 400
WVG 12x40

WVG 20x50
WVG 12x40
HD 10x30
Filtrasorb® 200
Filtiasorii® 400

WVG 12x40
WVG 12x40
HD 10x30
Filtrasorb® 400
Filtrasorb® Ctt

Type of
system'

PC/PF
PC/PF
PC/PA
FS/SR
FS/SR


FS/SR
PC/PA
FS/SR
FS/SR
FS/SR

FS/SR
PC/PF
PC/PF
PC/SR
PC/SR

PC/SR
PC/SR
PC/PA
PC/PA
FS/SR

EBCT,
min

3.2
3.2
3.7
4.5
5.8


5.8
6.6
7.1
7.5
7.5

7.5
7.5
7.5
9.0
9.0

9.4
9.4
9.6
10.0
10.1

Approximate
percent
initial
THMFP
removal

97
97
84
95
81


75
87
93
UNK"
97

97
98
*><•>
97
88

95
93
89
93
"

Approximate
time to
steady-state
condrtions.t
weeks

4
2
6
2
4


4
6
6
>14
2

2
4
4
16
16

6
6
6
16
11

Percent
THMFP
removal at
steady-state
conditions

6
14
16
38
32


32
26
11
73
50

33
41
30
0
40

37
36
31
44
11

Influent
THMFP it
steady-state
conditions,

281
232
58
222
51


60
58
120
26
222

222
281
281
27
42

244
244
58
137
110

Sample storage
conditions
Time,
days

7
7
3
7
5


5
3
7
**
7

7
7
7
4
2

7
7
3
6
7

Temperature,
"CSS

29.4
29.4
17
29.4
25


25
17
20
•«
29.4

29.4
29.4
29.4
20
50

29.4
29.4
17
25
10-20

pH

9.2
9.2
8.0
9.2
7.3


7.3
8.0
8.3
..
9.2

9.2
9.2
9.2
6.5
' *«

9.2
9.2
8.0
7.8
7.4

Reference

30
30
63
30,62
NR§


NR
63
18
66
30,62

30,62
30
30
tt
tt

30
30
63
tt
18


-------
TABLE 42. (Continutd)
Treatment Tect,
3
5'
S
M
"•»,
*«
P
S*
S'
^
*
s*
5
tfi
0)
5'
5
3"
s-
I"

0)
S


Location

Jefferson Parish, LA
Baavar Fads, PA
Beavir Falls, PA
Cincinnati, OH
Cincinnati, OH
Jefferson Parish, LA
Jefferson Parish, LA
Jefferson Parish, LA
Cincinnati, OH
Cincinnati, OH
Jefferson Parish, LA
Jefferson Parish, LA
Cincinnati, OH
Jefferson Parish, LA
Menchester, NH


Manchester, NH
Jefferson Parish, LA
Jefferson Parish, LA
Jsfferson Parish, LA
Jefferson Parish, LA
Continued
Type of GAC

WVG 12x40
Filtrasorb® 400
HD 8x16*
WVG 12x40
HD 10x30
Filtrasort® 400
WVG 12x40
WVG 12x40
WVG 12x40
HD 10x30
WVG 12x40
WVG 12x40
HD 10x30
FUtrasorb® 400
WVW8x30


WVW 8x30
WVG 12x40
Filtrasorl® 400
FiHrasorb® 400
WVG 12x40

T»Daof
system*

PC/PA
FS/SR
FS/SB
PC/PF
PC/PF
PC/PA
FS/SR
FS/SR
PC/PA
PC/PA
PC/SR
FS/PA
PC/SR
FS/PA
FS/PA


FS/PA
PC/PA
PC/SB
PC/PA
PC/PA

EBCT,
min

11.0
11.3
11.4
11.8
11.8
12.0
14.0
14.0
16.0
16.0
17.0
18.0
18.0
19.0
21.7


21.7
22.0
22.0
23.0
23.0

Approximate
percent
initial
THMFP
removal

68
•*
•*
98
97
77
64
74
98
97
10
65
92
S3
78


82
18
82
69
55

Approximate
time to
study-state
conditioro.t
waaks

18
11
11
8
4
20
8
18
8
5
18
21
23
21
8


8
22
19
21
21

Pireart
THMFP
removal at
steatfy-slata
conditions

0
19
IB
40
34
17
21
11
60
35
13
14
49
25
52


47
20
44
39
20

Inllutnt
THMFP at
stsady-stato
conditions,
^g/L

251
110
110
230
281
273
281
319
230
259
319
192
73
365
138


133
235
343
365
192

Sample storaga
conditions
Time,
days

5
7
7
7
7
5
5
5
7
7
5
5
4
5
7


3
S
5
5
5

Temperature,
°C§§

30
10-20
10-20
29.4
29.4
30
30
30
29,4
29.4
30
30
20
30
28.5


28.5
30
30
30
30

PH

10
7.4
7.4
9.2
9.2
10
10
10
9.2
9.2
10
10
6.5
10
8.0


8.0
10
10
10
10

Reference

14
18
18
30
30
14
14
14
30
30
14
14
ft
14
103


103
14
14
14
14


-------
8"
I
QJ
        TABLE 42. (Continued)
reatment
«. Mmi(|Mi, DE 19815.
f N« nportrf.
        ttll-lH>H.
        SM« CMMreMr mliHi.
        §§f = t * t.l + 3J.

-------
                                   BED DEPTH

         Figure 88.   Bed depth-service times8* for trihalomethane pre-
                     cursor adsorption by GAC. THMFP conditions: pH
                     9.0; 22°C (72°F); storage time, 6 days.*7

   Experimental Results—Ambersorb® XE-340 was tested in Miami, FL, for its
 ability to adsorb trihalomethane precursors.104 In this case, two adsorbers with equal
 EBCT's  (6,2 minutes) were compared—one treating source "water, and the other
 treating  lime-softened and  filtered  water. The  data in  Figure 89 show  that
 Ambersorb® XE-340 is partially effective for the removal of THMFP from source
 water, but when treating water that had been pretreated by softening, the resin could
 no longer remove any precursor material.

   Discussion—In this case, the type of precursor material that was adsorbable on
Ambersorb* XE-340 also appeared  amenable to removal by coagulation  and
sedimentation, and the precursor materials that remained following lime softening
were not adsorbed on Ambersorb® XE-340. The generality of these observations has
yet to be demonstrated, however.

Ion Exchange

General Considerations—-
   Because synthetic resins designed for other purposes are often reported to become
fouled with organic contaminants while in service (Reference 105 as one example),
they have been examined  as possible trihalomethane precursor  adsorbents. Also,
because humie acids are anionic (particularly as the water becomes more alkaline),
anion exchange resins were considered as good candidates for the removal of
trihalomethane precursors,

Experimental Results—
   Strong-Base Anion Exchange Resins—Amberlite® IRA-904—A synthetic resin
manufactured by  the Rohm &  Haas Company, Philadelphia, PA  19105,  is
Amberlite®  IRA-904. This material, a strong-base anion exchange resin, is used as
an organic scavenger in some industrial  processes.  This  resin  was evaluated at
 Miami, FL.104  Amberlite® IRA-904 was  initially quite  effective for removing

148  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
       1000
        900
        800
        700
        600
    CD
    a.
     .
    5
    I
        500
        500
        400
        300
                     20
                              40        60       80
                             TIME IN OPERATION, day
                                                          100
                                                                     120
          Figure 89.
Removal of trihalomethane precursors by Amber-
sorb® XE-340; EBCT, 6.1 min.THMFP conditions: pH
9.0; 22°C (72°F); storage time, 6 days.10*
trihalomethane precursor materials in the source water (as measured byTHMFP), but
it was unable to remove any precursor material from water that had been pretreated
by lime softening (Figure 90), Either the residual precursor could not be exchanged
or the high  pH had an adverse influence on the resin itself. The unexchangeable
fraction of precursor material also existed in the source water, as the initial contactor
effluent concentration for  THMFP (Figure 90) was the same even when the bed
depth was doubled from 75 to 150 cm (30 to 60 in), with 9-and 18-minute EBCT's,
respectively.
     Section VII, Treatment Techniques to Remove Trihalomethane Precursors  149

-------
I
1
a
I
o'
c
f
I
J
3"
I
I'
I
                             800
                             700
                             100
                                                                                                   Finished Waltr  -
                                               influent
                                                    V
                                               EHIuentO.75ma.Srt)
    14         28       42
TIME IN OPERATION, day
   14         28        42
TIME IN OPERATION, day
                                         Figure 90.   Removal of ttihalomethane precursors by Amber-
                                                     lite® IRA-904; EBCT, 6.1, 12.2 miri. THMFP condi-
                                                     tions: pH 9.0; 22°C {72°F); storage time, 6 days,104

-------
   Asmit  A259—A   strong-base  anion  exchange   resin   manufactured  by
 AKZO/lmacti Div., Amsterdam, The Netherlands, was evaluated at the Rotterdam
 Waterworks by Rook,26 His results (Table 43) show some promise, although he
 stated that regeneration was necessary after 250 bed volumes of water were treated
 (the equivalent of less than 1 week of operation under normal circumstances). If
 regeneration were simple and inexpensive, this factor might not be a detriment.

TABLE 43. USE OF ASMIT A259 FOR REMOVALOFTRIHALOMETHANE
                           PRECURSORS" 2»

                                                                TTHM
                  	Trihalomethane formed. ftg/L	    formed,
Sample     	 CHCI,     CHBrCI,    CHBr,CI    CHBra      pg/L
Resin influent         28         13           8          6         55
Resin effluent          9          6        Trace        hi Ft        14

•Formation of trilwlomatnanas after 2 houn at 12°C (E4°F) and pH 7.6-7.9.
fNon* found.


   Weak-Base  Anion Exchange Resins—Recently, Rook and Evans studied two
 weak-base anion  exchange resins—A 20S, AKZO/lmacti Div., Amsterdam, The
 Netherlands, and  368 PR Duolite®, manufactured by Diamond Shamrock.106 Two
 columns with an 'EBCT of 5.1 minutes were used to treat Meuse River water after
 sedimentation in a Lamella separator and dual-media filtration. Several tests were
 made, and Table  44 summarizes the results from the three runs in which the most
 water was treated. Significant removal rates were shown for both resins. Note that
 these resins are regenerated with lime followed by hydrochloric acid. Also, note that
 as with G AC adsorption (see preceding Subsection Granular Activated Carbon), the
 formation of the bromine-containing trihalomethanes  is retarded the least during
 treatment for trihalomethane precursor removal. Again, an economic analysis
 would show whether or not these short  runs are economical.

  TABLE 44. USE OF WEAK-BASE  ANION EXCHANGE RESINS FOR
         REMOVAL OF TRIHALOMETHANE PRECURSORS* 10*


Resin
A 20Si
368 PR§
A20S
368 PR
A20S
368 PR
Bed
volumes
treated
1320
1320
1250
1250
1780
1780
Inst.
TTHM,
ng/L
92
92
71
71
57
57




Percent precursor removal
CHCIj
71
77
86
86
64
68
CHBrCI,
38
50
46
58
40
45
CHBr,CI
13
7
17
17
9
9
TTHMt
58
64
66
69
48
52
•24-hr ttorago, 20°C (68°F), pH 7.6 to 8.0
fMolar turn.
JA 20S AKZO/lmacti Div., Amsterdam, Th* NelhaHandt
§368 PR Duolite®, Diamond Shamrock.


Discussion—
   Of the anion exchange resins investigated, the weak-base resins studied by Rook
and Evans106 were the  most effective. With these resins, however, the maximum
length of the tests was  only 6.3 days, and the disposal of the regenerate (lime and
hydrochloric acid) may be a problem.

     Section VII. Treatment Techniques to Remove Trihalomethane Precursors 151

-------
Biologic Degradation

Central Considerations—-
   The data summarized in Table 42 show that steady-state conditions (during which
 a rather constant removal of trihalomethane precursors occurs) develop in GAC
 adsorption beds after some time of operation. One explanation for this effect is
 biologic degradation, in which the microorganisms are using the precursor materials
 —either adsorbed on the activated carbon surface or in the passing water—as a
 substrate. Several reports have indicated that preceding an adsorption step in a
 drinking water treatment train with ozonation (supposedly to fracture some organic
 molecules to make them more biodegradable) will improve  the performance of the
 combination  of the two processes over the performance of adsorption alone,
 presumably by enhancing the biologic degradation.""»108»10' Results showing both
 the presumed naturally occurring biologic degradation as well as enhancement by
 the addition of ozone are presented here.

Experimental Results—
   For the in-house USEPA studies to investigate this possibility, a 290-L/day (75
gpd)  pilot column system was set up to treat unchlorinated coagulated and settled
Ohio River water. Two 9-minute EBCT parallel columns were used; in one, settled
water was applied directly to a GAC bed, and in the other,  an oxygen plus ozone*
mixture was added to the water before the filter/ adsorber so that the ozone dose was
approximately  1.5 to  2.5 mg/L.  The  GAC-only  system reached  steady-state
conditions after 4 months (Figure 91), showing presumed natural biologic activity.
For each of the  10 months studied, the monthly average THMFP in the effluent of
the system with oxygen plus ozone treatment was always  lower than the control
system without oxygen plus ozone. This additional beneficial effect was presumed to
be caused  by enhanced biologic activity.
      100
                                           Effluent-GACtuzone & Oxygen
          1      23456      78

                         TIME IN OPERATION, mo

         Figure 91.   Influence of ozonation before adsorption on removal
                     of trihalomethane precursors, THMFP conditions:
                     pH,  not  reported; 25°C (77°F); storage time,  2
                     days.34-104
•Bcc«u« pure onjgcn gas w«s used la generate Iheo/onc, the gas Ted into the gas contactor was an oxygen-o?onff mixture. For
 jtxurai.-}, therefore, the term "o.tvgert plus e»*one" is used for the system with oxidant added.


152  Treatment Techniques (or Controlling Triha/omethanes in Drinking Water

-------
  These findings led to a second experiment in which coagulated and settled Ohio
River water (580 L/day  or 150 gpd) was  fed to two parallel treatment trains
constructed  of stainless steel,  Teflon®,  and  3.7-cm (1,5-in) diameter  glass
columns,104  Each treatment train  consisted of a gas  contactor,  a dual-media
(anthracite coal over sand) filter, and a GAC column with a 10-minute EBCT. The
gas contactor was an unpacked eountercurrent-flow glass column with a stainless
steel diffuser;  the contact  time  was 18 minutes. One treatment  train received
untreated settled water as a control, and the test system received water that had been
treated with oxygen plus ozone (the ozone dose was approximately 5 mg/L).
  Investigations were carried out on the performance of this pilot column system for
the removal of trihalomethane precursors. Data in Figure 92 show that the control
was still removing 50 percent of the THMFP  after 140 days of operation. This effect
was possibly caused by  naturally occurring biologic degradation. Furthermore, the
data show that  when oxygen plus 5 rng/L of ozone was added to the system as an
additional treatment, the net effect was beneficial through the gas contactor, the
dual-media filter, and  the GAC adsorber. The effluent from  that  system had a
consistently lower fraction remaining (Ce/Cs) of THMFP than did the control. This
result confirms  the data from the previous experience (Figure 91).
  To investigate which  unit process was responsible for the improved performance,
the THMFP fraction remaining in the effluent of each of the unit processes, the gas
contactor, the dual-media filter; and the GAC adsorber was compared individually
with its respective control (Figure 92). Oxygen plus 5 mg/L ozone itself had some
influence on the THMFP,  as shown by a lower fraction remaining in the  gas
contactor  effluent as compared  with the control (Figure 92). This result is as
expected (see earlier Subsection Oxidation).
  Data in Figure 92 show that THMFP was  being removed in the dual-media filter
during the latter portion of the test, presumably because of biologic activity. Finally,
little difference  was shown in the  performance of the GAC adsorber, in spite of the
addition of oxygen plus 5 mg/L  of ozone. THMFP removal was the same in the
control GAC adsorber  as in the test system.
  In an effort to determine whether, or not the expected biologic growths could be
contained  in  the filtration/adsorption  system,  standard plate  counts were
determined for the influent settled water and  for samples taken at each intermediate
point in the treatment train. For the summer (from the start of the experiment
through September 21, 1978), these data show that 5 mg/L of ozone reduced the
geometric mean SPC from 2.900/ mL in settled water to 16/ mL in the gas contactor
effluent (Figure 93); essentially no change occurred in the control.
  Following the dual-media filter,  however, the geometric mean standard plat.e
count  had rebounded  to 26,000/mL in the  system receiving oxygenated and
ozonated water, whereas the geometric mean standard plate count actually declined
somewhat through the dual-media  filter of the  control (Figure  93). This high
bacterial population supports the'contention that the organic removal occurring in
the dual-media  filter portion of the system was caused by biodegradation.  Finally,
measurement of the dissolved carbon dioxide content in the dual-media filter usually
showed a higher concentration in'the oxygen-plus-5-mg/ L-ozone system than in the
control—further evidence of biologic activity.

Discussion—
  Evidence in  these two pilot-scale experiments indicates that  biologic activity is
presumed to occur naturally in GAC adsorbers and that this activity can be enhanced
by  the use of ozone as an  additional  treatment. Furthermore, a highly active
adsorbing media does not seem to be required, as shown by the  removal of trihalo-
methane  precursors that occurred in the dual-media  filter  during the second
experiment described above. Biologic degradation of precursor materials seems to
be the  only logical explanation of removal  on  the dual-media filter. Research is
under way with other oxidants and longer  EBCT inert  media  systems"0'1"'"2 to

     Sect/on VII. Treatment Techniques to Remove Trihalomethane Precursors  153

-------
                           40      60       80     100
                             TIME IN OPERATION, day
                                                           120
                                                                   140
                      AUG         SEP         OCT

                               DATE OF SAMPLING
                                                           NOV
         Figure 92.   Removal of trihalomethane precursors by various
                     steps in the treatment train with and without pre-
                     treatment. THMFP  conditions: pH,  not reported;
                     25°C (770FJ; storage time, 8 days,104
                     G = gas contactor
                     F = dual-media filter
                     A = GAC adsorber
define further the potential of this combined treatment technique. Preliminary
results of these field studies are not promising, indicating that the usefulness of this
approach  may be limited. The concept of using inert media to support biologic
degradation of organic materials in drinking water treatment is also supported by
extensive experience with ground treatment, with bank filtration, and slow sand
filters in Europe that have each shown effectiveness for removing organic materials
during drinking water treatment."5 A more detailed discussion of the bacteriologic
populations in  GAC adsorbers  and the influence of this unit process on the
bacteriologic quality of finished water will be presented in Section IX,

T54  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
   E
o
o

§'•
o.
o
DC
O
z
WJ'
 2
O
       10'-
       10*
       10'
       10°
            . ..   C = Control
             (O, = O, + 5 mo/I- O,)
           Settled Water
                                 Gas
                               Contactor
                                Effluent
                                         Dual-Media
                                            Filter
                                           Effluent
 GAC
Effluent
                             STAGES OF TREATMENT
         Figure 93.
                  Standard plate counts after various stages of treat-
                  ment.1*4
Lowering pH

General Considerations—-
  The pH  at which the trihalomethane formation reaction takes place has an
influence on the reaction rate, and possibly the yield (see Section III, Subsection
Effect of pH). This effect implies, therefore, that if the pH at a given water treatment
plant  could  be  lowered  (all  other conditions  being equal),  lower  THM
concentrations would occur at any given time following chlorination. Although this
practice would not remove trihalomethane precursor, it would lower the fraction of
the potential precursors  that  could  participate significantly in the chlorination
reaction, because only those that are reactive at the lower pH would be involved.
Two examples of this approach to trihalomethane control are given here.

Experimental Results—
  The water treatment plant at  Daytona Beach, FL, is a precipitative softening plant
with facilities for recarbonation during its treatment process (Figure 64). Duringthe
USEPA-sponsored project conducted at this location, tests were made with  and
without the recarbonation unit  process in operation.85 These results(Tab.Ie45) show
that during source  water  chlorination, when the  recarbonation  basin  was in
operation and the pH was lowered by 0.9 pH units, the InstCHCl.i concentration in
the finished water was lowered 22 percent compared with the control, and the
InstTHM concentration declined 19 percent on a molar basis.
  A similar result may have been noted at the Thomas L. Amiss Water Treatment
Plant No. 2 inShreveport, LA.1" In this case (Table 46), the normal pH range for the
control week was 8.4 to 9.4, with a median value of 9.1. During the test week, the pH
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  155

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   TABLE 45. TRIHALOMETHANE FORMATION AT DIFFERENT pH
   VALUES DURING SOURCE WATER CHLORINATION WITH AND
      WITHOUT RECARBONATION AT DAYTONA BEACH, FL«
                                Source water*
                                                     Finished water
Process
                    Median  InstCHC!,,  InstTTHM.  InstCHCI,,  InstTTHM,
                      pH	jufl/L	jumol/L	MB/L     nmo\/L
Without recarbonation
(control)
With racarbonation
8.26
7.36
NFf
NF
NF
NF
139
109
1.29
1.06
*THMFP did not ebang* tignlflctntly betwaan thoss two t»sti.
tNont found.

  TABLE 46. COMPARISON OF TRIHALOMETHANE FORMATION AT
 DIFFERENT pH VALUES DURING CHLORINATION BEFORE RAPID MIX
                        AT SHREVEPORT, LA1"


Week
Control week
Test week

Median
PH
9.1
8.6
Rapid mix
InstTTHM,
Mfl/L
62
87

Median
pH
9.1
8.6
Filtered water
InstTTHM,
MJ/L
123
116
 at the beginning of the treat ment was slightly lowered to a range of 8.2 to 8.9 (median
 8.6). The resulting data show a slight decline of about 7 percent in the finished water
 InstTTHM concentrations when the pH was lowered during the test week.

 Discussion—
   The two studies cited above suggest, on a full-plant scale, that the expected result
 %vas obtained from lowering the pH during the reaction between free chlorine and
 precursor materials. Thus if lower pH values can be maintained and other water
 quality parameters can be protected at a given water utility (for example, by using
 some corrosion control technique other than high pH), then a lower fraction of the
 total potential trihalomethane precursors will react with free chlorine. The result will
 be lower InstTHM  concentrations at any point in the distribution system, as well as
 lower TermTHM  concentrations at the extremities of the distribution  system.
 Considerable caution must be exercised, however, when using this approach for
 THM control because of the associated potential corrosion problems.

 Summary of Trihalomethane Precursor Removal as an Approach  to
 Trihalomethane Control

 Advantages of Trihalomethane Precursor Removal—
   The generalized reaction between free chlorine and precursor materials  is:
oHinRtHje-
CHLORINE
                PRECURSORS                                 OTHFR
             HUMIC SUBSTANCES)  - TRIHALOMETHANES + Rv pRrmiirTQ
                AND  BROMIDE                             BYPRODUCTS
 Thus, if the resulting trihalomethane concentrations are controlled by lowering the
 concentration  of precursor materials,  free chlorine can still  be used as the
 disinfectant. Such use is advantageous because free chlorine is used at most water

 156  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
treatment  plants currently,  and  water utility managers and operators have
confidence in its use and its ability to produce a microbiologically safe water.
  Controlling trihalomethane concentrations by treating water to remove precursor
materials  before disinfection  has a second advantage: The general reduction in
disinfectant demand caused by the presence of less material with which the disinfec-
tant can react. The data in Figures 94 and 95 show that the effluent from a G AC
adsorption column that  was removing some trihalomethane precursor material
could be disinfected with a lower dose of disinfectant, as demonstrated by a lower
number of organisms measured by the standard plate count.
        1000
                               riltratron/ Adsorption
                               GAC Effluent; pH, 7.9;
                               GAC Age. 8 Weeks In Operation
                      0.1
                               0.2       0.3       0.4

                                OZONE DOSE, mg/L
                                                          0.5
                                                                   0.6
          Figure 94.
Disinfection with ozone  after GAC adsorption to
remove trihalomethane precursors. Ozone contact
time, 6 min.
  A lower disinfectant demand leads directly to a third advantage of this approach
to trihalomethane control: The formation of fewer disinfection byproducts of all
types. When less disinfectant reacts with less precursor material, not only will the
concentration  of  trihalomethanes decline,  but the  concentrations  of  other
halogenated byproducts and other nonhalogenated oxidation byproducts will also
be lowered. Chlorination of a fresh  GAC effluent did not produce significant
quantities of other halogenated byproducts (Table 47) as measured  by the organic

     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  157

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             10000
              1000
           w
           1C
           o
           o
           I
           00
o
o
uj
            o
            1C
            <
            o

            I
               100
                                    Filtration/Adsorption
                                    GAC Effluents
                                    GAC Age: 24 Weeks In Operation
                            None Detected At
                            0.2 mg/L CIO, Dose
                    0      0.1       0.2      0.3      0.4
                          CHLORINE DIOXIDE DOSE, mg/L

         Figure 95.   Disinfection with chlorine dioxide after GAC adsorp-
                     tion to remove trihalomethane precursors. pH 7.0-
                     8.1; 22-26°C (72-79°F); CIO, contact time, 30 min.

         TABLE 47. ORGANIC HALOGEN PRODUCED UPON
       CHLORINATION OF GAC ADSORBER EFFLUENT AFTER
                        1 DAY OF OPERATION
       Sample
                                        NPOX,
                                      ng/L as Cl'
       Dual-media filter
         effluent + d, (control)
       GAC
         adsorber effluent + CI2
                                         237

                                           18
       'Blank valuo IB about 10 pg/L OX as Cl*.

758  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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halogen (OX) test.70  This test  shows the general advantage  of  reducing the
concentrations  of  trihalomethane  precursor   materials  before  disinfection.
Presumably, the concentrations  of other nonhalogenated oxidation byproducts
from chlorination would also be lowered if the concentrations of precursor materials
were controlled.

Disadvantages of Trihalomethane Precursor Removal—
  If disinfection of the source water is required at a  given  location,  practicing
trihalomethane precursor removal at some point later in  the treatment train will not
influence the reaction of the disinfectant with any precursor materials that may be
present  in the source  water. Thus even if the removal of precursor materials is
complete,  the  formation of trihalomethanes  will  not  be completely  prevented
because of the reaction of chlorine with the trihalomethane precursors in the source
water. Because the trihalomethane formation  reaction is not usually very rapid,
however, the formation of JnstTHM probably would not be complete at the point in
the treatment train where  precursor removal would be practiced; therefore some
unreacted  precursor would  remain and the  treatment process would  still be
somewhat effective. Such a disadvantage in this  approach to  trihalomethane
concentration control is not too serious.
  Another disadvantage to precursor removal has been suggested as a result of work
performed in the Federal Republic of Germany"4 that has indicated the importance
of humic acids in controlling corrosion in water distribution systems. If humic acid is
proven to play such a role, then water treatment to control trihaiomethanes by humic
acid removal might produce a  more corrosive water.
     Section VII. Treatment Techniques to Remove Trihalomethane Precursors  159

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                              SECTION VIII
              USE OF ALTERNATIVE DISINFECTANTS

General Considerations

Formation of Trihalomethanes—
  Trihalomethanes are  formed during drinking water treatment when the free
chlorine used as a disinfectant combines with trihalomethane precursors present in
the water. One approach to controlling trihalomethane concentrations is the use of a
disinfectant other than free chlorine that does not participate in this reaction. Several
disinfectants  are  possible alternatives  to free chlorine: chloramines  (combined
chlorine), chlorine dioxide, ozone, potassium permanganate, hydrogen peroxide,
bromine chloride, bromine, iodine, ferrate ion, high pH, and ultra-violet radiation.
Of these, chloramines, chlorine dioxide, and ozone are the most commonly used in
drinking water treatment practice today and have been studied in detail."5 Because
of the interest in using bromine chloride for the disinfection of wastewater, a brief
USEPA in-house evaluation of that disinfectant was made. One literature reference
to the use of iodine is also included.

Blocidal Activity—
  The primary reason forthe use of disinfectants in the treatment of drinking water
is  to ensure the destruction of pathogenic  microorganisms during the treatment
process, thereby preventing the  transmission  of  disease by drinking water.
Secondarily, the presence of a disinfectant in the water distribution system helps to
maintain the quality of water by preventing the growth of nuisance microorganisms.
An extensive examination of the impact of various treatment modifications on the
bacteriologic quality of finished drinking  water is provided in Section  IX.

   Disinfection Kinetics and Comparative Efficiencies—Biocidal activity by chemi-
cal disinfectants has frequently been considered a kinetic process similar to a chemi-
cal reaction, the microorganism being considered as one of the substances involved
in the reaction. The effectiveness or efficiency of biocidal agents is determined by the
rate at which the reaction or killing of the microorganism population proceeds. The
comparative  biocidal efficiencies of disinfectants are frequently expressed as the
relative concentration (mg/L) of different  disinfectants needed to obtain equivalent
disinfection rates, or as the relative inactivation rates produced by the same concen-
tration of different disinfecting agents. Most of this information has been obtained
by laboratory experimentation under carefully controlled conditions, which include
clean systems, the absence of extraneous  disinfectant-demanding substances, and
the use of pure cultures of the microorganism understudy. The presence (in solution)
of materials exerting disinfectant demand is likely to change disinfection efficiencies
by way of competing reactivation mechanisms. This effect  complicates extra-
polations  from  experiments with clean systems to expected  water utility perform-
ance. Nevertheless, comparisons of disinfectant performance under laboratory con-
ditions are instructive.
   A typical curve from such an experiment is shown in Figure 96. Data from the
results  of a number of such experiments conducted using different disinfectants at
various concentrations can be used to construct plots of the type shown in Figure 97.
As indicated, these results show the exposure times and concentrations of several

160  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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     100
     0.01
                       20
                                    40            60

                              EXPOSURE TIME, sec
          Figure 96.   Destruction of E. coli at pH 7,0, 15°C (59°F), in the
                      presence of 0.16  mg/L chlorine  dioxide. This
                      example shows the  method  used  to determine
                      points plotted in Figures 97 and 98.116
disinfectants needed to produce a given level of inactivation of a given micro-
organism. Figure 97 is a composite of results obtained in one laboratory over a
period of years using consistent experimental methods and microorganisms."6*"7
The results show that chlorine dioxide at pH 7 and HOCl at pH 6 produce similar
rates of inactivation of Escherichia coli.  Hypochlorite ion (OC1~) at pH 10 was less
effective, and monochloramineat pH 9 and dichloramineat pH 4.5 were even less so.
From the data shown in Figure 97, the degree of difference in efficiency between the
disinfectants could be calculated and expressed quantitatively. For example, HOCl
at pH 6 is 35 times as effective as OC1" at pH 10. A similar plot showing virucidal
efficiency of these disinfectants for poliovirus I is shown in Figure 98. Note that
higher disinfectant concentrations and longer contact times in general are needed for
inactivation of poliovirus I than for £. coli. The differences are on the order of less

                               Section VIII. Use of Alternative Disinfectants   161

-------
than I to 2 orders of magnitude, depending on the disinfectant used.  Also, the
difference in efficiency between HOC1 at pH 6 and OC1" at pH 10 is only about
4-fold, and the efficiency order of the two types of combined chlorine is reversed.
  Studies from which similar curves can be prepared have not been done using ozone
as the disinfectant. The main reason is that ozone is such a powerful and unstable
disinfectant  that limitations on sampling times and ozone measurements make
obtaining good experimental results difficult. In spite of this difficulty, ozone does
inactivate microorganisms at a high rate.
  For instance, Walsh et al."8 reported E. coli inactivation rates after 10 seconds'
response to ozone ranging from 99.999% at 0.239 mg/L to 86% at 0.014 mg/L.
Inactivation of poliovirus 1 after 10 seconds'  response to ozone  ranged  from
>99.993% at 0.28 mg/L to >99.4% at 0.012  mg/L.

  Factors  Affecting   Comparative  Disinfection  Efficiencies—Microorganism
Effects—As shown in Figures 97 and 98, neither the order of efficiency nor the degree
of  difference  between  the  disinfectants  is  the  same   for   E.   coli  as
for poliovirus 1. Further evidence of such differences is shown in Table 48. This study
examined tKe inactivation rates of six different enteroviruses by HOC1 at pH 6 and
by OCl'at pH 10."'The results indicate that the degree of difference in disinfection
efficiency of HOC1 at pH 6 and of OCFat pH 10 ranged from 5-fold  forCoxsackie
A9 virus to 192-fold for ECHO I virus. Also note the occurrence of differences of 10-
fold and 53-fold in the rates of inactivation of other viruses by HOC1 at  pH 6 ai\d
OCPat pH  10.
    1000 _cr
     0,01
         0.01         0.1         1.0          10          100
                 TIME REQUIRED FOR 99% INACTIVAT1ON, min
                                                                    1000
         Figure 97.  Inactivation of £ colt" (ATCC11229) by free and com-
                     bined chlorine species and chlorine dioxide.116'117

762  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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    1000 _pr
         E5  Ti I imij   I  I ! I III1|    TTT
     100-= =
   x
    OS
    £
      10
   Z
   w
   Q
      0.1— -
      ,01
         .01
                                                    NHCI2
                                                   . (pH 4.5)
                                   ocr
                                   IpH 10!
                    0.1  •        1.0          10         100
                TIME REQUIRED FOR 99% INACTIVATION, min
                                                                   1000
         Figure 98.  Inactivation of poliovirus 1  (Mahoney) by free and
                     combined chlorine species  and chlorine dioxide at
                     15°C{59°F)."V"
TABLE 48. VIRUS INACTIVATION BY FREE RESIDUAL CHLORINE119


Virus strain
Coxsackie A9 (Griggs)
ECHO 1 (Farouk)
Polio 2 (Lansing)
ECHO 6 (Noyce)
Polio 1 (Mahoney)
Coxsackie B5 (Faulkner)
Min.

pH6.0
0.3
0.5
1.2
1.3
2.1
3.4
required for 99% inactivation at
S.O ± 0.2°C (41 ± 0.4°F)
pH 10.0
1.5
96.0
64.0
27.0
21.0
66.0

Ratio*
6
192
63
21
10
19
•Tim« required «t pH 10.0/tinw requirod »t pH 6.0.

  Disinfectant Chemistry Effects—Assessing the efficiencies of different free and
combined chlorine species also is complicated by the nature of the chemical reactions
that determine  the  -chemical species  present  and  the  chemical equilibriums
established under various pH conditions. For instance, in the reaction
                          HOCl
H* + OCF
[Eq. 10]
a rapidly achieved equilibrium exists that is drastically influenced by pH. At pH 10,
however, approximately 0.5 percent of the free residual chlorine is still present as
                               Section VIII. Use of Alternative Disinfectants   163

-------
HOC1, and because it is a much more powerful biocide than OC1", its presence could
substantially influence the biocidal activity observed.
  Similarly, Equation 11 is reversible,

                      HOC1 H- NH3 s==* NHzCl + HiO              [Eq, 11]

and a solution of 2 mg/L NHiCl is estimated to be 0.58 percent hydrolyzed (0.58
percent HOC1) at pH 7 and 25°C (77°F).1JO Because of the much higher biocidal
efficiency of  HOC1, its influence  on the disinfection rate observed  could be
substantial and  could explain the influence of pH on the biocidal efficiency of
monochloramine.
  Furthermore,  the equation:

                     H* + 2NH2C1 *=s NH4* + NHCh             [Eq. 12]

indicates that although mostly monochloramine is formed when excess ammonia is
present at high pH (>8), addition of hydrogen  ion (lowering  pH) will cause
formation of dichloramine, with the position of this equilibrium being determined by
the pH of the treated water. Thus with chlorine and chloramines, pure species are
never present, and pH determines their identities.  The influence of pH  therefore
cannot be experimentally separated  from species effectiveness for  disinfection.
  Nevertheless, in the case of chlorine, disinfection efficiency declines rapidly as the
pH is  increased from 7 to 9. The efficiency of chlorine dioxide also changes
substantially over this pH range; but in contrast to chlorine, the effectiveness
increases as the pH increases (Figure 99). "6 In this case, the change appears to be in
microorganism sensitivity rather than in disinfectant species present, because unlike
chlorine, chlorine dioxide does not dissociate or disproportionate into different
chemical species within this pH range. In earlier studies, a similar effect was shown
with E. coli (i.e., more rapid inactivation at pH 8.5  than at lower pH by equivalent
concentrations of chlorine dioxide).121
  The pH of the water also affects ozone chemistry.  At highpH values, ozone decay
is accelerated, proceeding through hydroxyl radical intermediates;  thus, the pH of
the water being treated may also  influence ozone effectiveness.

  Dissolved Salt Effects—In 1972, Scarpino et al. reported that OCfwas a more
efficient  virucide than   HOC1 against  poliovirus  1.'"  Results  of subsequent
unpublished studies indicated that 0.05M K.C1, present in the buffer used in the OC1"
experiments, was  responsible  for  the increased  virucidal efficiency  of OC1".
Engelbrecht et al., in  further studies in this area, confirmed and extended the earlier
studies and showed that 0.05M K.C1 enhanced the virucidal efficiency of both OCF
and HOC1."* Sharp and co-workers have also confirmed this effect and  shown that
similar results are produced by the presence of NaCl and CaCl.123'1" This effect was
not seen in £. coll disinfection studies reported by Scarpino et al., although the same
KC1-containing buffer was used in these studies.1"
  From the information  provided above,  ranking these disinfectants precisely and
quantitatively as to their biocidal efficiency is not possible, A major reason for this is
that various microorganisms react differently,  and the same microorganism  may
react differently under various experimental conditions. Note that the effects de-
scribed above influence the rate at which microorganism  inactivation occurs, not
whether or not inactivation occurs at all.

  Adequacy  of Chlorine-Ammonia  Treatment—Despite the  generally weaker
biocidal efficiency of chloramines, the chlorine-ammonia treatment process has been
used successfully for primary disinfection for years by a  number of utilities. The
chloramine  formation,   as  accomplished in  these treatment  plants, differs
significantly from  the procedures used in preparing chloramine for  use  in the

164  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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     0.1
                                      100
                  TIME REQUIRED FOR 99% INACTIVATION, sec

          Figure 99,   Effect of pHoninactivationof poliovirusl (Mahoney)
                      by chlorine dioxide at 21 °C (70°F)."«
1000
laboratory chloramine disinfection studies described above. In the experimental
work, the chloramines were preformed and the microorganisms were added sub-
sequently. In chlorine-ammonia treatment for primary disinfection, as practiced in
the field, ammonia and chlorine are added to the water either simultaneously or in
close succession. The rate of conversion of free chlorine to chloramines depends on
pH, temperature, and the chlorine/ammonia ratio present.
  Although the reaction to form chloramines occurs in hundredths of a second
at high temperatures and optimum pH (8.3), it can occur at much slower rates at
lower temperatures and lower of higher pH values. Thus free chlorine could be
present  for  several minutes and  result in rapid inactivation of microorganisms
(particularly at  lower pH values) because of the presence of free residual chlorine in
the form of HOCI. This possibility was suggested by Heather and Houghton as an
explanation for the much faster bactericidal action observed in ammonia-chlorine
treatment than  could be shown using preformed chloramines.'2*'127 In more recent
pilot-scale chloramination studies involving both clean water and tertiary effluent,
Selleck  et al.  ascribed the  initial  rapid phase  of bactericidal  action during
chloramine  treatment  to oxidation  reduction  reactions occurring  between the
chlorine and substances present in  the water, rather than  to  unreacted  free
chlorine.128 They postulated that highly reactive, short-lived, free radicals produced
during the oxidation of ammonia nitrogen may be responsible for the rapid inactiva-
tion of bacteria.
                              Section VIII, Use of Alternative Disinfectants   165

-------
   From these studies, the much slower experimental inactivation rates shown by
preformed chloramines may not be directly relevant to chloramine treatment in the
field. The enteroviruses are, however, much more resistant than coliforms to both
free residual chlorine and chloramines (see Figures 97 and 98). If, in a particular field
situation, the margin of safety provided by free residual chlorination is minimal,
conversion to chloramine treatment might further reduce the disinfection efficiency.
Therefore, whether or not the initial rapid inactivation phase would be of sufficient
duration to ensure virus destruction  would depend on the source water and other
treatment processes used. Because of this uncertainty, conversion from free chlorine
to chloramine treatment for primary disinfection should be considered with caution.
For this same reason, theTrihalomethane Regulation* placed the use of chloramines
at the discretion of the Primacy Agency, to be considered on a case-by-case basis.

   Application of Laboratory Study Results to Field Situations—Although informa-
tion derived from laboratory studies is useful in assessing the biocidal efficiency of
disinfectants, other factors are important in the application of this information to
actual drinking water treatment in the  field. In water treatment, pure  cultures of
organisms  are  not present as clean suspensions in a medium free of extraneous
materials that might react with the disinfectant used, thereby destroying or altering
its biocidal capability. Rather, in the field, a variety of microorganisms are present in
their  natural state, suspended in a medium containing a variety of other solid and
dissolved materials, some of which can have pronounced effects on disinfectant con-
centration and activity. Because of these effects, disinfection in the field does not
operate as a constant rate process as it does in laboratory studies, changing the shape
of the decay curves and perhaps even the order of disinfectant effectiveness observed.
A particularly good example of changing the order of effectiveness  might  be the
influence of disinfectant demand rapidly depleting a free chlorine residual while
combined chlorine remains at a higher  level for a longer.period of time providing
better overall effectiveness. Nonetheless, some of these conditions can be simulated
in laboratory experiments and can provide information that will be more relevant to
actual practice.
   For example, protection of microorganisms has been considered  because their
association with paniculate matter could result in  their being shielded from* disin-
fectant  action. This possibility has been the major consideration in establishing a
turbidity limit for drinking water. Hoff has recently provided direct evidence of such
protective effects.12* Poliovirus association with washed-cell debris has been  shown
to offer substantial protection against inactivation by HOC1 when compared with
freely suspended  virus (Figure  100). Similarly, the data  in Figure 101 show that
coliforms associated with washed primary effluent solids are inactivated by HOC!
much more slowly than clean suspensions of laboratory-grown E. colt. Hijkal et al.
have also shown that poliovirus associated with fecal material is provided  substantial
protection against inactivation by free chlorine,130
   Furthermore, Foster et al. showed  that cell-debris-associated virus also was
protected from inactivation  by  ozone, the most efficient  biocide under considera-
tion.111  Ozone levels  in excess  of 2 mg/L  failed to completely inactivate viruses
associated with cell debris in 30 seconds. In longer term experiments,  viruses could
be detected even after exposure for 75 minutes to an initial ozone level of 2.5  mg/L.
Comparable information for chlorine dioxide and chloramines is not  yet available,
but in  view  of the ozone results, they will likely  show the same limitations in
efficiency for inactivating microorganisms associated with such solids.

Summary—                                          .   • .            •
   Because of the influence of environmental factors on disinfection, precise rankings
of  the three  alternative  disinfectants—ozone,  chlorine  dioxide,  and
chloramines—cannot  be made. In general, however, ozone and chlorine dioxide are

166   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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                                    HEP-2 Cell-Association Virus
                                            O Virus Only
                                                Turbidily-0.15 mu
                                            • HEP-2 Cell-
                                                Association Virus
                                                Turbidity-1.4 ntu
       -7
                      I
                               20        30        40
                                EXPOSURE TIME, min

          Figure 100.  Free chlorine  inactivation  of  freely suspended
                       poliovirus  and  poliovirus associated with  cell
                       debris. pH 6.0; 5°C (41°F).'*»


ranked as strong disinfectants that are nearly equal to or better than free chlorine,
even at low pH. Furthermore, in contrast to free chlorine, the disinfecting power of
neither is reduced  by increasing pH; in fact, with chlorine dioxide, the opposite is
true. Chloramines are generally ranked as disinfectants that are weaker than free
chlorine  at all pH  values. But they are adequate in  many cases, and some utilities
have been successfully using chloramines for some time. Furthermore, the  equilib-
rium between monochloramine and dichloramine, which have different disinfecting
powers, is influenced by pH.

                               Section VIII, Use of Alternative Disinfectants  167

-------
                                               O Washed £ Colt
                                                 Coliforms associated with
                                                   washed Primary Effluent
                                                   solids (5 nlu)
                                                 Coliforms associated with
                                                   washed Primary Effluent
                                                   solids (1 ntu!
       -6
                                20         30        40
                                 EXPOSURE TIME, min
          Figure 101.   Free chlorine inactivation  of washed, laboratory-
                        grown £. colt and conforms associated with primary
                        effluent solids, pH 6.0;5°C (41 "F).'29
Experimental Results

Formation of Trihatomethanes*—

   Chloramines (Combined Chlorine)—An in-house USEPA study compared the
formation of chloroform in Ohio River water when free chlorine and combined
chlorine were the disinfectants. In this study, ammonia-nitrogen was added to the
Ohio River water before the introduction  of chlorine in an attempt to prevent as
much free chlorine as possible from being present in the sample. The results of this
study were presented in Figure 14 (Section [[[), These data show littie development
of chloroform during the 70 hours of exposure when combined chlorine was the dis-
*ln mtny of these studies, the influence of the disinfectant on both the formation of trihalomethanes and the inactivation of
 rflkfoorgiaisms was studied, As noted previously, the influence of various treatment modifications on bacteriologic quality
 Kilt be presented in Section IX.


168  Treatment Techniques for Controlling Trihatomethanes in Drinking Water

-------
infectant. In contrast, much higher concentrations of chloroform were formed in the
presence of a free chlorine residual. At many water treatment plants where chlora-
mines were used alone or where ammonia was added after a period of free chlorina-
tion to form chloramines, data have also shown lower resulting trihalomethane con-
centrations when compared with situations in which free chlorine  was the disin-
fectant.  Several of these studies are summarized in this subsection.
  Figure 102 shows a block diagram of one of the water treatment plants of the St.
Louis County Water Department.132 In this case, 8 hours of free chlorine residual
existed  before  the addition of ammonia and more chlorine to carry a combined
residual throughout the distribution system. Little if any increase in chloroform
concentration occurred during the 12-hour transit time from the treatment plant to a
storage  tank (Table 49).
                  Lime
          Hexa-
          meta-
Fej(SO4)j   phosphate
                                                                 Pump
                Fe,(S04!3
         Figure 102.  Block diagram of a St. Louis County water treat-
                      ment plant.m (Adapted from AWWA Water Quality
                      Technology  conference—IV PROCEEDINGS JDe-
                      cember 5-6  1976J by permission. Copyright 1976,
                      the American Water Works Association.)
         TABLE 49. INFLUENCE OF AMMONIA ADDITION ON
                    TRIHALOMETHANE FORMATION
           AT THE  ST. LOUIS COUNTY WATER COMPANY132
Finished
plant water
Date
9/20/76
9/22/76
9/23/76
9/27/76
CHCI3
MI/L
38
36
34
38
CHBrCI,
/•9/L
12
11
12
12
Combined
CI2 res,
mg/L
1.8
1.6
2.2
2.3
Storage tank
1 2 hours away
NHj-N
mg/L
0.55
0.50
0.35
0.40
CHCI,
^g/L
34
35
36
35
CHBrCU
Mg/L
8
12
13
12
   One of the water utilities included in a project managed by the Ohio River Valley
Water Sanitation Commission (ORSANCO) was Beaver Falls, PA." At this water
utility, breakpoint chlorination was temporarily halted sometime between February
15 and 22, 1978. As a result of this alteration in treatment practice, a considerable
decline in the InstTTHM concentration occurred (Table 50), even though a rise in
                              Section VIII. Use of Alternative Disinfectants  169

-------
water temperature in the spring months would usually cause a rise in trihalomethane
concentrations.  When  breakpoint chlorination  was  reinstated in  June,  the
InstTTHM concentration rose significantly.

 TABLE 50, INFLUENCE OF ENDING BREAKPOINT CHLORINATION
                TEMPORARILY AT BEAVER FALLS,  PA18


Data,
1978
1/3
1/13
1/18
1/25
2/8
2/15
2/22
3/1
3/15
3/29
4/12
4/26
6/27

Measured free CI2
residual.
mg/L
0.8
0.9
1.0
0.8
O.8
0.5
0.4*
O.5*
<0.1*
NRt
0.1 •
NR
1.6
Clearwell
Total CI2
residual.
mg/L
0.3
1.0
1.2
0.9
0.9
0.5
1.2
1.2
1.2
0.9
1.1
1.2
NR


InstTTHM,
M9/L
52
48
61 '
45
62
41
7f
7
11
12
12
10
126§
•Som« porm«ngin«to pniont. mooturad at Iron Cl,
tBroikpoInt chlorfnatlon stoppad.
$Not run.
SBraikpoInt chlorinitlon resumad.


   During the ORSANCO project, InstTTHM  concentrations were determined
 monthly at several participating water utilities treating various qualities of river
 water.   Of these, five maintained a  relatively high free chlorine residual in the
 finished water, and two practiced marginal chlorination. Although the source waters
 were different, the InstTTHM concentration was significantly lower for any given
 month in the two water utilities that maintained relatively highchloramine residuals
 (Wilkinsburg-Penn Joint Water Authority and Fox Chapel Authority) than in the
 five utilities that  maintained relatively high free chlorine residuals (Figure  103).
   During this same project, investigations were carried out at the Hays Mine Plant
 of the Western Pennsylvania Water Company.18 At this plant, routine  treatment
 included chlorination of both source water and filtered water. Because of the varying
 concentration of ammonia in the source water, a free chlorine residual was present
 sometimes, and a combined chlorine residual occurred at other times. Although no
 true control existed in this study, an average of only 22 jug/ L InstTTHM was present
 in the finished water when the ammonia was present in the source water, contrasted
 to 42 /^g/L InstTTHM when a free chlorine  residual existed (Figure  104). This
 difference was probably caused by the presence of the combined chlorine residual.
  The Louisville Water Company has tried several alternative treatment techniques
 involving various disinfectants and combinations of disinfectants in an attempt td
 control the trihalomethane concentrations in their distributed water,'""135 Their
 treatment scheme consists of plain sedimentation with no coagulant, followed by
 coagulation and  sedimentation,  softening, and dual-media filtration.  The  first
 modification,  in August  1977, involved chlorination of the coagulation basin in-
 fluent and the addition of chlorine and ammonia in the clearwell following filtra-
 tion. Under these conditions,  the InstTTHM  concentration in the clearwell was

 170  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
about  150  itg/L,  but  no  further  increase  in  trihalomethane concentrations
occurred in the distribution system because  of  the absence  of a  free chlorine
residual.
      180
                                                      Wheeling. WV
                                                    O Louisville, KY
                                                    • Huntington, WV
                                                    D Cincinnati, OH
                                                    * Evansville, IN
'   ,        ,    ,                 DATE OF SAMPLING
         Figure 103.   Seasonal variation in finished water TTHM concen-
                      trations for treated surface waters.18

  The second test, conducted in October 1977, involved the movement of the point
of ammonia addition from the clearwell to thesoftening basin. Thisstep reduced the
InstTTHM concentration in the clearwell  to about 95 MS/L, with only about an 8
percent increase in trihalomethane concentrations from the effluent of thesoftening
basin through the distribution system."1 .
  Currently,  the  following treatment is practiced: Potassium permanganate and
copper sulfate are added to the plain settling basin, as needed, to control taste, odors,
and algae; chlorine is added to the effluent of the coagulation-sedimentation basin,
and ammonia is added  10 minutes later. This practice has reduced the InstTTHM
concentration in the distribution system to approximately 15 ^g/L.1J4'l'!S Although
no  controls  were available  during these  tests, the  changes in trihalomethane

                               Section VIII, Use of Alternative Disinfectants  171

-------
concentrations were most probably caused by the treatment changes, A possible
future summertime operation involves combining chlorine dioxide with ammonia.
This procedure is discussed  later in this section under Chlorine Dioxide.
    CJ
    a.
    o
    o
    o
I
    o>
    a.
    O
    o
    u
    ui
50



40-


30—



20-




10-


July, 1978 §
No Background s 5 s •£
Ammonia jE x f •<

= 88

— 5 «
x ®
f- IE
w "•
f- *- s
~~ rr W QC ui U)
S ~ ® «
j^i° J^ a: cc
o ~i
33
— uT
a
. U • ™ n
W —  I p» aiTT « o*t~
i|| i|| i|[

—

ui
0>
M<£"
gj
a: _T
0 O
O li
»,§•
ai r-
u.
«-

_
Z
I
Z
f Influent 4 Coagulated Settled GAC - 4 Finished
Water I & Clarified Water Treated 1 Water
z.emg/uCf, I Water Water 1
1.3 mg/L KMnO4 1.1mfl/LCIj
50


40-




30-



20-



10-
0
October, 1978 g
Background * S
Ammonia u 8 °1
— — EC — ^
(0 (J
z S z *• —
. H- - J3 »
p» n
I







VI
_ OC
S "
p c
1 I
"T -r-
" _, O
3; (5 H"
f ^ T s I-
- • x
w O
c __
z z
1
x ^ S x ^
• ™ m X -^ t« n
°= i | ^ || S^
S " T-S S |1 « s
ce 13™ 1 - S °
T "• J z T 1 * "-i-
8>2-
OCT
z ~
"O
Z OJ ~
li
                                                                    2.0
                                                                    1.0
                                                                        O)

                                                                        _r
                                                                        <

                                                                        9
                                                                        tn
                                                                        LU
                                                                        OC
                                                                        Ui
                                                                       "Z.
                                                                        cc-
                                                                        3
                                                                        o
                                                                    2,0
                                                                    1.0
                                                                    01
                                                                    UJ
                                                                    OC
                                                                    u_

                                                                    O

                                                                    O
                                                                    O
                                                                    Z
                                                                     w
                                                                    I
                      {Influent 4 Coagulated  Settled     GAC - f Finished
                      Water  I & Clarified  Water     Treated I Water  '
           2,2m8/LCIj       | Water                Water |
                        0,4 mg/L KMnO,                1.2 mg/L CI,
          Figure 104.  Influence of ammonia nitrogen in the source water
                      on trihalomethane concentrations at the Western
                      Pennsylvania Water Company, Pittsburgh, PA.1"
  The Jefferson Parish  Water Department has  used combined  chlorine as the
primary disinfectant for some time. Brodtmann et al. reported on the InstTTHM
concentrations in the Jefferson Parish distribution system as compared with the
THMFP concentration measured with free chlorine in the samples in the sand filter
/ 72  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
effluent.1"  During an  18-month period (January 1978 to June 1979), some 19
samples per month were analyzed and averaged. The data in Table 51 show how
much lower the monthly mean InstTTHM concentrations were in the distribution
system with combined chlorine present than they would have been with the tempera-
ture, pH, and storage time shown for the free-chlorine-treated sample, as indicated
by the THMFP concentration.

       TABLE 51. COMPARISON OF TTHM's IN AMMONIATED
   DISTRIBUTION WATER WITH THMFP OF CHLORINATED SAND
           FILTER EFFLUENT AT JEFFERSON PARISH,
Month
1978:
January
February
March
April
May
June
July
August
September
October
November
December
1979:
January
February
March
April
May
Juno
Number of
distribution
samples
analyzed

15
20
20
15
20
25
15
25
20
20
10
20

25
10
20
20
25
20
Mean
distribution water
InstTTHM,
MB/L

3,2
3.1
5.0
2.8
5.2
4.2
23.9$
7.3
8.8
7.3
7.2
6.1

4.2
3.0
1.9
3.4
6.2
7.9
Sand filter
effluent
THMFP,»
PB/L

241
271
269
302
t
t
319
232
191
250
211
173

171
t
t
203
365
272
•Five days, 30°C (86°F), pH 10; initial trm Cl,, 10 mg/L.
tNo data collected during this period.
$Ammoniator out of service; free chlorine residual present In pert of distribution system.

   Water treatment at  Huron, South Dakota, consisted of adding to James River
Water alum and polyeleetrolytes for coagulation and lime for softening, followed by
settling, recarbonation, filtration and disinfection with chloramines.   Before 1979,
when breakpoint chlorination was  practiced, the TTHM  concentrations  in the
distribution system sometimes exceeded 300 ftglL. Following a USEPA sponsored
project, ammonium sulfate is  now  being added to produce combined chlorine.
Trihalomethane reductions ranging from 72 to 79 percent occurred at two places in
the distribution system immediately following institution  of the new treatment.
   At the University of Texas at San Antonio, research is under way to investigate
methods of reducing  the trihalomethane formation while maintaining effective
disinfection by achieving instantaneous and  total  mixing of the  disinfectant
following dosing, preventing trihalomethane formation by reducing reaction time, "*
Disinfectant is introduced by means of a high-energy (G = about 40,000 sec""'), in-line
mixer to a 4lO-m}/day (75-gpm) flow stream. After 16 seconds of contact time, the
water passes through a second high-energy, in-line mixer.  Flow continues in a pipe
loop system for 55 seconds to provide  short, but precisely known contact times.

                              Section VIII, Use of Alternative Disinfectants 173

-------
Longer contact times for disinfection or trihalomethane formation are obtained by
collecting samples of water discharged from the pipe loop and holding them for the
desired time period.
  This project studied the formation of trihalomethanes in disinfection systems
involving chlorine only, chlorine followed by addition of ammonia 16seconds later,
ammonia followed by addition of chlorine 16 seconds later, or chlorine dioxide.
Addition of ammonia after 16 seconds eliminated the free chlorine residual, thereby
reducing the trihalomethane formation (Table 52). These data show that reducing
trihalomethane formation by limiting the free chlorine contact time in this type of
mixing system is feasible.
    TABLE 52. TRIHALOMETHANE FORMATION IN LAKE WATER
     PASSED THROUGH A HIGH-INTENSITY MIXING SYSTEM"8
Disinfectant
dose.
mg/L
0

0.5
0.5
0.5
O.5
1.5
1.5
1.5
5.O
5.0
5.0
TermTTHM,"
System
No disinfection
(control)
Chlorine
Chlorine + ammoniaf
Ammonia + chlorinof
Chlorine dioxide
Chlorine
Chlorine + ammoniaf
Ammonia + ohlorinef
Chlorine
Chlorine + ammoniaf
Ammonia + chlorinef
pH


—
7.65
—
—
7.7
7.6
_
7,5
7.85
—
M9/t
<0.1

6.3
2.5
0.13
2.7
119
7.4
0.43
179
10.2
4.3
Fre«
chlorine
residual
at 48 hr,
mg/L
0

0.1
O
o
—
0.3
0
0
2.5
0
0
 •48 houn, 14»C (67°F) lo 17"C (63°R,
 tAmmonii dote *qual to ehlorlno dot* in mg/l.
   The North  Jersey  District  Water Supply Commission compared free  and
 combined chlorine for trihalomethane formation control during 1979 (unpublished
 data). Flow from the  Wanaque Reservoir was divided between two 1.9-m (74-in)
 diameter, cement-lined steel mains, one of which was treated with free chlorine, and
 the other with chlorine plus ammonia. The flows were divided for 6 hours and then
 combined downstream. With ammonia following free chlorine injection, the total
 trihalomethane concentration at the juncture reached 6 jug/ L; without ammonja, the
 total  trihalomethane concentration was 38 Mg/L at this same point.
    Lange and Kawczynski, in their efforts  to control TTH VI concentrations at the
 Contra Costa  County Water District, experimented with the use of chloramines.20
 They conducted jar tests arranged to resemble treatment at the  water plant with
 source water chlorination, ammonia being added to the chlorinated water at a weight
 ratio  of 3/1 (NHj/Ch). The data (Table 53) show that the addition of ammonia did
 arrest the formation of trihalomethanes.  But because the  high bromide concen-
 tration caused a  rapid formation of bromine-containing  trihalomethanes, very
 little time could be allowed to elapse between the addition of chlorine and ammonia
 if significant reductions  in InstTTHM concentrations were to be achieved. The
 174  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
California State Department of Health required that under these circumstances, a
free chlorine residual be maintained for a minimum of 10 minutes before the addition
of ammonia. Other Primacy States may have similar requirements.

           TABLE  53. RESULTS OF CHLORAMINE STUDIES
            AT CONTRA COSTA, CA, SEPTEMBER 1977»
. Clj contact time
before adding NH3,
hr
0
0.5
1.0
1.5
4.0
Control treatment
sample (excess CI2)
Trihalomethanes, fifl/L
pH
7.0
7.0
7.0
7.0
7.0

8.2
CHCI,
3
15
7
8
9

5
CHBrCI,
2
16
18
20
26

18
CHBr,CI
1
39
45
51
58

84
CHBr, (.
<1
50
55
60
50

189
TTHM,
Jfl/L
6
120
125
139
143

296
  Siemak et al. reported on the efforts  of several California utilities to control
trihalomethane concentrations.13' They briefly mentioned a study by the Casitas
Municipal Water District on use of the addition of ammonia. In a summary of this
work, they reported that the InstTTHM concentration was reduced from about 150
jig/L when chlorination only was used, to  approximately 75 ftg/L when post-
ammoniation was practiced to produce a chloramine residual.
  Sontheimer, reporting on the work of Sander and Oehler at the Stuttgart Water
Works,  Federal  Republic  of Germany, presented  data showing that  when
breakpoint chlorination was  no  longer practiced  at this utility, the  resulting
trihalomethane concentrations were significantly lowered (Table  54),H0 When
breakpoint chlorination was not used, chlorine was added in small amounts in a
stepwise  fashion throughout the treatment  train without  ever producing a free
chlorine residual.

   TABLE 54. EFFECT OF HALTING BREAKPOINT CHLORINATION
       AT STUTTGART, FEDERAL REPUBLIC OF GERMANY140
                 Breakpoint ehlorination
                             Sedimentation
                  River           basin
                  water          effluent
Nonbreakpoint chlorination
             Sedimentation
  River          basin
  water         effluent
NHt mg/L
TTHM, fig/L
1.2
0.2
0.03
53
0.9
0.1
0.4
5
These  12  studies all confirm that  trihalomethane formation will be reduced if
chloramines rather than free chlorine are used for disinfection.

  ' Chlorine Dioxide—To investigate the reaction of chlorine dioxide with typical
trihalomethane precursors, an in-house USEPA study was conducted using humic
acid* treated with chlorine dioxide  that was prepared as described in Section VI,
Subsection Oxidation.39 Generated in this manner, the chlorine dioxide solution was
nearly  devoid of free chlorine.
  In these experiments, humic acid solution (5 mg/L)  was dosed with  8 mg/L
chlorine dioxide. After 48 hours of contact time, 1.7 jig/ L of chloroform was formed
*See Section VI], Subsection Oxidation (Chlorine Dioxide) for a description of humic acid preparation.

                              Section VIII. Use of Alternative Disinfectants  175

-------
(Figure 105), but no  other trihalomethane species occurred. For comparison, a
similar humicacid solution was dosed with 8 mg/L of free chlorine. In the same time
period, 108 /zg/L of  chloroform (Figure 105) and  1.5 fig/L of bromodichloro-
methane were formed—about 110 ng/L TTHM. This study indicates conclusively
that chlorine dioxide  does not produce trihalomethanes from precursor materials
that will react with  free chlorine to produce trihalomethanes.
       120
           0     5     10    15    20    25    30   35    40    45     50
                                REACTION TIME, hr

          Figure 105.  Chloroform formation in water containing 5 mg/L
                      humic acid dosed with chlorine-free chlorine diox-
                      ide or free chlorine.39

   In another experiment (Table 55) chlorine-free chlorine dioxide was added  to
Ohio River water.16 Again, low concentrations of trihalomethanes were formed.  In
this experiment, the companion control dosed with free chlorine was not run, but
many  previous  experiences  have shown that  Ohio River water  will produce
significant concentrations of trihalomethanes upon chlorination. These results again
indicate that in a natural medium, chlorine-free chlorine dioxide does not produce
significant concentrations  of trihalomethanes.
   During normal continuous flow operation, chlorine dioxide is usually generated
by adding chlorine to sodium chlorite in a concentrated stream. Because this reaction
proceeds best at a low pH, hydrochloric acid or excess chlorine is added to reduce the
solution pH. In either case, the chlorine dioxide produced contains some chlorine
(more if excess chlorine is used).
   At the USEPA  Evansville,  IN,  project,  stoichiometric quantities of NaOCl,
NaClOj, and HC1 were mixed together in a chlorine dioxide generator in an attempt
to produce chlorine dioxide with little chlorine in it.63 On the average, the generator
effluent produced chlorine dioxide containing 9.5 percent chlorine and 56 percent
chlorite (of the total oxidants)  by weight.
   Although the presence of chlorine in this mixture suggests that trihalomethanes
would be formed under these circumstances, as previously discussed in Section VII,
Subsection Oxidation (Experimental  Results), chlorine  dioxide  alters  certain
trihalomethane precursors so that the yield of trihalomethanes is reduced when free
chlorine reacts with them. Thirteen tests were performed with various doses  of
chlorine dioxide and free chlorine to determine how these mixtures would behave
when treating Ohio River water that had been coagulated,  settled, and  passed
through a dual-media filter in the USEPA pilot  plant. Although more research is

176  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
 needed to  elucidate the reason, the resulting trihalomethane concentrations are
 generally inversely  related to the chlorine dioxide/free chlorine ratio (Table 56).
 Significant concentrations of trihalomethanes would not be expected under these
 circumstances, because a well operated chlorine dioxide generator using acid forpH
 control can produce chlorine dioxide containing relatively small quantities of free
 chlorine.
TABLE 55. TRIHALOMETHANE PRODUCTION WITH CHLORINE-FREE
        CHLORINE DIOXIDE ADDED TO OHIO RIVER WATER*"

CIO2
dose.
mg/L
0
1.4
2.7
2.7
2.7
2.7
ClOa
residual.
mg/L
0
0.7
1.5
1.3
0.8
0.3

Contact
time, hr
—
0.5
0.5
6
18
42

Chloroform,
M9/L
<0.2
0.2
0.2
0.1
0.1
<0.2

   As part of the Evansville, IN, project, the performance of a545-m"'/day (100-gpm)
 pilot plant using source water chlorination followed by chlorine dioxide disinfection
 was compared with that of the  full-scale  plant  using chlorination only.** This
 comparison using the full-scale plant as a control was performed after a 2-week study
 showed that equivalent amounts of trihalomethanes were produced in both plants
 when a sufficient free chlorine residual was maintained through filtration, thus indi-
 cating that the control was valid. As shown in Table 57, little InstTTH M was formed
 with chlorine dioxide addition in the pilot plant (note that the chlorine dioxide con-
 tained an average of 9.5 percent free chlorine). But when chlorine was applied to the
 full-scale plant, the TTHM concentration increased from an average of 1.7 ng/ L in
 the source water to 64 /*g/L.
   During the ORSANCO project, the use of chlorine dioxide was investigated at the
 Hays Mine Plant of the Western Pennsylvania Water Company.18 At this location,
 the chlorine dioxide was generated by adding hydrochloric acid to sodium chlorite
 (Figure 106). Because chlorine is not involved in the reaction, a nearly chlorine-free
 chlorine dioxide solution was  produced. The chlorine dioxide dose to the source
 water was 1.5 mg/L, which did not exceed the disinfectant demand, as chlorine
 dioxide was not found in the coagulation-clarification basin effluent. The significant
 decrease in  InstTTH M  concentration  that  occurred when the source  water
 disinfectant  was switched from chlorine to chlorine dioxide is shown in Figure 107
 (page 180);
   Chlorine dioxide has been widely used in Europe as an alternative to chlorine
 for drinking water disinfection for some time,141 Although these operations are con-
 sidered successful with regard to disinfection, control of trihalomethanes through
 the use of chlorine dioxide disinfection has not been well documented in most places.
 Several examples are given here, however, to demonstrate that the USEPA findings
 reported above are borne out by others.
   For example, Hamilton, OH, has been  using chlorine dioxide for disinfection for
at least the last 6 years.142 Here, the finished water contained less than  I ng/L of
 InstTTHM,  and the 2-day TermTTHM, measured with 5 mg/L of chlorine added,
 was  16 jig/L. Although the trihalomethane  precursor concentration in this water
was  low, the use  of chlorine dioxide  has avoided the production of significant
quantities of trihalomethanes.

                              Section  VIII. Use of Alternative Disinfectants  177

-------
g
I                   TABLE 56. INFLUENCE OF A MIXTURE OF CHLORINE DIOXIDE AND CHLORINE ON

~                              TRIHALOMETHANE PRODUCTION IN OHIO RIVER WATER39


 -
B>
3

8
Test
reaction
time.
hr
23
48
25
42
22
24
38.5
27
27
24
50
21
24
CIO.

Dose,
mg/L
0.5
0.7
0.5
1.9
1.3
2.0
2.2
4.2
4.2
1.8
4.7
3.5
2.8
— . _^
Residual,
mg/L
Tt
0.3
0.2
0.5
0.6
0.4
0.3
3.2
2.3
1.3
2.7
3.1
1.8

Dose,
mg/L
2.0
2.3
1.4
4.1
1.5
2.0
2.0
2.5
2.5
0.9
2.0
0.8
0.5
Cl,

Residual,
mg/L
0.3
1.2
0.4
2.4
0.2
0.7
0.6
1.6
1.5
0.4
0.5
0.4
NR*
Control
(Cl, only)
residual.
mg/L
0.8
0.6
0.3
1.9
0.05
0.8
0.4
1.0
1.0
0.1
0.4
T
T


CICVCI,
ratio
0.25
0.31
0.33
0.46
0.87
1.0
1.1
1.7
1.7
1.9
2.4
4.3
5.6


TTHM,
M9/L
54
30
26
41
25
28
29
6
8
6
5.3
1.6
<0.1

%
TTHM
reduction*
20
23
48
40
60
59
49
84
80
84
93
96
100
                *Compired with a chlorine-only control when the chlorine due is equal to the chlorino due in the tait cyttern.

                tTr.ce.

                f Not run.


-------
  TABLE 57. USE OF CHLORINE DIOXIDE FOR TRIHALOMETHANE
       CONTROL IN  OHIO RIVER WATER  AT EVANSVILLE, IN"
Date,
1979
9/18
9/25
10/2
10/9
10/16
10/23
10/30
11/14
11/20
11/27
12/4
12/11
Avg.-

Raw water
influent
0.9
6.1*
0.3
0.5
0.3
0.1
0.4
0.6
0.5
0.4
9.9$
0.2
1.7
InstTTHM, ^fl/L
Full-scale plant effluent,
CI2 treatment only*
109
84
'. . 95
82
84
36
53
51
40
46
42
41
64

Pilot plant effluent,
Clj and CIO; treatment!
1.2
3.0
2.9
0.7
1.2
0.8
0.9
1.2
1.3
1.2
5.9
0.8
1.8
"Average applied Clx dote to raw water ~ 6.3 mg/L.
 Average residual Cl» in full-seala plant affluent =1.7 mg/L.
tAverage applied ClOi doaa to raw water = 1.6 mg/L.
 Average recidusl CIO, in pilot plant effluent K O.3 mg/L.
(Reason thece value* were higher than normally found is not known.
    Make-Up Water
    (From Finished
       Water At
        Elevated
        Storage)
Metering Valve
   {Typical)
                                                             Delivery
                                                             (To Mix Tanks)
        Valve
       {Typical)
                 Flow
                 Meter
                                                      Sample
                                                       Port
          Figure 106.  ORENCO (Rio Linda Chemical Co., Rio Linda, CA)
                       chlorine dioxide generator  used at  the Western
                       Pennsylvania Water Company, Pittsburgh, PA.1*
                                 Section VIII, Use of Alternative Disinfectants  179

-------
 s
 I
•5*
 c
 8
 §
 3=
 a*
     U
     o
     o
                         50
                         4°'
                     I  20-
                     us  10-
                     1
                                         Routine Treatment, (pro- and post-treatment chlorination, July 1978)
                                         Modified Treatment, (pre-treatment ClOj and post-treatment chtorination, September 1978)
                                        Source
                                        Water
                Routine Treatment
                                4       Influent  f
                                 I       Water   I
Coagulated and
Clarified Water
Settled
Water
                                             2.6 mg/L Cl,      1.3 mg/L KMn04
6AC-
Filtered
Water
Finished
Water
                                                                                                 1.1 mg/LCI2
I
3'
*-

I"

I
Modified Treatment
                                             1.5 mg/L CIO, < 0.1 mg/L Clj
                                             0.8 mg/L KMnO«
                            Figure 107.  Mean TTHM concentration in water given routine
                                         (Clj only) and modified {CIO, and Cl,} treatment at
                                         the Pennsylvania water company, Pittsburgh, PA.
                                         (45,000-mVday [12-mgd capacity].)18
                                           1,4mg/LCI2

-------
  The Louisville  Water Company has also  performed some experiments with
chlorine dioxide as an alternative disinfectant (a companion to the studies with com-
bined chlorine reported earlier in this section under Chloramines).135 In this case, the
addition of ammonia was included in the treatment process to combine with any free
chlorine that might remain in the water as a result of the generation of the chlorine
dioxide. Note that chlorine dioxide does not react with ammonia. Specifically, 0.6 to
0.8 mg/L of chlorine dioxide was added to the coagulation basin effluent, and 0.5
mg/ L of ammonia was added to the softening basin influent. At this utility, softening
follows coagulation-sedimentation.  Under this treatment scheme, the InstTTHM
concentration in the distribution system was less than 5 pg/L. If needed, this
treatment may be used in the  summer months.
  Several reports have appeared recently in which various utilities have investigated
the use of chlorine dioxide in  place of chlorine as the primary disinfectant. These
data (Table  58) show the same pattern as reported in the in-house USEPA studies
and the four case histories presented above. Both in the laboratory and in the field,
the use of chlorine dioxide clearly can  reduce  the resulting TTHM formation
when compared with equivalent free chlorination.

           TABLE §8. TTHM's PRODUCED IN TREATMENT,
          WATER DISINFECTED WITH CHLORINE DIOXIDE



Location
Shreveport, LA
Davenport, IA
Peoria, IL
Bethesda, OH
Contra Costa, CA
InstTTHM
with
free chlorine.
Mg/L
68
152
60
284
>100
InstTTHM
with
CIO;.
*»B/L
1,2
62
6
16
None



Reference
111
66
66
Peraonai communication*
20
•J. Luca«, USEPA, 1980.

  Ozone—In a previously unpublished in-house USEPA study on the possibility of
trihalomethane  formation  during ozonation,  a 3.7-em (l.5-in) diameter  glass
counter-flow contact chamber with a fritted glass sparger was used. Ohio River
water was ozonated at 2 different doses, and the trihalomethanes produced were
compared with those of a control in which chlorine was used as the disinfectant. The
data in Table 59 show that virtually no trihalomethanes were formed during the
ozonation experiments.  Consideration was given to the possibility that the ozone
might oxidize either  chloride or  bromide  or both to active chlorine or bromine
species and thereby produce trihalomethanes during ozonation. But the data in
Table 59 indicate no such occurrence.

     TAiLE 59.  EFFECT OF OZONATION ON TRIHALOMETHANE
PRODUCTION IN OHIO  RIVER WATER, CONTINUOUS-FLOW STUDIES
Applied
ozone
dose,
mg/L*
0.7
0
18.6
0
Chlorine
dose,
mg/L
0
8
0
8
Trihalomethanes, /jg/L
CHCI,
0.2
6
0.2
12
CHBrCI,
NFf
14
NF
9
CHBr2CI
NF
4
NF
2
TTHM,
MB/L
0.2
24
0.2
23
  j contact limn ™ B to 6 mimita*.
  one found.
                              Section VIM. Use of Alternative Disinfectants  181

-------
  The data collected during the study cited in Reference 141 show that more than
1000 water utilities in Europe use ozone as the primary disinfectant. Although
bromoform may be formed under unusual conditions of high bromide content,143 the
USEPA in-house studies show clearly that ozonation does not cause formation of
trihalomethanes under normal drinking water treatment conditions. Therefore, even
though the trihalomethane content is not known for most of these European utilities,
trihalomethanes should not be formed at these plants as a result of ozonation. The
Strasburg, PA, water utility used ozone as the only disinfectant and was the only
utility  in  the National  Organics Reconnaissance  Survey that did not  have
measurable quantities of trihalomethanes  in the finished water.' In this  ease,
however, comparisons are difficult, because  the TermTHM concentration was not
determined on this water,

  Bromine Chloride—When free chlorine was used as a disinfectant in an in-house
USEPA study (Table 60), the primary trihalomethane was chloroform; but when
bromine chloride was used as a disinfectant, almost all of the trihalomethane content
appeared as  bromoform, with hypobromous acid probably being the  primary
reactive hydrolysis product of bromine chloride.36 Furthermore, more TTHM's were
formed when bromine chloride rather than free chlorine was used as the disinfectant
(Figure  108). Thus these data indicate that the use of bromine chloride is not
necessarily desirable because of the formation of large quantities of bromine-con-
taining trihalomethanes, mostly bromoform.

TABLE 60. TRIHALOMETHANE FORMATION IN TREATMENT, WATER
    DISINFECTED WITH CHLORINE AND BROMINE CHLORIDE3'

                  Trihalomethanes                 Trihalomethanes
                                              formed with
Rsaction
timo, hr
6
24
48
72
96

CHCIj
44
85
106
116
118

CHBrCI,
16
23
28
30
41

CHBr,Cl
3.4
4.5
5.2
5.8
5.9

CHBr3
0.2
1.3
0.3
0.2
0.3

CHCI,
0.3
0.4
0.5
0.6
0.5

CHBrCI,
<0.1
<0.1
0.1
0.2
0.1
orvsi], PH
CHBr,CI
1.7
2.0
2.7
3.2
3.4

CHBr,
149
177
194
209
209
  Iodine—The formation of trihalomethanes during iodination was studied by
Rickabaugh and Kinman.H
-------
  For  purposes  of comparison, the  subject of other disinfectant byproducts is
introduced with  a summary of the available information regarding chlorination
byproducts other than trihalomethanes, followed by a corresponding discussion for
each alternate disinfectant (chlorine dioxide, chloramines, and ozone).
       200
       175
20        30       40
  REACTIONTIME.hr
                                                           50
                                                                    60
         Figure 108.  Formation.of trihalomethanes during water treat-
                     ment using free chlorine and bromine chloride as
                     disinfectants,3*

   Chlorine—Nonpolar compounds other than trihalomethanes that were either not
 detectable in the source water or were present in lower concentrations have been
 detected in finished water at ng/L to Mg/L concentrations. Most of the sources of
 these are poorly understood. At ieast 19 nontrihalomethane, halogenated, volatile
 compounds were found by Rook2' in the Rotterdam Storage Reservoir. Stieglitz et
 al. found additional compounds formed at low concentrations in a Rhine River bank
 filtrate  sample upon chlorination.14' Rook speculated  on a possible pathway to
 explain the formation of some of the observed byproducts as related to his proposed
 mechanism for trihalomethane formation  from  m-dihydroxyphenyl  moieties.
                               Section VIII. Use of Alternative Disinfectants  183

-------
X1
01
a



t

-------
Stieglitz suggested  no mechanism.  Coleman et  al. reported the  co-presence of
chloropicrin, chlorobenzene, a chlorotoluene isomer, and a chloroxylene isomer as
well as their respective logical precursors (nitromethane, benzene, toluene, and
m-xylene) in finished chlorinated tap water.14* With the exception of benzene, all of
the above precursors were shown  to react with free chlorine to form the expected
products.
  In later studies at the USEPA  laboratory (unpublished data, 1978) chloroace-
tonitrile derivatives  were  observed  in a finished tap water. Concentrations of
acetonitrile in the mg/L range could not be made to react with free chlorine under
realistic reaction conditions to form detectable chlorinated derivatives. But Trehy
showed that dichloro-, bromochloro- and dibroraoacetonitrile were formed upon
low pH chlorination of a south Florida drinking water source.'49 At high pH, such
as in lime softening systems these byproducts are not formed or are later destroyed.
In addition, in-house work by USEPA in cooperation with Manchester, NH, has
shown the formation of dichloro-and  1,1,1-trichloroacetone upon chlorination.'01
Suffet et al. previously found 1,1,1-trichloroacetone in two tap  waters, but not in the
respective source waters.150
  Furthermore, even simple aromatic hydrocarbons have been observed in some
studies to be more prevalent or in higher concentrations in finished tap waterthanin
the  respective raw source water.151*152 With regard  to some  hydrocarbons, sub-
sequent  in-house USEPA studies  have shown that  biodegradation of  these
compounds during sample transit and storage are important considerations and may
have occurred to a greater extent in the undisinfected source water samples than in
the chlorinated finished water samples. The result  would be an apparent increase in
compound concentration in the finished water when little or no  increase had actually
occurred.
  The best known reactions of free chlorine with aromatic compounds in the water
treatment field are those that occur with phenols.153 Chlorine reacts rapidly with
phenol to form mono-, di-, and tri-chloro derivatives. These compounds are highly
odorous and are slowly decomposed  by excess chlorine. Other phenolics  and
substituted aromatics can also be  chlorinated.15'1
  Samples  collected  by  USEPA   at eight  utilities   show  that  significant
concentrations of halogenated disinfection  byproducts  other than the trihalo-
methanes (as measured by the organic halogen test70) are formed in many cases, and
that the ratio of nontrihalomethane halogenated byproducts to the trihalomethanes
varies from location to location (Table 62).M
  Chlorine Dioxide—Organic Byproducts—Although chlorine dioxide does not
react  to  produce trihalomethanes, considerable evidence indicates that chlorine
dioxide does react with organic material during water treatment and, like chlorine,
is therefore likely to produce other organic byproducts. Specific observations about
this likelihood are as follow:

  1. Because chlorine dioxide is a good disinfectant, some reaction does take place
between the cell components of the organism and the chlorine dioxide.
  2. Even though chlorine dioxide does not react with ammonia, most waters exhibit
a chlorine dioxide demand similar to (but  somewhat  less  than) that of chlorine
(Figure 109).
  3. At applied chlorine dioxide concentrations higher than those encountered in
drinking  water treatment, identifiable  byproducts have been isolated.155
  4. Chlorine dioxide destroys phenolic compounds when the oxidant is used for
taste and odor control in water supplies.120
  5.  Most important, as shown in Section  VII, Subsection Oxidation (Chlorine
Dioxide), the presence of chlorine dioxide reduces the formation of trihalomethanes
by chlorine. This and other evidence obtained  by Miltner indicated that chlorine

                              Section VIII. Use of Alternative Disinfectants  185

-------
dioxide reacts with  natural humic acids.*9 Such Information is not surprising,
because chlorine dioxide is effective for reducing  the concentration of color in
drinking water supplies."6
  The possible formation of organic byproducts arising from the use of chlorine
dioxide as a disinfectant in drinking water was first considered by USEPA on the
basis of the existing literature. An in-house laboratory study followed to determine
the validity of  extrapolations  from  the  literature that described  work where
concentrations of oxidant and organic materials were generally high.
  As a result, a brief review of the literature considered pertinent to drinking water
applications was presented by Stevens et al.,IST although a much more extensive and
complete review of chlorine dioxide chemistry is available elsewhere.153 Briefly, the
literature  describes  chlorinated and nonchlorinated derivatives (including acids,
epoxides, quinones, aldehydes, disulfides, and sulfonic acids) that are products of
reactions carried out under conditions somewhat different from those experienced at
water treatment plants.

    TABLE 62. ORGANIC HALOGEN (OX) IN FINISHED WATERS*38

              Nonpurgeable OX       Purgeabla OX (POX)
          (NPOX)f concentration,       (mostly TTHM)
  Utility	pg/LasCI"	^g/L as CI"       NPOX/POX Ratio
A
B
C
D
E
F
G
H
17
NF$
52
36
165
136
66
98
9.8
NF
64
31
180
114
133
27
1.7
—
0,8
1.2
0.9
1,2
0.5
3.6
•Raw watars did not contain OX.
tNPOX » Tha concantrallon of organic halogan that rttnalhi in • «imp1e after It hat baan
       purgad for a trlhalomathaae analysis.
$Non< found.

  Nonetheless, because of  the potential  for  undesirable byproduct formation
resulting from chlorine dioxide disinfection of drinking water, an in-house investi-
gation was begun at the USEPA laboratory to determine if byproducts of the type
predicted by the literature (where reactions described were carried out at generally
higher concentrations) would prevail under drinking water disinfecting conditions.
This work was carried out in two phases:
  1. A search of gas chromatographic data for differences in purgeable compounds
found in chlorine-dioxide-treated and  untreated waters, and
  2. Development and  use of a more elaborate analytic scheme to detect products
of a more diverse nature, specifically  those expected from reactions of phenolic
compounds.
  The semiquantitative  results of the first phase have been briefly described in the
literature where Cj through Cj aldehydes were noted to increase in concentration
after treatment of a natural water with chlorine dioxide.1" In that work, no other
dramatic differences were observed between treated and untreated samples with
regard to compounds amenable to the purge-and-trap3 type of chromatographic
analysis used.7'2''""
  Phenol was selected as the model compound for the beginning of the second phase,
primarily because of  the  supposed  polyphenolic nature  of humic  materials
(trihalomethane precursors that make up a large fraction of the organic material
present in natural waters where trihalomethane formation is a problem)  (Figure
110).'"Table 63 presents the results of one experiment where phenol was exposed to
varying molar ratios of ClOj to phenol.

186  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                             DISINFECTANT DOSE, mg/L

         Figure 109.  Comparison of disinfectant demands for Ohio River
                      water, November 17, 1975. pH 7.5; 23 ntu; stan-
                      dard plate count 10,000/mL; total coliform density
                      700/100 mL"
  The data in Table 63 show that chlorophenols were produced at low molar ratios
(4/5) of chlorine dioxide to phenol. Higher ratios (I4/5 and I4/1) did not produce
chlorophenols, but they did favor hydroquinone formation. This effect was expected
to some extent, based on the literature,157'15*"161 even though odorous chlorophenolic
materials are avoided in drinking water through the use of chlorine dioxide.  "Other
expected  organic  byproducts such  as  oxalic and maleic acids,  and 2,6-  and
2,5-dichioro-p-benzoquinone were not  immediately  identifiable, although total
'organic carbon  concentration data  indicate that  the phenol  is not completely
converted to carbon dioxide. To date, no gas chromatographable compounds in this
category that were not present in the untreated sample  have  been identified in
chloririe-dioxide-treated natural waters or in humic-and fulvicacid solutions. Note
that detection limits were estimated to be in the range of 5 to 10 /ig/ L as phenol.
  The finding of individual identifiable species from the chlorine dioxide treatment
was" not necessarily expected because of the polymeric nature of the  natural humic
material  in contrast to the monomeric phenol model. To investigate the possible
formation 6f higher molecular weight chlorinated species that could not be identified
by gas chromatographic techniques, humic acid was added to chlorine dioxide at two
different chlorine dioxide to carbon (CICh/C) ratios. To compare yields of organic
halogen, two reaction ratios with corresponding electron equivalents to chlorine
Were  included in the experiment. That is, the molar ratios 1/15 and 1/3 selected for
CIOs/C  correspond  to  the  molar ratios 1/3 and 5/3, respectively, selected for
                               Section VIII. Use of Alternative Disinfectants  187

-------
Cb/C (Table 64). The basis for this correspondence is that chlorine dioxide going
to chloride requires 5 electrons perchlorine atom, whereas chlorine going to chloride
requires only one electron per chlorine atom.
                                                          COOH
          OH
                                                                   —IN
          Figure 110.  A  proposed  humic structure.168 (Adapted from
                      JOURNAL American Water Works Association,
                      Volume 58, No, 6 [June 1966J by permission. Copy-
                      right 1966, the American Water Works Associa-
                      tion.)
   TABLE 63. PRODUCTS RESULTING FROM CHLORINE DIOXIDE
                       TREATMENT OF PHENOL
Percent yield from phenol*
ClOj/phonolf
mol/mol
4/6
14/5
14/1
o-chloro-
phenol
11
NF*
NF
phenol
(recovered)
3O
NF
NF
2,4-dichloro-
phenol
0.3
NF
NF
p-chloro-
phenol
13
NF
NF
p-hydro-
quinone
3,B
7.2
45
Total
recovery
58
7.2
46
•Ruction time * 4 hour»,
fin mg/i.! 4/8 = 43.S/7S, 14/B = 1iO/75, and 14/1 = 184/18.
$Nona found.
  According to the chlorination data (Table 64), the organic halogen yield is much
higher than the chloroform yield for the I-hour reaction time and increases with
chlorine  dose,  the chloroform concentration  remaining essentially  constant.
Chlorine dioxide produced some (but  less) organic halogen and, as expected, an
insignificant  concentration  of chloroform.  The  trend toward  less  halogen

188  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
substitution at the higher CICh/C ratio, observed with phenol reactions, was not
observed here; however, this  interpretation is complicated by the longer reaction
time that was allowed at the higher chlorine dioxide dose. Factors Influencing
organic halogen yields relative to trihalomethanes from all disinfectants are now
under investigation in the USEPA laboratory,

       TABLE 64. REACTION OF HUMIC ACID WITH CHLORINE
                       AND CHLORINE DIOXIDE
Oxidant/C
ratio.
mol/mol
CI./C:
1/3
5/3
CIOZ/C:
1/15
1/3

CI2,CIO2 doses.
mg/L

3.8
19.4

0,75
3.7
Reaction
time.
hr

1
1

1
2

CHCIj,
jjg/L

39
32

0.4
1.6 .

OX,
/ig/L as Cl~

198
278

23
52.5
  Inorganic Byproducts—As noted above, when chlorine dioxide reacts with organic
compounds to oxidize them, the byproduct chlorite (ClCh~) is formed. Furthermore,
as chlorine dioxide disproportionates in water, both chlorite and chlorate (ClOj~) are
formed as byproducts. The relative proportion of these byproducts was determined
during a USER A in-house study in which 1.5 mg/ L of chlorine dioxide was added to
Ohio River water that had been treated in a pilot plant. "2 The data in Table 65 show
that approximately 50 percent of the original chlorine dioxide was converted to
chlorite, about 25 percent to  chlorate, and approximately 25 percent to chloride.162
Thus when chlorine  dioxide is  used as an alternative disinfectant, the health
significance of  inorganic anions other than chloride  (the sole  major  inorganic
byproduct of chlorine treatment) 'must be considered. These  inorganic byproducts
are  unique to chlorine dioxide.

TABLE  65.   INORGANIC  CHLORINE  DIOXIDE   BYPRODUCTS*'"
Initial concentration.

Species
CIO,
cior
CIO^
cr
Total

mg/L
1.5
—
—
17.9
—

mg/L as Cl~
0.8
—
—
17.9
18.7
Final concentration.

mg/L
0
0.7
0.4
18.1
— -

mg/L as Cl~
0.1
0.4
0.2
' 18.1
18.7
Percent
CIO2
demand
—
50
25
25
100
*1,6 mg/L CIOt added to coagulated, settled, dual-media filtered Ohio River water.
 Reaction time ~ 42 hours; pH s 7,1,
  Chloramines—The potential for formation of organic byproducts as a result of
disinfection  with  chloramines is  not  as  obvious  as  with chlorine  dioxide.
Chloramines  are weaker disinfectants (less reactive with cells)  compared  with
chlorine  and  chlorine  dioxide, and  waters generally  exhibit  a much lower
disinfectant demand when chloramines are used. Because chloramines do hydrolyze
to form traces of free chlorine (see Subsection Disinfectant Chemistry Effects earlier
in this section), some reaction  products of this oxidant might be expected, but at
                               Section VIII. Use of Alternative Disinfectants   189

-------
much lower concentrations in a given time than when free chlorination is practiced.
Except for chlorine exchange reactions with primary and secondary amines present
in treated waters, information regarding specific byproduct formation  from
chloramines under drinking water treatment conditions is virtually absent from the
literature."1
  Sontheirner, reporting on research performed at Stuttgart, Federal Republic of
Germany, showed that chloramines do produce some organic halogen when they are
used as the disinfectant, although the concentration is considerably lower than that
produced when free chlorine is the disinfectant140 (Table 66).
TABLE 66. ORGANIC HALOGEN FORMATION IN DRINKING WATER AT
          STUTTGART, FEDERAL REPUBLIC OF GERMANY""

               Type of                            Dissolved organic
            treatment and                              chlorine
 	water	  M9/L as Cl~	
With breakpoint chlorination:
      River                                             50
      Sedimentation basin effluent                        640
With combined chlorine residual:
      River water                                        23
      Sedimentation basin effluent                         72
  Ozone—Ozone is a highly reactive oxidant that might be expected to produce
oxidation products of organic materials found in water supplies. Unlike the oxidants
chlorine, chlorine dioxide, and chloramines, however, ozone would not be expected
to produce chlorinated byproducts.
  Although much is known about ozone reactions in other media, surprisingly little
information exists about the action of ozone as an oxidant of organic compounds in
aqueous solution. This lack of data exists even though ozone has been in widespread
use for decades as a water and wastewater disinfectant. The sum of knowledge in this
area is summarized in a recent National Academy of Science Literature Review.'63
This document suggests that oxygenated products such as ketones, aldehydes, and
acids are most likely formed from alcohols and olefinic double-bond and aromatic
ring cleavage.
  Of the few studies performed in connection with drinking watertreatment, a'study
by  Schalekamp  is  the  most  revealing concerning  byproduct formation.
Sehalekamp analyzed water before and after an ozone treatment step at various
ozone doses. He found that the concentration of total aldehydes and ketones rose by
a factor of more than 10 as the ozone dose increased from 0 to 5 mg/ L and declined
slightly when the ozone dose was changed from 5 to 7 mg/ L. The data in Table 67
show the increases  in specific aldehydes during  these  studies (note that  the
concentrations are in nanograms per liter).
  Sievers et al.  also found  the  same aldehydes and reported some apparent
hydrocarbon formation upon ozonation of  the effluent from  a secondary waste
treatment plant in  Estes Park, CO.165 To date, no other studies of actual in-plant
treatment byproducts have been reported.

  Summary—Individual Compounds—The  following  is  a quotation  from  the
conclusion of National Academy of Sciences review of the literature on disinfection
byproducts for the USEPA,16'

ISO  Treatment Techniques for Controlling Trihatomethanes  in Drinking Water

-------
  Nonetheless, it, is clear that each disinfectant chemical that was examined in this survey
produces by-products that  may occur in actual water treatment applications. Of particular
concern are the following substances that result from the use of the various disinfectants,
  •  From chlorine: the trihalomethanes (TH M's), trichloroacetone (CCUCOCH j), and other
     largely uncharacterized chlorinated and oxidized intermediates that are formed from the
     complex set of precursors in natural waters; chloramines; chlorophenots; and the largely
     unknown products of dechlorination.
  •  From ozone: epoxides which may in principle result from unsaturated substrates such as '
     oleic  acid, although none have yet been found in drinking water; peroxides and other
     highly  oxidized intermediates such  as glyoxal (OHCCHO)  and  methyglyoxal
     (CHjCOCHO) from aromatic precursors.
  •  From bromine and iodine: TH M's and other bromine and iodine analogs of chlorinated
     species; bromophenols,' bromoindoles, and bromoanisoles; plus the halogens themselves,
     which may remain in drinking water as residual,
  »  From chlorine dioxide: chlorinated aromatic compounds; chlorate (ClOsl and chlorite
     (CIO:") which are often present  as by-product or unreacted starting material  from
     production of chloride dioxide; and chlorine dioxide itself.
  This list, incomplete as it is, is compelling in that  it shows that  each disinfectant
produces chemical side effects that should  be examined in more  detail before the disin-
fectant is  widely adopted  for  water treatment. It  is clear that each of  these  disinfect-
ants, being highly reactive chemical agents, will have inevitable side effects.

   Organic Halogen—Two in-house USEPA  studies compared the formation of
organic halogen when four different disinfectants were used.  In these experiments,
Ohio River water that had been coagulated, settled, and filtered in the pilot plant was
disinfected  with free  chlorine, chloramines,  chlorine  dioxide,  and  ozone.  The
resulting samples were then analyzed for organic halogen. For this experiment, these
data show that organic halogen is formed by the action of these disinfectants in the
following order of yield (Table 68):

            free chlorine > chloramines > chlorine dioxide  > ozone

In this case, the disinfectant dose varied among samples and was adjusted (except Oj)
to be roughly equivalent to the 2-day disinfectant demand. In Test 1, the OX was
approximately   1/4  trihalomethanes  and  in Test 2,  1/10  trihalomethanes;
trihalomethane formation was  insignificant  for  the other disinfectants.  Under
circumstances where the disinfectant dose was equivalent among the tests, the order
of organic halogen production might change. Ozone formed  no organic halogen in
either test when compared with the no-disinfectant control.  The chlorine dioxide
data confirmed the findings presented in Table 64.
   Although  information  on  byproducts  other  than  trihalomethanes   from
disinfection is currently limited, the data presented here indicate that sufficient evi-
dence is available to show that these byproducts certainly do occur. Furthermore,
although the health effects have not yet been evaluated, research is under way  in an
attempt to provide this  information.7''""'166'"7 Although these byproducts are not
currently regulated, water purveyors should make every effort to minimize  their
concentration in finished drinking water.

Discussion

   The  data presented in Section V!ll indicate that none of the three alternative
disinfectants   investigated   extensively—chloramines,   chlorine  dioxide, or
ozone-—will react  with humic  acids or other  precursor  materials  to  produce
significant concentrations of trihalomethanes. This conclusion was reached  first in
the laboratory and then verified with many case histories of actual experiences on the
treatment-plant scale. Nonetheless, the use of disinfectants other than free chlorine
to control trihalomethanes has advantages and disadvantages, which are discussed
in the following subsection.

                                Section VIII. Use of Alternative Disinfectants   191

-------
•

5"
3
                    TABLE 67. FORMATION OF ALDEHYDES IN WATER TREATED WITH VARIOUS

                                OZONE DOSES AT THE LENGG WATERWORKS1"
                                                  (ng/L)
Ozone dose, mg/L
Aldehyde
Hexanal
Heptanal
Octanal
Nonanal
Decanal
Undecanal
Dodecanal
Tridecanal
Tetradecanal
1
Before O3
NF'
8
6
7
12
NF
NF
NF
12
2.5
After O,
40
82
74
160
260
40
28
NF
26
Before O,
NF
30
22
34
36
NF
16
NF
10
After O3
78
140
190
340
240
64
24
12
6
5
Before O3
NF
18
16
26
38
NF
NF
NF
NF

After O,
74
145
320
680
920
82
58
24
30
7
Before O,
NF
20
26
55
80
26
24
20
20

After O3
24
68
110
164
134
16
12
8
4
              'None found.
3'
 '
                     TABLE 68. FORMATION OF ORGANIC HALOGEN (OX) IN OHIO RIVER WATER

                                   TREATED WITH VARIOUS DISINFECTANTS

                                                     as en

Test 1
Test 2
Free chlorine
194(2.5 mg/L)*
53(3.3 mg/L)
Chloramines
101(2.0mg/L)
26(0.8 mg/L)
Chlorine dioxide
61 (3.0 mg/L)
17(2.4 mg/L)
Ozone
9(3.0 mg/L)
11 (1,0 mg/L)
No disinfectant
(control)
17
13
               •Disinfectant 
-------
Summary of Advantages and Disadvantages to Using Alternative
Disinfectants for Trihalomethane Control

Advantages of Using Alternative Disinfectants—

  The major advantage to using alternative disinfectants is the ability to lower
trihalomethane concentrations near detection limits in most cases through the use of
any of the three  alternative disinfectants  studied (chlorine dioxide, chloramines
[combined chlorine], or ozone). Furthermore, two of the alternative disinfectants,
chloramines and  chlorine dioxide,  can readily be prepared and fed  at a water
treatment  plant,  although careful attention  is needed  to  maintain a  low
concentration of chlorine in the chlorine dioxide. In addition, worldwide experience
with the use of all three of these disinfectants already exists, giving water treatment
plant designers and operators confidence in their use. Finally, two of the alternative
disinfectants, chlorine  dioxide and ozone, are excellent disinfectants and their
disinfecting power is consistent over the pH  range usually encountered in water
treatment; the third, combined chlorine, is a weaker disinfectant, but it is adequate in
many cases.

Disadvantages of Using Alternative Disinfectants—

  The major disadvantage to using alternative disinfectants as a technique for
controlling trihalomethane concentrations is that  because  they are  themselves
oxidants, they will produce other organic byproducts unless the organic content of
the water is  lowered.  This disadvantage  is  analogous  to  the removal of
trihalomethanes  themselves (such  as  by  aeration) after  they are formed by
chlorination.  Little evidence  exists at  the present time to indicate whether the
byproducts of the alternate disinfectants are more or less safe to consumers than the
non-trihalomethane byproducts of chlorination.
  Thus,  although the  trihalomethane  concentration  of the  finished  water is
improved, the overall water quality may not be equally improved because the health
hazard of the  organic  byproducts that may be formed has yet to be completely
evaluated,"'146'166'167  Additionally, each of  the disinfectants itself has inherent
disadvantages; for example, ozone does not produce a residual for the distribution
system, chloramine is a weaker disinfectant than free chlorine and may itself have
some  toxicity,168 and chlorine dioxide produces chlorite and'chlorate as inorganic
byproducts—anionic species   whose  health  effect  is currently unknown."'145
(Because of the  potential  toxicity of  chlorite  and chlorate,  the USEPA  has
recommended  in  the  Trihalomethane  Regulation'  that  the  total  residual
concentrations of chlorine dioxide, chlorite, and chlorate be limited to 0.5 mg/L in
drinking water).
  Finally, water is used for many purposes in a community—industrial, medical,
and nonpotable domestic uses such as houseplants, tropical fish, and so forth. Thus,
any change in  the  chemical  makeup  of  drinking  water, such as a  change in
disinfectant, may cause some problems in the community. For example, chloramines
cause difficulty to kidney patients usingdialysis machines'69 and can cause problems
to those raising tropical fish  (L. Harms, South  Dakota  School of Mines  and
Technology, 1979, and  P. Lassovszky, USEPA, Washington, D.C., 1980. personal
communications).
                              Section VIII. Use of Alternative Disinfectants  193

-------
                              SECTION IX
            MAINTAINING BACTERIOLOGIC QUALITY

Background

  The microbial barrier concept in the treatment of drinking water is of particular
importance in the processing of unprotected surface waters laden with a variety of
sewage inputs, stormwater, and animal waste discharges. Groundwater may also
become contaminated with seepages of landfill leachates, migration of organisms
from land application of sewage effluents, or movement of wastes in sewage lagoon
basins through ground faults to the aquifers below, AH of these sources of pollution
often  contain pathogenic bacteria, viruses, yeasts, and multicellular  parasites.
  Effective water treatment has had a major impact on the reduction of waterborne
disease.  Where  waterborne disease outbreaks have  occurred, deficiencies  in
treatment  (particularly  filter  breakthrough  and  inadequate  or interrupted
disinfection) have been major causes of the problem. For this reason, maintaining
the integrity of the treatment barrier is essential as treatment changes are made to
meet the requirements of the Trihalomethane Regulation3 (see Sections VI-V1I1),
  The treatment  changes most  likely to  alter the transport  and  fate  of
microorganisms within the treatment chain involve: 1) lowering the trihalomethane
concentration by changing the point  of chlorination to follow clarification (see
Section VII,  Subsection  Clarification), 2) organic chemical removal by biologic
activity during GAC adsorption (see Section VI1, Subsection Biologic Degradation),
and 3) changes in types of disinfectant and  disinfectant application (see Section
VIII),  This section  discusses  the impact of these treatment processes on  the
bacteriologic quality of finished water and,  where possible, the influence on the
bacteriologic quality of distributed water.

Removal of Trihalomethane Precursors

Clarification—Changing Point of  Chlorine Application—
  Although the primary  reason  for  the  use  of  disinfectants in potable  water
treatment is to kill or inactivate pathogenic organisms that may be present, source
water chlorination has often been used for a variety of other reasons:

  1. To oxidize hydrogen sulfide  and similar objectionable compounds  in source
    water,
  2. To improve coagulation of waters containing iron and manganese,
  3. To aid in maintenance of filtration sand beds by  preventing slime growths,
    algal formation, and other organic deposits, and
  4. To  limit microbial populations  applied  to filters,  thereby enabling  more
    uniform efficiency in bacterial reduction in that part of the treatment chain.

  As  can be seen from several of these benefits for source water chlorination,
locating the point of chlorine application near the end of the treatment chain could
impose  an  increased  burden on coagulation, filtration,  and clarification  to
perpetuate a high level of microbial reduction in the processed water. In two full-
scale field evaluations of a change in  the chlorine application point from source
water to clarified water, variation in the water utility source waters and clarification
processes resulted in two different in-plant conditions,18'170

134   Treatment Techniques lor Controlling Trihatomethanes in Drinking Water

-------
   The  Pittsburgh,  PA, Department  of Water  routinely chlorinated untreated
 Allegheny River water. Water quality data representative of 2 weeks of sampling
 during routine treatment and 2 weeks of sampling during modified treatment are
 presented in Table 69. These data indicate that chlorination of source water before
 clarification resulted in a reduction of the mean total coliform density from 6,200
 organisms/100 mL in the source water to <1 total coliform/100 mL in the clarified
 water. The modified treatment scheme produced a similar reduction of the source
 water total coliform population (from 6,300 organisms/100 mL to <1 organism/100
 mL) before the application of chlorine. With this scheme, coagulation and settling
 combined with the application of P AC for taste and odor control and approximately
 1  mg/L potassium permanganate for  manganese control during clarification and
 before chlorine application were as effective in coliform reduction as source water
 chlorination and clarification combined. Some evidence of a delay in the reduction
 of standard plate count until after  chlorine application did, however, occur.
   Changing the  point of chlorine application  was also studied at the Cincinnati
 Waterworks (OH) in a series of 2-week study periods." During routine treatment
 plant operation,  chlorine was applied to the source water after 48 hours of open
 reservoir storage. Adequate retention time of source water is in itself a beneficial first
 step in microbial  population reduction through self-purification processes; it is also a
 buffer  against temporary impairment  of  water quality from some accidental
 upstream spill of industrial chemicals. In the Cincinnati water treatment operation,
 coagulant is added to the open reservoir, and chlorine is routinely applied ahead of
 in:plant treatment processes. The modified chlorine application took place after an
 additional 4-hour clarification  process consisting of coagulation and settling.
   The results of both the routine and modified treatment schemes show that 48-hour
'source  water storage with  alum treatment reduced the total coliform densities by
 approximately 97 percent, and the turbidities by approximately 90 percent (Table
 70).18*170 The coagulation and settling process, however, had little effect on further
 turbidity reductions, and  further reduction of the coliform  population was only
 about 50 percent. Locating the point of chlorination after coagulation and settling
 resulted in an intrusion of coliforms into the early stages of water treatment and
 placed increased  importance on maintaining an effective disinfection process at this
 stage to reduce  the burden  on filtration. The apparent persistence of a residual
 standard plate count into the filtration stage, regardless of the point of disinfection,
 illustrates the chlorine-resistant nature of some of these organisms. In either event,
 neither a measurable change in the bacterial quality  of the finished water, nor any
 apparent in-plant problems developed as a result of the modified treatment scheme.

 Granular Activated  Carbon  Adsorption—
   Coliform and  Standard Plate Count Organisms—In the adsorption of organic
 substances, including those that may be trihalomethane precursors, GAC particles
 become focal points for bacterial nutrients and also provide suitable attachment sites
 for  microbial habitation. Although the portion of organic removal in this process,
 possibly attributable to biodegradation, is small compared with physical adsorption
 to the activated carbon surface, a substantial microbial population develops at the
 water-activated  carbon surface interfaces. This process  can therefore   be  of
 microbiologic concern in  that  treatment  barriers must remain effective against
 increased bacterial population densities that can include regrowth of indicators and
 selective adaptation by some organisms that are disinfectant-resistant, opportunistic
 pathogens, or known antagonists to coliform detection. As a result of these concerns,
 the  bacteriologic conditions  associated with virgin GAC placement and full-scale
 use  in the  sand replacement  mode were evaluated at two utilities.18
   A pilot-scale investigation of GAC adsorption was conducted at the Huntingdon
 Water Corp., Huntington,  WV. A single bed of virgin  WVW 14x40 GAC, selected
 for  its history of  effective taste and odor control, was evaluated for trihalomethane
 control and for its effect on microbiologic densities.  A 0.8-m (2.5-ft) layer of GAC

                                Section IX, Maintaining Bacteriologic Quality  19S

-------
CO
OS
•a*
q

-------
                  TABLE 70, CHLORINE APPLICATION POINT STUDY USING OHIO RIVER SOURCE WATER

                                      AT THE CINCINNATI, OH, WATER WORKS1**170
Cfl
a
5'
5
3'

I
CO
D

g
Mean value at various sample points*
Clj application to source water CI2 application to
stored 48 hr and treated with alumf coagulated and settled waterj
Stored Coagulated Stored Coagulated
Source
Parameter water
Flow time.
hr 0
Turbidity, ntu 32
Total coliforms/
100 mL 9,600
Standard plate
count/mL §
pH 7.3
Free CI2 residual.
mg/L §
Total CI] residual.
mg/L §

source
water

48
1.0

200

§
7.0

§

§

and settled Filtered Finished Source source and settled
water

52
1.2

<1

600
8.5

1.8

2.0
1
water water water water

52.5 55.5 0 48
0.11 0.10 14 0.80

<1 <1 84,000 2,400

<1 6 § §
8.3 8.7 7.6 7.2

1.6 1.5 § §

1.8 1.6 § §

Clj application.

3.6
mg/L

water

52
1.1

1,400

5,600
8.1

0

0

Filtered
water

52.5
0.07

<1

15
8.1

1.8

2.0
t
Finished
water

55.5
0.06

<1

<1
8.2

1.4

1.5

CI] application.
3.3
mg/L

                •Two-waok umpfe period, Mv*a umplas,

                fSource water temperature = 24°C (76°F|.
                JSource water Mrnptratuni = 22°C (?2°F).

                §Not run.

-------
was placed on top of 0.3 m (1 ft) of sand and gravel and then backwashed several
times to remove fine particles. When the bed was placed in operation, it received
water that had been chlorinated, coagulated, and settled. The flow through the bed
represented only 8 percent of the flow through the entire plant.
  Results of this investigation are summarized in Table 71. The mean total coliform
density in  the  source  water  during  the  32-week  study period  was 3,400
organisms/100  mL.  Following chlorination, coagulation, and settling, the total
coliform density in the influent to the GAC bed was found to be <1 coliform/ 100 mL
at the time of sampling. The standard plate count in this water (aside from one
indeterminant high value) ranged from 4 to 55 organisms/ mL. On passing through,
the activated carbon filter/adsorber, some deterioration in the bacterial quality
occurred during  the first 9  weeks of operation,  when warm  water conditions
prevailed. At that time, 1 to 8 total coliforms/100 mL were found in the GAC
filter/adsorber effluent, but this occurrence was not accompanied  by a significant
increase in the standard plate count. No correlations with turbidities or peak total
coliform loadings could be made. Note that GAC treatment did consistently reduce
turbidity.
  These data suggest that total coliforms did occasionally break through early
treatment stages,  which included chlorination, but  because  of the infrequent
sampling, they were not detected in the  activated carbon filter/adsorber influent.
Although these total coliform occurrences could not be related to one or more breaks
in the early stages of the treatment  barrier, the data dp indicate that coliforms may
persist for some time or possibly multiply in an activated carbon filter/adsorber bed
provided with inflows of warm water. Although not shown in Table 71, application
of chlorine following the GAC filtration/adsorption was found to be adequate in
maintaining a finished  water quality of 
-------
        TABLE 71. SAC STUDY USING OHIO RIVER SOURCE WATER AT THE HUNTINGTON, WV, WATER WORKS1*
§
>5

I
I'
D
s
5°
CO
Source water


Week
1
2
3
4
6
6
7
8
9
10
11
12
13
14
15
16
17
20
22
23
25
27
32
•Tr«o«.
tNot run.
Temper-
ature,
°C
27
28
28
28
28
27
26
27
27
27
26
24
19
19
14
16
15
11
8
6
3
2
2


Turbid-
ity,
ntu
14
21
26
13
15
80
37
34
17
18
26
24
47
98
34
22
18
42
240
160
24
30
34


Total
coliformi/
100mL
1,600
1,200
910
870
1,800
3,000
5,300
2,300
1,400
970
1,100
1,700
3,100
4,300
3,900
2,600
3,000
3,900
1,400
26,000
2,800
5,900
610


GAC influent (chlorinated,
coagulated, settled water)
Residual
chlorine.
mg/L
Free
0.8
0.3
1.8
0.6
0.6
0.5
0.4
0.3
0.6
0.6
0.4
0.6
0.6
0.6
0.5
0.6
0.4
0.6
0.2
0.6
0
0.9
0.3


Total
1.4
0.4
3.7
0.7
0.9
0.8
0.7
0.6
0.7
0.7
0.6
0,7
0.8
0.9
0.7
0.9
0.9
0.8
0.3
0.6
0.7
1.1
0.9


Turbid-
ity.
ntu
2.0
4.6
4.9
4.4
6.6
6.8
3.8
6.9
3.3
4.6
7.9
4.4
8.7
4.3
16
9.1
10
5.6
9.8
8.0
7.0
9.0
14


Standard Residual
Total plate chlorine.
colrforms/ count/
1 00 mL ml
<1 4
<1 62
<1 42
<1 7
<1 18
<1 28
<1 17
<1 22
<1 24
<1 26
<1 28
<1 28
<1 31
<1 t
<1 34
<1 39
<1 18
<1 >200
<1 66
<1 36
<1 30
<1 f
<1 t


mg/L
Free
0
0
0.1
•
0.4
0.1
*
0.2
*
9
*
11
*
0.1
t
*
*
0.3
0.2
0.2
0
0.3
0.4


Total
0
•
0.3
0.3
0.6
0.2
0.1
0.4
0.2
0.2
0.2
*
0.2
0.4
t
0.6
0.6
0.4
0.4
0.3
0.6
0.5
0.8


GAC effluent
(WVW 14x40)
Turbid- Total
ity, colforms/
ntu 100 ml
0.21 <1
1.6 <1
1.4 6
1.7 8
1.8 6
1.1 <1
0.64 <1
1.6 2
0.27 2
3.2 <1
1.7 <1
0.36 1
0.42 <1
0.44 <1
0.44 <1
0.97 <1
0.47 <1
0.65 <1
12 <1
0.78 <1
0.50 <1
0.15 <1
0.34 <1



Standard
plate
count/
ml
100
53
12
41
18
13
3
25
46
140
23
12
30
t
2
10
2
4
11
3
<1
t
t



-------
               TABLE 72, 6AC STUDY USING BEAVER RIVER SOURCE WATER AT THE BEAVER FALLS, PA. MUNICIPAL AUTHORITY"."*
1
3'
53

I
I'
1
2
3
4
S
6
7
8
9
10
11
12
13
14
IS
17
18
22
23
25
27
29
32
21
21
15
11
18
16
IS
10
10
8
6
3
4
2
1
1
1
1
4
4
7
10
11
44
28
22
9.5
7.5
9
10
9
16
10
14
10
22
10
10
12
8
14
10
ISO
12
8
6
91,000
71,000
140,000
150,000
39,000
190,000
80,000
98,000
220.000
120,000
120,000
69,000
89,000
75,000
65,000
48,000
27,000
6.000
23,000
84,000
13,000
24,000
8,400
2.0
1.7
U
1.1
1.2
1.4
1.1
1.0
1.3
1.0
1.4
1.0
1.2
1.3
1.0
1.4
1.0
0.4
0.3
t
t
0.2
0.2
t
1,7
1,4
1,3
1.4
1.6
1.2
1.0.
1.6*
1.3
1.6
1.1
1.7
1.5
1.2
1.7
1.1
1.6
1.6
1.4
1,4
1.1
1.6
5.6
4,8
2.3
2.9
2.5
3.3
3.6
3.2
4.6
4.5
3.7
5.9
4.6
6.6
4.8
5.9
5.5
6.4
5.8
6.6
6.3
1.7
1.9
<1 t
<1 t
<1 t
<1 100
<1 800
<1 350
<1 10
<1 42
2 110
<1 33
<1 95
1 360
<1 660
1 200
<1 120
<1 150
<1 33
<1 30
<1 24
<1 38
<1 58
<1 33
<1 17
0 0
0 0
0 0
0 0
0 0
*<0.1
t<0.1
* <0.1
t *
t<0.1
t <0,1
t<0.1
t <0.1
t t
t <0.1
t <0.1
t <0.1
* 0.3
t 0.4
t 0.2
t 0.1
t 0.1
t 0.3
64
75
98
45
34
42
28
22
13
12
2
1
<1
1
<1
<1
<1
<1
M 8K n.di. iKbinti mi btiew 1 ntu.

-------
                      TABLE 73. RESULTS OF ADDITIONAL SAMPLING DURING GAC STUDY USING

                   BEAVER RIVER SOURCE WATER AT BEAVER FALLS, PA, MUNICIPAL AUTHORITY18."0
Cfl
I
a'
t»
3'

I'
f>

Q


|

•?'
GAC effluent
Source water



Week
53
54
55
56
57
58
59
60
61
62
63
64

Temper-
ature.
00
26
23
22
19
14
12
14
13
11
9
8
6

Total
coliforms/
100mL
1 8,000
10,000
22.000
9,200
31,000
10,000
8,700
19,000
5,000
12,000
82,000
8,000
GAC influent Filtrasorb® 400
Free
chlorine
residual.
mg/L
1.4
.2
.6
.6
.4
.1
1.4
1.3
1.5
0.8
1.2
1.0
Free
Total chlorine
coliforms/ residual.
100 mL mg/L
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t
<1 t

Total
coliforms/
100 ml
100
120
230
470
62
44
30
8
t
1
<1
<1
Filtrasorb® C*
Free
chlorine
residual,
mg/L
t
t
t
t
t
t
t
t
t
t
t
t

Total
coliforms/
100 mL
64
25
21
5
9
10
3
<1
2
<1
<1
<1
HD
Free
chlorine
residual.
mg/L
t
t
t
t
t
t
t
t
t
t
t
t
8x16

Total
coliforms/
100 mL
130
240
730
330
82
55
31
9
<1
<1
<1
<1
                •Not commercially available.

                fTrace.

                JNot run.

-------
all  three activated carbon filter/adsorber beds exceeded influent densities of <1
organism/100  mL when  temperatures  were  above  10°C  (50°F).  When  the
temperature again dropped below 10°C (50°F), effluent total coliform densities
returned to  below detectable  levels in  100 mL. High initial  total coliform
occurrences may also be attributed to the difficulty of disinfecting adsorption beds
when putting them into service. These field data confirmed the similar observation
from the Huntington,  WV, study (Table 71). They also suggest that occasional
coliform penetration past the early stages of treatment and  before filtration can
occur, and that these organisms may become temporarily established in the activated
carbon  filter/adsorber  effluent.
  Both coliform and standard plate count density increases during GAC treatment
were much more pronounced at Beaver Falls, PA, than at Huntington, WV. Higher
levels of total coliform contamination in the source water for Beaver Falls also
suggest that nutrient levels in that source water may have been higher. This condition
would tend to support growth in GAC adsorbers. No TOC data were available, but
the THMFP was somewhat higher at Beaver Falls than at Huntington. THMFP
declined as temperature and organic concentrations also dropped. These changes
contributed  to a parallel recession in the  bacterial population. The variability in
results observed at these two plants points up the need for close monitoring wherever
GAC adsorption is employed as a treatment process. The increased coliform and
standard plate count density occurring  during  GAC  treatment place a critical
importance  on  maintaining an  effective disinfectant barrier following  GAC
filtration/adsorption.  Because  of final disinfection, finished water  bacteriologic
quality  at Beaver  Falls,  PA, was adequately maintained during the  entire  study
period,  with a total coliform density of <1 organism/100 mL and a standard plate
counl density  below 500  organisms/ mL.                                .

  Bacterial  Populations  in  Granular Activated  Carbon (GAC) Adsorbers—The
bacterial population that develops in activated carbon adsorbers (both in the sand
replacement and post-filter  mode) includes (1) a specialized group of organisms
capable of biodegrading organics adsorbed from the source water and (2)  those
bacterial survivors passing through the early stages of the water treatment  train."
Included in studies by the Philadelphia Water Department (Torresdale facility) on
activated carbon  adsorber designs  for  better  organics  removal  was  routine
monitoring for total coliforms and general bacterial populations.110 Although this
investigation is still in progress,  available data  confirm the recovery of several
coliforms,  including   Citrabacier freundii,  Enierobacter   cloacae,  Klebsiella
pneumonia,  and K. oxytoca.
  Furthermore, GAC adsorbers showed approximately a 10- to 100-fold increase in
the general bacterial populations, compared with control systems, when the influent
was ozonated. This stimulation of bacterial growth on GAC adsorbers is presumably
caused  by the oxidative  breakdown of some organics by ozone treatment, which
results in more usable  organics for bacterial metabolism. Pilot-plant studies (see
Section VII, Subsection Biologic Degradation) confirm that the number of bacteria
in the activated carbon adsorber effluent after ozonation of the  influent waters
remains significantly higher than if the influent waters were simply aerated (that is,
passed through the contact chamber unexposed to ozone). As a result, bacteria may
eventually penetrate the adsorber in  large  enough numbers  to challenge the
disinfection  barrier.
  The Philadelphia study also included examinations for Actinomycetes and fungi.
Limited available information on these  microbial contributors to taste and odor
suggest  that colonizations may occur in activated carbon adsorbers and sand filters,
but at an apparently lower density than  encountered in the source water.110
  The bacterial flora of activated carbon adsorption  and sand filter beds, the
bacterial quality of adsorber and filter effluents, and theeffects of disinfection on the
organisms colonized in a  model treatment process have been studied by Parsons.171

202  Treatment Techniques for Control/ing Trihalomethanes in Drinking Water

-------
Results of this investigation indicated that a variety of bacteria in a groundwater
source survive lime softening and colonize downstream in sand filters or activated
carbon adsorbers. The size and composition of the bacterial population within these
filters will: 1) change more with seasonal temperatures than with treatment processes
or operations of the system, 2) vary with the chemical quality of the influent water,
and 3) possibly form slime that may interfere with bed maintenance by preventing
adequate backwashing and that may slough off large numbers of organisms into the
system effluents.
  Population profiles of bacteria released from activated carbon adsorbers and sand
filters used to treat unchlorinated groundwater were investigated at Miami, FL."1*"2
Dominant organisms in the effluent from aged G AC adsorbers and sand filters were:
Pseudomonas,  Moraxella, Acinetobacter, Alcaligenes, gram positive bacilli, and
unidentified organisms.  During  the  USEPA  in-house  study, bacterial  profiles
obtained from dual-media filters receiving either nonozonated or ozonated water
revealed that the exposure to ozone caused a  more selective bacterial population to
be released in the effluent (J. Caruthers, Spelman College, personal communication
1979).  Profiles of dominant organisms present in the influent and effluent of dual-
media filters receiving ozonated and nonozonated source water are shown in Figures
111 through 113. Note that although similar types  of dominant organisms were
encountered in these studies, bacterial survivors of ozonation were greatly restricted
in species diversity. This change in bacterial flora composition in turn stimulated a
significant increase in the bacterial density of ozonated effluent. Among the recessive
strains encountered (i.e., a broad spectrum  of bacteria with  less  than 5  percent
occurrence) were a variety of pigmented organisms that became established in the
adsorbers and found their way into the effluent. Although the significance of these
organisms is uncertain, they appear frequently in drinking water and possibly may
colonize GAC adsorbers  and sand filter beds.
  A study of pigmented organisms in the activated carbon adsorbers at  Evansville,
IN, also  revealed  a periodic  colonization (D. Reasoner,  USEPA, personal
communication 1980). Both virgin GAC and  reactivated carbon adsorber effluents
contained some pigmented bacteria, even though the influent to the GAC adsorber
sometimes showed  no significant pigmented bacterial population  during  periods
when  increased concentrations of chlorine dioxide were applied to the untreated
river water (Table 74). Apparently, disinfectant residuals during May-December
1979 were inadequate to be an effective, controlling force in the GAC adsorbers. No
disinfectant  residuals were detected in these GAC adsorber effluents  because of,
specific oxidant/GAC  reactions. Analyses  during  March-April  1980, however,
showed a few pigmented bacteria in the source water and essentially none from the
GAC adsorber (these data are not included in Table 74). This change may have been
caused by a drastic seasonal decline in the occurrence of these bacteria in the source
water,  or it may have resulted from the more effective (higher dose) application of
chlorine dioxide to the  source water to  maintain a residual  of 0.3 to 0..5 mg/L
chlorine dioxide in the GAC adsorber influent.
  One  of the areas of  greatest  confusion in studying  changes  in  the bacterial
population and speciation of organisms in GAC adsorbers has been theselection of a
culture protocol (including medium, incubation, time, and temperature)  to optimize
recovery and identification of these organisms. The standard plate count procedure
(SPC agar, 35° C [95° F] incubation for 48 hours) measures that portion of the total
bacterial population related to coliform interference, opportunistic pathogens, and
effectiveness of chlorine residuals.17*'174 This procedure probably does not, however,
adequately detect either the magnitude of bacterial growth in adsorber  beds or the
full extent of regrowth within the distribution system.
  Investigation of the problem reveals the need to use a  medium with a variety of
nutrients in low concentrations, such as R-2A medium."5 Increasing the length of
the incubation  time at a lower temperature—28°C  (82°F)—further enhances the
recovery of organisms that may be present in the GAC adsorbers. Table 75 illustrates

                               Section IX. Maintaining Bacteriologic Quality  203

-------
                                          Enterobacter
                                           agglomerans
                             Acinetobacter Iwoffi
                                    60%
         Figure 111.  Prof Me of dominant organisms present in influent of
                      a dual-media filter receiving nonozonated source
                      water. {Average specific plate count of 5,500 orga-
                      nisms/mL).
                                                    Enterobacter
                                                       agglomerans
         Figure 112,  Profile of dominant organisms present in effluent of
                      a dual-media filter receiving nonozonated source
                      water. (Average specific plate count of 3,900orga-
                      nisms/mL.)
204  Treatment Techniques for Controlling Trihatomethanes in Drinking Water

-------
                             Alcaligenes Species
                                    70%
         Figure 113.  Prof He of dominant organisms present in effluent of
                     a  dual-media  filter  receiving ozonated source
                     water. (Average specific plate cou nt of 36,000 orga-
                     nisms/mL.)
 TABLE 74. PERCENT OCCURRENCE OF PIGMENTED BACTERIA IN
                    GAC FILTER EFFLUENTS FROM
        CHLORINE-DIOXIDE-TREATED OHIO RIVER WATERM
Coagulated, settled. Virgin
activated Reactivated
filtered water carbon effluent carbon effluent
Sample
date
(1979J
May 15
May 29
June 12
June 26
July 10
July 24
Oct 9
Oct23
Nov22
Dec 4
CIO,
residual.
mg/L
0.3
0.1
0.2
1.O
0.5
0.6
0,3
0.2
0,6
0.5
Percent CIO,
pigmented residual.
bacteria mg/L
94 <0.1
68 <0.1
90 <0.1
27 <0.1
None 
-------
KJ
§
^
It!
0)
I
       TABLE 75. BACTERIAL POPULATIONS IN WATER TREATMENT PROCESSES USING STANDARD PLATE COUNT
                         MEDIUM OR R-2A MEDIUM WITH EXTENDED INCUBATION TIMES*'1"
•hniques for C
1
o
3*
«a
5*
3s
8>
S"
a

3-
a
3'




Source water
Sampling
day
Initial
7
14
21
28
35
42
49
56
63
SPC.t
2 days$
110
<1
4
<1
<1
<1
10
3
8
2
SPC,
6 days!
300
14
2
2
<1
2
11
11
21
25
R-2A.
6 days
470
43
13
43
28
10
3
15
84
200



Lime-softened water
SPC,
2 days
120
31
7
7
3
<1
70
9
<1
29
SPC,
6 days
350
202
7
18
39
490
120
1,200
10
190
R-2A,
6 days
510
510
130
150
530
330
1,700
23
<1
3,000



Sand filter effluent
SPC,
2 days
890
820
<1
2,200
700
100
1,200
5,000

170
SPC,
6 days
1,200
22,000
1,200
2,500
7,800
6,000
71,000
41 ,000
700
2,000
R-2A,
6 days
1,500
35,000
9,400
33,000
67,000
25,000
22,700
3,000
12,000
3,000



GAC adsorber effluent
SPC,
2 days
<1
1
<1
<1
1
<1
»*
80

»*
SPC,
6 days
140
25,000
600
5,200
11,000
12,000
56,000
4,200
1,900
5,000
R-2A,
6 days
220
95,000
4,400
16,000
55.000
74,000
52,000
100
50,000
48,000
•All cultural incut*tod at 3B°'
tStandard plate count.
^Standard plat* count incubation tima*
§ Extended incubation tim«,
"Not run.

-------
recovery data for organisms found in several different stages of drinking water
treatment processes using two different media and extending the incubation time to 6
days for the standard plate count procedure.
  Accurate  location of the sites  where bacterial colonization occurs in  a GAC
adsorber and the determination of the magnitude of the bacterial population have
presented two difficult problems in analyses that may account for conflicting results
and conclusions derived from the research literature. In a  recent study,  Parsons
found that shaking exposed OAC in buffered dilution water was not adequate for
removal of adhering bacteria.172 Furthermore, grinding in a blender or tissue grinder
was also inadequate because of some cell disruption, reattachment of bacteria to a
newly created activated carbon surface, or simultaneous settling of bacterial  cells
with activated carbon particles.  Highest density recovery of bacteria from GAC
particles was obtained with sonication—20-kilohertz, 180-watt output for 4 minutes
(Table 76). Sites for intense bacterial colonization in GAC adsorbers appear to vary
with the adsorber bed age (Table 77), bacterial  species dominance, and  perhaps
approach (flow-through) velocity. Flow rate is probably critical because it affects
nutrient transport to the microorganisms on the granular particles.176 Though the
species composition of the  effluent bacteria reflected that of the bacteria established
in the activated carbon adsorber, the bacterial density near the bottom of the GAC
bed did not correlate with the bacterial density in the effluent (Table 77).  Overall,
these results suggest that bacterial growth on activated carbon particles in localized
areas may be substantial and that bacteria do appear to become established in the
lower part of an adsorber bed. Furthermore, these populations may pulse widely in
densities, because they are  a reflection of numerous variables in the adsorber column
ecosystem.
  Although  pronounced regrowth in both the filter and adsorber beds occurred,
little of this biologic activity correlated with  a  measurable removal of organics
adsorbed on the activated  carbon  over a 2-month operational period (Table 78)."'
These data were developed from a comparison of TOC removed by sand  filters and
GAC  adsorbers that received lime-softened, unchlorinated groundwater  as their
influent. No apparent correlation of TOC removal occurred with the age of the sand
filter (63 days maximum). The data do suggest, however, that TOC removal in sand
filters may be related to microbial activity, and TOC removal in GAC adsorbers of
similar age may be a function of physical-chemical adsorption.
  In a  study on filtration-adsorption, ozonation of the  influent water before
application to a dual-media filter stimulated a rapid growth of organisms on the filter
media (see Section VII, Subsection Biologic Degradation). This growth could have
been a significant factor in the removal of organic compounds through the filter.
Perhaps long-term use of  sand filter beds  might eventually produce a specialized
population of bacteria capable of some measurable degradation of organics.
  Microbial biomass concentrations were monitored at the Shreveport, LA, project
where the application of extended ozone  contact time for  filtered water passing
through several pairs of activated carbon post-filter adsorbers is being studied.1
This investigation has produced some evidence that bacteria on activated carbon
particles in these adsorbers range from 240,000 to 20 million organisms/gram of wet
activated carbon by  weight. Because bacterial standard plate counts in effluents
reflect only a small portion of the total viable  biomass established in an activated
carbon adsorber, measurements of adenosine triphosphate (ATP) concentrations (a
measure of metabolic energy in living cells) were also made to obtain a better total
indication of all viable microbial  activity.
  With the use of both standard  plate counts and ATP measurements,  data were
gathered on the source water, influent, and effluent of two GAC adsorbers  in series
without prior ozonation. Simultaneously, the same coagulated, settled, and filtered
water was ozonated at two different detention times and then applied to other GAC
adsorbers in series.  Ozone contact time was the sole difference between  the two
ozonated waters. Results of monthly sampling demonstrated  that bacterial densities

                              Section IX. Maintaining Bacteriologic Quality   207

-------
208 Treatment Techn
•5-
1
,
O
o
i.
1

§
CD
0
a
(6
3-
1
8


TABLE 76. RECOVERIES OF BACTERIA FROM SONICATED* OR HAND-SHAKEN

Minutes processed
Method 12 4 6 6 8 10
Test 1:
Sonication 700.000 940,000 980,000 430,000 680,000 370,000 240.000
Hand shaken 14,000 — — — — — —
Test 2:
Sonication 3,300.000 4.300.000 116.000,000 2,300.000 1,600.000 700.000 400,000
Hand shaken 620,000 - - — - - -

"Sonicate* acoustic *n»rgy rat«d at 20 kllohtrtz and 180 watt* maximum output.
fShaken or lonicattd in dilution water bafora plating (R2-A pour plataa Incubated at 36°C I96°F] for 1 2 days).


GAC PARTICLESf m


12 14

230,000 380,000
— —

1,100,000 100,000
— —








16

380.000
—

83,000
—




-------
   TABLE 77. BACTERIAL COUNTS* FROM TOP, MID-POINT, AND
     BOTTOM OF AN ACTIVATED CARBON BED AND FROM ITS
                              EFFLUENT72
Organisms/0. 5 g dry wtf
Column age.f
days
6
11
17
20
25

Top
§
650,000
130,000
2,790,000
7.700
GAC Motion
Mid-point
58,000
45,000
4,400,000
460,000
90,000,000

Bottom
55,000
28,000
2.700,000
320,000
50,000,000
Effluent,
counts/mL
250,000
1 35,000
30.000
44,000
520,000
"R2-A pour plates (38°C [96°F] incubation for 6 days).
t Am Want room tamparatures.
jAetlvaiBd carbon partfclas sonicated for 4 minute*.
IJNot run.

   TABLE 78. BACTERIAL DENSITY IN SYSTEM EFFLUENTS AND
                      PERCENT TOC REMOVAL"7

Bod
age.
days
0
7
14
21
28
35
42
49
56
63
Sand

Bacteria,*
No./mL
1,500
35,000
9,400
33.000
67.000
25,000
71,000
41,000
12,000
3.000
filter effluent

TOC.
mg/L
6.7
6.4
6.4
6.3
6.4
6.3
6.2
6.4
7.0
7.0
Percent
TOC
removal
0.0
7.2
1.5
5.9
1.5
3.0
10.1
13.5
6.6
6.6
GAC adsorber affluent

Bacteria,*
No./mL
220
95.000
4,400
1 6,000
55,000
74,000
56,000
100
50,000
48,000

TOC,
mg/L
0.3
1.3
2.6
2.9
2.9
2.2
2.9
4.6
4.4
4.8
Percent
TOC
removal
95.5
79.6
60.9
53.9
54.6
65.0
53.2
28.1
37.1
31.4
•R-2A medium with 3S°C {96"F) incubation for 6 dayc.
tended to increase in O AC adsorber effluents as the temperature rose (Table 79). No
positive correlation occurred between ATP concentrations and water temperature
changes. Correlation of ATP concentrations with bacterial density measured by the
standard plate count was inconclusive. This discrepancy occurred partly because of
recovery limitations, as only a portion of the total biomass is measured in the
standard plate count procedure. Furthermore, the ATP content of an average
bacterium is approximately 2.5xlO"'%ig/cell, varying among 19 species tested from
0.25 to 8.9X 10  fig/ cell. ATP activity must therefore be judged as a parameter on its
own merit and not in relation to heterotrophic bacterial density as measured by the
standard plate count of a water sample.
  Essentially no change occurred in bacterial densities  for nonozonated water
passing through two GAC adsorbers  in series. GAC influents that received prior
ozonation had fewer than 10 organisms/mL, except for one test involving extended
ozone contact time. In this sample, 1,500 organisms/mL were reported; yet the ATP
measurement  remained low, suggesting possible sample contamination during
collection. All effluents from GAC adsorber pairs receiving water that  had been

                              Section IX. Maintaining Bacteriologic Quality  209

-------
s
I
I
I
3"
I

I
            TABLE 79. MICROBIAL ACTIVITY IN GAC ADSORBERS RECEIVING NONOZONATED AND
                                           OZONATED WATER1"



6.3°C (48°F)

Stage
Source
Nonozonated water;
GAC influent
GAC affluent
Ozonated water, short
detention (3 m\n):
GAC influent
GAC effluent
Ozonated water, long
detention (40 min):
GAC influent
GAC effluent
BPC»
No./mL
*

150
160


2
190


5
90
ATPf
ng/L
886

68
50


27
77


73
150


6.9DC (44°F)
BPC
No./mL
t

1,500
1,100


<1
717


<1
490
ATP
ng/L
7.500

113
117


13
70


70
57
Seasonal
10.4°C
BPC
No./mL
*

2,800
3,700


<1
1,900


<1
1,500
water temperature intervals
(51 °F) 13.8°C(57°F)
ATP
ng/L
3,280

334
335


285
303


303
300
BPC
No./mL
t

10,000
6,000


<1
1,000


<1
3,600
ATP
ng/L
4,100

23
68


13
30


13
38
15.4°C(60°F»
BPC
No./mL
t

2,600
2,300


5
480


8
15,000
ATP
ng/L
2,520

41
49


27
50


23
68
25°C J77°F)
BPC
No./mL
t

6,100
3,100


<1
1,600


1,500
2,400
ATP
ng/L
2,680

74
52


<1
17


5
30
•Bacterial plat* count (28°C [82°F] for 7 dava on *oli •xlract «g»r|.
tAdwioiln* trfphoiphcti •> « muiura of metabolic aetMty.
(Not run.

-------
ozonated demonstrated a significant regrowth of organisms within the adsorber bed,
reaching 10- to  1,000-fold  increases over influent values. The magnitude of the
regrowth was directly related to water temperature and was more intense with warm
water.
Alternative Types of Disinfectants and Application Techniques

Chlorine-Ammonia Treatment (Combined Residual)—
  Another approach to minimizing trihalomethane production in water treatment is
to replace the free chlorine with an alternative disinfectant. Chloramines, chlorine
dioxide, ozone, and ultra-violet light have been proposed as practical alternatives.
Because of  the desire to maintain a disinfectant residual in distributed water,
chloramines and chlorine dioxide  have received  the most  attention. Although
monochloramine is definitely a less effective disinfectant than free chlorine, when
compared at comparable low-dose concentrations and short contact periods (see
Section VIII,  Subsection Biocidal  Activity) it  may be practical in many plant
operations where longer  contact times and application of high concentrations are
feasible.
  Such is the case at the Jefferson Parish Water Department, Jefferson Parish, LA,
where monochloramine has been relied fan as the sole water disinfectant for over 30
years. In a study of data collected over an  18-month period from this water treatment
plant, Brodtmann et al.  reported only two  total coliform occurrences in 6,720
samples of finished water.1  This treatment system provided a 30-minute contact
time before filtration, with 1.1 to 2,0 mg/L combined chlorine residual measured in
the gravity sand  filter effluent.  Initial processing  of the river source water with
potassium permanganate and polyelectrolyte addition lowered the standard plate
count by an average 84 percent during water clarification (Figure 114). Clarification
together with 8 to 10 minutes of monochloramine contact resulted in an average 96.1
percent reduction of the source water population of standard plate count organisms.
Continued processing with sand filtration in combination with a total combined
residual contact time of 30 minutes lowered the initial level of measured organisms
99.7 percent. The average monthly standard plate count, reported to be below 50
organisms/ ml in the distribution system, may be misleading because the problem of
regrowth is generally associated with warm water temperature conditions,  areas of
slow flow, and deadrend sections of the distribution system. The samples measured
for the monthly  average were not collected  exclusively  under  these  adverse
conditions.
  The Louisville Water  Company,  Louisville,  K.Y, was involved  in a study of
trihalomethane concentration control by three different disinfectant treatments.
Normal plant  operations used  free chlorine applied to gravity-settled source water
before the clearwell. During modified treatment, ammoniation of the free chlorine
residual was practiced at the clearwell during several weeks of data gathering.'* Later
in the year, application  of chloramines occurred following  coagulation. When
ammonia  was added  at the softening basin, it was in some excess so that further
chlorination at the clearwell would restore the chloramine residual. The net result
was that a combined chlorine residual was maintained throughout the latter stages of
treatment and into the distribution system.
  A comparison  of the bacteriologic. conditions indicates that the  application of
chlorine to the gravity-settled source water effected a complete reduction in both
total coliforms and standard plate count densities (Table 80). Densities remained low
in all  subsequent in-plant  samples. Injecting ammonia into the clearwell at the end of
the treatment train or adding ammonia in the softening basin followed by filtration
and clearwell  chlorination resulted in  no  further bacterial penetration of  the
treatment train. In all cases, the data demonstrated finished  water of acceptable
quality.

                      '       " Section IX, Maintaining Bacteriologic Quality 211

-------
    10000  —-
  E
  o
  o
  Ul
  Q
  ec
  1
     1000 — r
      100 -ztr
       10  -=r
                  I     T      I
                                             vvCoagulated And Settled Water
Disinfected Water
(Chloramines!
                                       Sand Filter Effluent
                 JAN  MAR   MAY  JUL  SEP   MOV  JAN  MAR   MAY   JUL
                 1978                                                  1979
                                    DATE OF SAMPLING
          Figure 114.  Standard plate count at various stages of water
                      treatment at the Jefferson Parish  Water Depart-
                      ment (LA)."«
Chlorine Dioxide—
   Chlorine dioxide is  another disinfectant that does not  react with precursor
 materials to form trihalomethanes during water treatment (see Section VIII). The
 Louisville Water  Company  investigated  the efficiency  of  chlorine  dioxide
 disinfection by adding 0.6 to 0.8 mg/L chlorine dioxide at the coagulation basin
 effluent and applying ammonia about  10 minutes later at the influent to the next
 treatment step, the softening basin."8 The chlorine dioxide residual in the softening
 basin effluent was usually 0.1 mg/ L or less. Disinfection after filtration resulted in a
 combined chlorine  residual  of 0.8 to 1.2 mg/L,  which  remained  unchanged
 throughout the 2-week chlorine dioxide study period. For comparison purposes, 2 to
 3 mg/ L of free chlorine was applied to the influent of the coagulation basin both
 before and after the study period, creating a contact time of approximately 6 hours
 before ammoniation.
   Monitoring the standard plate count in the treatment train during both free
 chlorine and chlorine dioxide disinfection periods revealed a 10- to 100-fold decrease
 in bacterial density between the treatment plant influent water and the coagulation
 basin effluent. Typical values in the coagulation basin effluent were 5 to  50
 organisms/mL when free chlorine was applied, and 10 to 50 organisms/mL jvhen
 chlorine dioxide was added. For some unexplained reason, one high value (1,000
 organisms/ mL) did occur in the coagulated water early in the chlorine dioxide study,
 suggesting that this marginal dose of chlorine dioxide was less effective than the
 higher dose of free chlorine at this point in the treatment train.
 212  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
TABLE 80. CHLORAMINE APPLICATION POINT STUDY USING OHIO RIVER SOURCE WATER
                 AT THE LOUISVILLE, KY, WATER COMPANY1*."*



Sample point (mean values*)


Ammoniation at clearwellt Ammoniation following coagulation!


Coagu-
Source Settled lated



03
1
5'
3
><
^
3"
3"
3'
aa
CO
5'
1
n'
O
^.
•V

M
2
Parameter water
Turbidity, ntu 19
Total coliforms/
100mL 3,200
Fecal coliforms/
100 mL 62
Standard plate count/
mL §
pH 7.3
Free Cl, residual.
mg/L §
Total Cl, residual.
mg/L §



•Band on five nmpla* ovsr e 9-day period.
tSourca water temperature, 29°C (84°F).
iSource WMar temperature, 18°C (61 °F).
§Not run.


water water
23 4.7

4,900 <1

104 §

§ <1
7.5 7.0

§ 2.6

§ 2.8
t
Chlorine







Coagu-
Softened Filtered Finished Source Settled lated Softened
water water water water water water water
3.8 0.4 0.5 16 18 4.6 2.4

<1 <1 <1 4,000 1,100 <1 <1

S S § 204 177 § §

51 9 6 § § 2.2 4
9.2 9.1 8.2 7.6 7.6 7.2 9.3

0.6 0.4 0.2 § § 1.7 §

0.7 0.6 1.4 § § 1.9 1.8
t t t
Chlorine & ammonia Chlorine Ammonia









Filtered Finished
water water
0.3 0

<1 <

§

2
9.0 8

0.1 <0

1.5 1
t
Chlorine







.2

:i

§

1
.6

.1

.9










-------
   A significant increase in the general bacterial population did, however, occur in
 the filtered water during chlorine dioxide treatment. Standard plate count values in
 the filtered water were often 10 to 100 times the density observed in the coagulation
 basin effluent, indicating that bacterial regrowth was occurring in the filter bed. The
 higher bacterial densities  released from the filter bed during the chlorine dioxide
 experiment are shown in  Figure 115.  This  bacterial  intrusion was, however,
 suppressed by the last treatment barrier, a secondary addition of chloramines before
 the clearwell. Thus the finished water quality was satisfactory.
   Although concentrations of coliform bacteria were usually controlled to less than
 1/100 mL upon application  of either free  chlorine or chlorine dioxide  at  the
 coagulation  basin  effluent, some significant exceptions during treatment with
 chlorine dioxide did occur (Figure  116). In particular, 2 to 4 coliforms/100 mL were
 found in the softened and filtered  water, both during and after the use of chlorine
 dioxide. Perhaps  this result  could  be attributed to the decreased disinfectant
 residuals in the softening basin  effluent  and the filtered water (only 0.1 mg/L of
 chlorine dioxide or less). No coliforms were observed, however, in any samples of the
 finished  water before, during, or after the 2-week  investigation involving chlorine
 dioxide and ammoniation.
   The Western Pennsylvania Water Company, Hays Mine Plant, presented another
 opportunity  to study the alternative use of chlorine  dioxide as the primary
 disinfectant during a project managed by the Ohio River Vailey Water Sanitation
 Commission." For this investigation, the  routine  practice was  source water
 chlorination, potassium permanganate  treatment,  coagulation,  settling, GAC
 filtration/adsorption, and  free chlorine  application  in the clearwell. Later, the
 treatment train was modified to inject chlorine dioxide and potassium permanganate
 into the  source water entering the coagulation basin,  with free chlorine used as a
 secondary disinfectant in the clearwell before distribution. Chlorine dioxide dosage
 to the source water was 1.5 mg/L  and contained less than 0.1 mg/L of chlorine.
   Bacteriologic data presented in Table 81 (page 217) indicate that 1.5 mg/ L of chlorine
 dioxide was less effective as a source water disinfectant than was 2.6 mg/ L chlorine.
 During source  water chlorination, mean total coliform and standard plate count
 densities in the activated carbon/ filter adsorber influent were 1/100 mL and SO/ mL,
 respectively. When chlorine dioxide was the applied disinfectant before coagulation
 and  settling, a disinfectant  residual could not be maintained. As a result, mean
 bacterial densities reaching the activated carbon filter/adsorber were 43 total
 coliforms/100 mL and 7,100 standard plate count organisms/ mL. In-plant survivors
 of the total coliform population passed through the 2-1/2-year-old Filtrasorb® 400
 GAC filter/adsorber essentially unchanged in density.  In both treatment trains, the
 secondary application of chlorine in the clearwell was, however, an effective barrier
 to detectable coliform penetration  into the distribution system.
  These  data indicate that 1.5  mg/ L of chlorine dioxide evidently was not equal to
 the disinfection effectiveness  of free chlorine  during source water disinfection.
 Increasing the dose of chlorine dioxide was  not economically feasible and might
 exceed the limit  of 0.5 mg/L residual chlorine dioxide,  chlorite, and chlorate
 recommended by the USEPA.3
  In the next modification evaluated at this water plant, the chlorine dioxide feed to
the source water was lowered to 1.0 mg/ L, and source water chlorination (1.2 mg/ L)
was  also practiced.  Source water ammonia concentrations  during this period
were unusually high, averaging 0.6 mg/ L.
   Bacteriologic data presented  in Table  82 (page 218) indicate that source water disin-
 fection with a lower concentration of both disinfectants was effective in reducing the
 bacterial densities in the GAC filter/adsorber influent, but some regrowth of total
coliforms and the standard plate count organisms did occur in the filter/adsorber
and  appeared in the effluent. With  the  application of chlorine at the clearwell,
however, the finished water did meet the bacteriologic standard for total coliforms,
and a low mean standard plate count of 8  organisms/ mL was present.

214   Treatment Techniques for Controlling Trihalomethanes in Drinking Wdter

-------
     1000
                MARCH
APRIL
1979
MAY
                                                  CIO,
          I                                    I          I                 I
          U	2-3 mg/L Free Chlorine	*4*- 0.6-0.7-*f*-Free Chlorine—H
          '                                        mg/L-  '                 '
                 DATE OF SAMPLING AND TREATMENT EMPLOYED

          Figure 115.  Standard  plate counts for periods of disinfection
                      with free chlorine and chlorine dioxide at the Louis-
                      ville Water Company (KY).1'8 (Adapted from JOUR-
                      NAL American Water Works Association, Volume
                      73, No, 2 [February 1981) by permission. Copyright
                      1981.  the American Water Works Association.)

   At Evansville, IN, a Micro-Floe Water Boy®* pilot water treatment unit was used
to study chlorine dioxide as an alternative to chlorinatton as routinely applied by the
treatment plant,63 Basically, the pilot plant treatment consisted  of disinfection and
alum and polymer addition to the source water. This chemically treated water was
mixed, flocculated, and then clarified in a tube settler. Clarified water then passed
through  a mixed-media filter and onto  two GAC post-filter adsorbers before
reaching a clearwell. In an effort to simulate a dead-end in a distribution system, an
iron pipe 10 cm (4 in) in diameter and 11 m (36 ft) long was connected to the end of
the pilot plant.
'Manufactured fay Neptune Micro Floe. Corvallis. OR 97330
                               Section IX. Maintaining Bacteriologic Quality 21S

-------

_]
8
N.
d
CC
O
u
o
o
2
g



a
6-
Coagulated 4 -
2-
0
8-
6-
Soflened 4.
2-
0
B-
Filtered 6"
4 -
2-
0
8-
6 -
Clearwell ,
4 -
2 -
O
I ' I
I
: A A




_
:
LA^M-AjU
—

A A



—
W* r\ A^
-
_
-
MARCH ' APRIL MAY
1979
                                 • Free Chlorine -
                                                       1  NH2C1  '  Chlorine

                     DATE OF SAMPLING AND TREATMENT EMPLOYED
         Figure 116.  Total coliform density for in-plant processes during
                      periods of free chlorine and chlorine dioxide disin-
                      fection at the Louisville  Water Company (KY).178
                      (Adapted from JOURNAL American Water Works
                      Association, Volume 73, No, 2 [February 1981] by
                      permission. Copyright 1981, the American Water
                      Works Association.)

  The full-scale water treatment plant at Evansville, IN,  involves source water
chlorination (6.6 mg/ L), coagulation and settling, pH adjustment, and rapid sand
filtration. Booster chlorination is used ahead of the clearwell only during periods
when the chlorine  residual falls below 1.0 mg/L as the water enters the distribution
system. Because of the similarity of preliminary data obtained from both the full-
scale treatment and pilot plants during parallel studies with identical chlorination
applications, the full-scale treatment  plant was viewed  as a suitable control for
disinfection effectiveness.
  A study of data  collected from three runs over an 11-month period revealed that
chlorine dioxide treatment of the source water was effective in reducing the total
coliform and standard plate count populations, but not always to the level observed
with chlorination of the same water in the full-scale operation (Table 83, page 219).
Because chlorine dioxide was not present in the OAC post-filter adsorber effluent, a
booster application of chlorine dioxide was applied to the clearwell influent. This
secondary  disinfectant application to achieve  a chlorine dioxide residual  was
effective in  producing a finished water  of essentially the same  high quality as
obtained in  the full-scale plant operation.
  Regrowth of standard plate count organisms occurred in the  GAC  adsorbers
during warm-water conditions and was more pronounced  in virgin activated carbon
(Adsorber #1) than in reactivated carbon (Adsorber #2). Although the total coliform
count did not increase in the reactivated carbon adsorbers during the warm period,

2/6  Treatment Techniques for Controlling Trihalamethanes in Drinking Water

-------
      TABLE 81. CHLORINE DIOXIDE APPLICATION STUDY USIN6 MONONGAHELA RIVER SOURCE WATER
                             AT THE WESTERN PENNSYLVANIA WATER COMPANY'*
Sample point (mean values*)
Cl] application to source waterf






ft?
«
S
a
3'
S
1

CO
01
o
S'
1"
«'
U


Parameter
Flow time, hr
Turbidity, ntu
Total coliforms/
lOOmL
Standard plate
count/ mL
PH
Free Cl, residual.
mg/L
CIO, residual.
mg/L
Total Cla residual.
mg/L


Source
water
0
51

21,000

§
7.2

§

§

§


Plant
influent
0,6
39

4

490
7.1

0.4

§

0,8
t
Coagu-
lated
water
3.75
6.7

1

200
7.3

<0.1

§

0,4


Settled
water
12.5
8.5

1

50
7.1

<0.1

§

0.3

Chlorine,


2.6

mg/L





GAC-
filtered
water
13,6
0.6

8

160
7.2

<0.2

S

0.2


FinMiad
water
14.75
0.2

<1

3
7.1

0.6

§

0.8
t

Source
water
0
6.8

14,000

I
7.1

§

§

§

Chlorine,
1.1

mg/L



CIO, application to source water}

Plant
influent
0,6
6.2

4,200

29,000
7.1

**

#»

§

Coagu-
lated
water
3.75
6.3

100

4,790
7.5


-------
TABLE 82. STUDY OF CHLORINE DIOXIDE APPLICATION TO SOURCE
  WATER WITH BACKGROUND AMMONIA USING MONONGAHELA
 RIVER SOURCE WATER AT THE WESTERN PENNSYLVANIA WATER
                              COMPANY"
Parameter
Flaw time, hr
Turbidity, ntu
Sample point (mean values*)
Source Plant Coagulated Settled GAC-filterad Finished
water influent water water water water
0 0.5 3.75 12.5 13.6 14.76
12 7.9 6.2 2.7 0.1 0.1
Total coliforms/
  lOOmL            14,000  2,000     <1       <1         2        <1
Standard plate count/
  mL                     t  5,900      66      33       440          8
pH                     7.1    7.1     7.2      7.7       7.0        6.9
Free Cl* residual.
mg/L
;iOj residual,
mg/L
fatal Cl] residual,
mg/L
§ <0.1
t t
t 0.8
t
Clr application,
1.2 mg/L
1.1 0.9
t
CIO] application
1.0 mg/L
J 0.1
<0.1 0.7
t
Cl, application,
1.1 mg/L
 •Bind on 4 umplM over *-d«y period; source w*Mr t«mp«r»tur», Z5°C (77°F).
 tNot run.
 JNot d*MCt*d,

 they did persist at low levels. Loss of a chlorine dioxide residual through the latter
 stages of treatment also contributed to further bacterial penetration in the treatment
 train during this warm-water period.

 Instantaneous Disinfection-
  Maintaining a free chlorine residual for only a short time period is an effective
 method of reducing the formation of trihalomethanes (see Section VIII). To achieve
 adequate disinfection during such a short contact period requires high-intensity,
 instantaneous mixing of chlorine with every portion of the water being treated. A
 research  project is under way to test the applicability of this approach at the
 University  of Texas  at San Antonio.13*  In  this investigation, disinfectant is
 introduced by means of high energy in-line mixing (G = about 40,000 sec"1) to a410-
 m'/day (75-gpm) flow stream. After 16 seconds of contact time, the water passes
 through a second high energy (G = about 40,000 sec"') in-line mixer. Flow continues
 in a pipe loop for 55 seconds to provide short but precisely known contact times.
 Longer contact times for disinfection or trihalomethane formation are obtained by
 collecting samples of water discharged from the pipe loop and holding them for the
 desired time period.
  In these experiments, coliform bacteria were fed into the undisinfected, filtered
 water as it was pumped from a holding tank into the disinfection system.  The total
 coliform  data (Table 84) indicate that  effective  disinfection  could be  achieved
 without  producing  high concentrations of trihalomethanes  when  the rapid,
 high-energy,  plug-flow mixing system was used.  Addition of ammonia after 16
seconds eliminated the free chlorine residual, thereby limiting the trihalomethane
 formation (see  Table 52 in  Section VIII). Because of the very efficient mixing
attained in this system, most of the coliform inactivation occurred within 15 seconds

218   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
§:
5«

I
5'
*


I
                          TABLE 83. PILOT PLANT EVALUATION OF CHLORINE DIOXIDE USED AS AN

                                                 ALTERNATIVE DISINFECTANT83
Test run No. 1*
Treatment stage
Pilot plant (CIO,
applied to source water): -
Ohio River intake
Settled water
Mixed media effluent
(GAC influent)
GAC No. 1, effluent
GAC No. 2, effluent
Clearwell
Simulated dead end
Full-scale plant (source water
chlorination):
Ohio River intake
Settled effluent
Clearwell influent
SPC**/
mL


8.000
92

77
760
390
2.6
19,000


8,800
13
<1.0
Total coliforms/
100 mL


32,000
<1.0

1.0
<1,0
1.3
<1.0
<1.0


32,000
<1.0
<1.0
Teat
run No. 2f
SPC/ Total coliforms/
mL 100 mL


6,300
110

76
6,200
330
7.9
7,100


6,300
10.9
1.8


18,000
<1.0

1.9
1.6
<1.0
<1.0
<1.0


18,000
<1.0
<1.0
Test run No. 3f
SPC/ Total coliforms/
mL 100 mL


1,700 2,900
94 <1.0

1 .4 <1 .0
16 <1.0
12 <1.0
1.6 <1.0
6,300 <1.0


1,700 2,900
6.2 <1.0
1 .0 <1 .0
o
§
•April 23 to July 27, 1979; totnl Mmplu per tit* = 86; lourca water t»mp«»tut», 22°C (72°F).

tS*pl, 17 to OK. 11,1979; tettl Mmplu per ilt« = S2; fount 
-------
ta
i
*
3
I
•8"
s
o
3-
8
8"
a
n
 "


o
                  TABLE 84. EFFECTIVENESS OF DISINFECTION IN A HIGH-INTENSITY MIXING SYSTEM13*
Ditinfection system
Dose,
mg/L
0.6
0.6
0.5
O.S
1.5
1.8
1.5
6.0
B.O
i.O
Agent(s)
Chlorine
Chlorine + ammoniat
Ammonia •*• chlorinet
Chlorine dioxide
Chlorine
Chlorine + ammoniat
Ammonia + chlorine!
Chlorine
Chlorine + ammoniat
Ammonia + chlorine!

PH
t
7.7
t
t
7.7
7.6
t
7.8
7.9
t
Control
No./100mL»
8,900,000
170,000
11,000,000
12,000,000
15,000,000
280,000
8,200,000
11,000,000
5,800,000
6,000,000
Total coliforms
Surviving organismt/100 mL
16 tec
<30
<30
87.000
<30
<30
t
7,000,000
<30
<30
50,000
56 toe
<30
t
15,000
<30
<30
<30
<30
<30
<30
<30
15 min
<30
<30
<30
<30
<30
t
<30
t
<30
<30
60 mln
<30
<30
<30
<30
<30
t
<30
t
<30
<30
                 "Standard plata count.
                 fNot run.
                 t Ammonia doae In mg/L aquai to cWorioa dOM In mg/L.

-------
and before ammonia was added. Disinfecting action during this brief time period
was less effective, however, when ammonia was added first and followed by chlorine
15 seconds later.
  High-intensity, rapid disinfectant mixing was less effective for inactivating the
standard plate count organisms to the same order of magnitude. This weaker
response to controlling a wide spectrum of organisms may affect the selective nature
of surviving organisms released into the distribution system, their ability to become
established in the distribution network, and the need  for longer contact times or
higher concentrations of chloramines  in treatment  and distribution.  Further
investigations of this treatment concept should be made in field studies of water
systems in different geographical areas.
  An unpublished study by the North Jersey Water Supply Commission did present
one field opportunity to study the concept of short-term mixing of free chlorine. This
water supply district maintains twin, cement-lined  steel mains, 1.9 m (74  in) in
diameter, from the Wanaque Reservoir to the Little Falls treatment plant. Following
chlorination, lime is added for pH adjustment, and the water is then transmitted to
the consumer. A filtration plant is being built but is not yet operational. The use of
twin transmission lines created the opportunity to add ammonia to one of the lines.
The  time between injection of chlorine and sufficient ammonia to  convert free
chlorine to chloramines was estimated at less than 1 minute. The flow in each line was
great enough to provide intense mixing.
  As a measure of disinfectant efficiency,  standard  plate counts were determined
after 1 minute of contact time and following the 6-hour flow In both transmission
lines. Inspection of the winter data (I-4°C [34-39°F]) revealed  no significant
difference in residual bacterial densities after exposure to short-term  mixing with
free chlorine and after 6 hours of contact time with or without ammoniation (Table
85), Apparently, maximum disinfection effectiveness was provided instantaneously
because of the intense mixing; no significant further reductions were achieved by
extending contact time with either type of disinfectant residual, Coliforms/100 mL
were detected neither in water leaving the high-intensity mixing location nor in the
transmission lines after 6 hours of contact time. During the following summer, both
types of high-intensity disinfection were again studied bacteriologically, and the data
indicated an even more effective reduction (10-fold) in the standard  plate count.
Again, no coliforms/100 mL were detected after 1-minute contact  or following 6
hours flow in both transmission lines. Finally, the addition of ammonia prevented
the  formation of trihalomethanes (see  Section  VIII, Subsection,  Formation of
Trihalomethanes).


Impact on  Distributed Water Quality

  The data presented in the previous subsection relate to the bacteriologic quality of
finished water. Modifications in treatment train processes to reduce trihalomethane
production may ultimately change the character of the bacterial populations passing
through the distribution system. These quality changes may be of immediate concern
if the last barrier to bacterial passage into the finished water is interrupted, if changes
occur seasonally with increased water temperature or slowly with time as habitats
develop and the microflora adjust to changes in  this water environment.
  In the Louisville Water Company study of chlorine dioxide as an alternative
disinfectant, bacteriologic data from the distribution system were reviewed for any
significant changes.178 Data points in Figure 117 represent theaverage values for8 to
12 daily distribution system samples collected over 29 days before the use of chlorine
dioxide treatment, 10 days during the treatment modification, and for 5 days after
routine  chlorination  was  restored. Standard  plate count  densities  averaged
approximately 83, 87, and 65 organisms/mL before, during, and after disinfection
with chlorine dioxide, respectively, suggesting that a slight lowering of the bacterial
population  occurred  during  treatment  modification.   Because   the  treatment

                              Section IX. Maintaining Bacteriologic Quality 221

-------
TABLE 8E. FIILD STUDY OF HIGH-INTENSITY MIXING OF CHLORINi»

                                  Standard plata count. No./ml
Data Temperature
1979
Jan 10
Jan 19
Jan 26
Jan 30
Fab 6
Fab 14
Fab 20
Fab 26
°C
4
2
2
2
2
1
1
1
Chlorination station,!
contact time, <1 min
Little Falls plant, f
contact time, 6 hr
°F Combined Cla§ Froe CI2$ Combined Cl,§ *
39
36
36
36
36
34
34
34
23
26
28
66
64
38
#
a
24
11
32
46
49
36
#
#
26
#
23
38
41
26
28
27
' Free Cl,t#tt
16
#
. 16
43
47
27
31
22
 •Source Unpubilihid diu from North «l*rs«y D!«trict Witor Supply Commlnlon.
 tpH rung*. 8,5 to 9.1.
 1CI dot* > 2,2 to 2,4 mg/L.
 iCI d«»* * 1.2 to 2.4 mg/U NH, dots = 0.3 to 0.65 mg/L.
 "Frn midtinl Cl, » <0.1 mg/l; taul railduti Cl, = 0.9 to 1.2 mg/L.
 11Fr»» nilduil Cl, * 0.0 to 1.0 mg/L* total raslduil Cl, = 0.8 to 1.0 mg/L.
 KNot run.

modification  period  was only 17 days,  no long-term effects on distribution water
quality could be determined, but the initial results were encouraging.
  The Cincinnati Water Works stopped chlorination of the Ohio River source water
and began chlorinating at the influent to the treatment plant on July 14,1975, as an
initial  step  in changing  the  in-plant water treatment  process to  control
trihnlomethanes  (see   Section  VII,  Subsection  Cincinnati,  OH,  Results).
Chlorination  at the clearwell was used to inactivate any residual coliform population
that might have penetrated other processes in the treatment chain.  With careful
control of chlorine dose, point of application, and water pH, a significant decrease in
trihalomethane concentration  was realized  (see Figure 63 in  Section VII). The
impact that this treatment modification might have on the  bacteriologic quality of
drinking water at the distribution system dead-ends and other slow-flow sections in
the distribution network was determined from an intensive 2-year study.'79
  With the  cooperation  of  the Cincinnati Water  Works Water  Distribution
Maintenance Section, samples from 32 dead-end water mains were examined on a
rotating basis of eight sites per week. These sites are among a number of troublesome
dead-end water mains that are flushed out each week to clear accumulated sediments
and  bring fresher waters with free chlorine residuals  into these distribution lines.
Samples from these flushes were iced immediately and processed within 5 hours of
collection. Analyses of 613 water samples over the 2-year period included a 10-tube,
three-dilution total coliform most probable number (MPN) and a standard plate
count  incubated  at 35°C (95°F) for  48  hours. Physical/chemical parameters
measured were free chlorine residual, turbidity,  water temperature, and pH. Results
for an 18-month portion of the study that included 8 months of data before the
treatment modification are given in Figure  118.
  Changes in water quality in the distribution system were not observed immediately
on the day of the  treatment change. Approximately  15 days passed before some
decrease in free chlorine residual concentrations, turbidity, and pH occurred. Before
the change in the point of disinfection application, increased chlorine residuals were
inconsistent in  limiting some coliform occurrences, probably because of sediment
accumulations that resulted in an average turbidity of 20.7 ntu in these dead-end
sections (see  Figure 118). The most extreme example occurred during one  week in
December 1974, when the total coliform density averaged 138 organisms/100 mL in
the eight samples collected from selected dead-end flushings. Once  the turbidity

222   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                        1000
to

I
?<
I
3"
£
§"
Co
D
S
                     E
                     x
                     d
                     Z
                     O
                     O
                     LU
                     o
                     K
                     <
                     O
                     I
                     CO

                     1
                         100
10 --
                                                                  I        I       III       I
                             3/1
                                    3/7
                                           3/14
                                                   3/21    3/25
                                                                 4/4
                                                                         4/11
                                                                                4/15
                                                                                        4/25
                                                                                                S/2
                                                                                                       5/9
                                                1 Routine Chlorinatton •
                                                                                        - CIO,,Chloramines
                                                                                                              5/16   S/23
                                                                                 Restoration of  i
                                                                                   Routine   »l
                                                                                 Chlorination
                          DATE OF SAMPLING AND TREATMENT EMPLOYED
                Figure 117.  Standard plate count for distributed water before,
                             during, and after disinfection with chlorine dioxide
                             at the Louisville Water Company (KY). Data points
                             represent averages of 8 to  12 daily distribution
                             system  samples.'™  (Adapted  from  JOURNAL
                             American Water Works Association, Volume 73,
                             No.  2 [February 1981] by permission.  Copyright
                             1981, the American Water Works Association.

-------
        1000
13
O
U
UJ
s
a.
a
cc
g
     -

     8
     cc
     O
     8
         100
    z>
    a
    e7>
    ui
    cc
    UI
    z
    cc
    3
          10
                  1975
                   Av. Turbidity 20,7 ntu
                                 July 14
                                  1975
         1976

Av, Turbidity 10.1 ntu
                      Source Water
                Chlori nation. Pt A, Figure 62
                                         Chlorination after off-stream
                                           Storage, Pt B, Figure 62
                  DATE OF SAMPLING AND TREATMENT EMPLOYED

          Figure 118.  Bacteriologic quality of water in dead ends of the
                       Cincinnati, Ohio, distribution system after changes
                       in point of .chlorine application,

decreased to an average  of 10.1 ntu, this interference with disinfection was not
apparent. Why the turbidity in the dead-ends was reduced following the treatment
change is not  known; the protocol and  frequency of main flushing  remained
unchanged. Perhaps this reduction in turbidity was a result of more water  flow with
increased tap-ins from residential developments or it may have been a result of more
stable  scale formation  on the pipe walls (pH shifted from 8.0 to 7.8) following
treatment modifications.
  After the point of chlorination was moved, a free chlorine residual concentration
of at least 0.2 mg/ L was effective in controlling coliform occurrences in the dead-end
sections  of the distribution network (Figure 118).  When free chlorine residual
concentrations declined to O.I mg/L or less, however, coliforms in protected pipe
224  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
habitats reached the sampling sites in a viable state and were detected in densities as
great as  10 organisms/100 mL. During warm-water  periods, when free chlorine
residual concentrations occasionally declined to 0,1 mg/L or less, some coliform
regrowth occurred, with densities ranging from 12 to 30 organisms/ 100 mL. Water
temperatures during these periods of low free  chlorine residual  concentrations
ranged from 20 to 25°C (68 to 77°F). Finally, sudden increases in standard  plate
count densities often occurred a few days to a week in advance of the appearance of
coliforms in these waters. Standard  plate counts would thus serve as an early signal
of undesirable quality changes occurring in water distribution systems or during a
loss of disinfection effectiveness.
Disinfectant Stability during Water Distribution

  Stability of disinfectants during water supply distribution is important for a
number of purposes, particularly to prevent colonization of surviving organisms and
protection from the intrusion of contamination in the pipe network. Microbial
colonization  may lead to corrosive effects on the distribution system and aesthetic
effects such as taste, odor, and appearance. Regrowth of potential health-related
opportunistic organisms and  their impact on coliform detection should not be
dismissed as a trivial problem. Further, the maintenance of a biocidal residual to the
consumer's tap keeps the system clean and protects against some cross-connection
contamination, and its sudden disappearance is a rapid indication of distribution
system problems. While maintenance of a disinfectant residual in the distribution
system  will not stop massive levels of external gross contamination  that are
detectable through  odors, color, and milky turbidities,  it may quickly inactivate
pathogens in the more frequent cases associated with contaminants seeping  into
large volumes of high-quality potable water,180
  Distribution system problems associated with the use  of combined  chlorine
residual or no residual have been documented in several instances."MSJ In these
cases, the use of combined chlorine is characterized by an initial satisfactory phase in
which chloramine  residuals are easily maintained throughout the system  and
bacterial counts are very low. Over a period of years, however,  problems may
develop, including  increased bacterial counts,  dropoff of chloramine residuals,
increased taste and odor complaints, and reduced main carrying capacity. Therefore,
as  noted later,  increased  monitoring  is  recommended  if this  technique of
trihalomethane control is practiced.
Discussion

  Drinking water treatment modifications to reduce trihalomethane precursors and
thus control  trihalomethane  concentrations must be cautiously applied. Careful
consideration must be given to the changes such alterations may introduce in the
bacteriologic quality  of drinking water produced in the plant and transmitted
through the distribution network. Not all source waters are of uniform bacteriologic
quality; thus  adequate treatment barriers must be maintained at all times to meet
changing  water qualities. In ail field studies  reported  in this  volume, no overt
evidence was found to indicate the bacteriologic deterioration in the finished water
leaving the  treatment   plant.  In  the trade-off  to decrease  trihalomethane
concentrations  by  delaying  disinfection, however,  some  critical reductions  of
bacterial population later in the treatment train must be accepted. Greater reliance
must   therefore be placed  on  effective, continuous  final  disinfection,  with
maintenance  of a  disinfectant  residual in the  distribution system  to counter
effectively the residual coliform populations and associated pathogens that have
survived earlier stages of water treatment.

                               Sect/on IX. Maintaining Bacteriologic Quality  225

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Monitoring during Heavy Pollution Loads—
  Bacterial penetration of the  multiple barriers in the drinking water treatment
process is more pronounced during abnormal pollution loads in the source water.
Under these circumstances, expected bacterial decreases during the early phases of
the treatment chain will not adequately suppress the residual bacterial population.
This  condition  places  a  greater  burden  on  the  last in-plant  treatment
barrier—disinfection. A daily bacteriologic monitoring of all in-plant processes is
therefore  recommended  during periods of abnormal increases  in source water
pollution (determined from baseline monitoring data) to evaluate the transport and
fate of the total coliform and general bacterial population through the treatment
chain.

Monitoring Systems  with GAC Adsorbers-
  Treatment   systems  incorporating  GAC  adsorbers present  some  unique
bacteriologic monitoring problems. Substantial bacterial growth in GAC adsorbers
can  occur, the flora being a  reflection of source water  organisms (including
coliforms) that survive early treatment processes. Changes in organism dominance
occur partly because of habitat site selection, competition with other members of the
bacterial flora, and available nutrients adsorbed  onto activated carbon particles.

  Ozonailon—Ozonation of influent waters before they pass through activated GAC
adsorbers has three effects:  1)  It provides  more nutrients for microorganisms  by
making some organic compounds more biodegradable;  2) it restricts the  number
and kinds of organisms reaching the adsorber bed, and 3) it accelerates the growth of
survivors  by  inactivating  bacterial  antagonists and  competitors for available
nutrients. The net result can be the release of substantial numbers of bacteria (many
of which may be selectively resistant to disinfection) into the GACadsorber effluent.

  CAC Adsorption  without Prior Disinfection—In  water plant modifications
involving GAC adsorption without prior disinfection,  coliform survivors  may
become established  in  the GAC  bed under warm ambient  temperatures  and
ultimately migrate into the adsorber effluent. Because of the potential problem of
coliform regrowth and release of a  highly specialized bacterial population from the
GAC adsorber, bacteriologic monitoring of the adsorber effluent is recommended as
part  of  in-plant quality   assurance,  especially  during  periods  when water
temperatures  rise above 12°C(54°F). Such monitoring data would serve as  an early
warning of bacterial penetration of the treatment train. The operator could then
evaluate the need for  backwashing the adsorbers to reduce bacterial buildup and the
need for increasing the dose of disinfectant in the final treatment process.

  Concepts for Measuring  Bacterial Populations—If bacterial densities in GAC
adsorbers are to be adequately characterized, traditional concepts for measuring the
general bacterial population must be revised.  These  organisms  are not easily
cultivated, either on standard plate count agar or at 35° C (95° F), Thus consideration
should be given to optimizing their  detection by using 28°C (82° F) incubation for 7
days. Furthermore, a medium such  as R-2A agar or soil extract agar is desirable for
recovery of a broad spectrum of this specialized  population.


Bacteriological Quality of Finished and Distributed Water—
  Although field studies have demonstrated that the treatment modifications
recommended in this volume will not adversely affect the bacteriologic quality of
finished water, they  will result  in a lowered bacterial  barrier,  particularly during
warm-water periods  or  during the occurrence of gross  deteriorations in  the
bacteriologic  quality of source waters. For this reason, final  application  of a
disinfectant and  establishment of a disinfectant residual become the critical


226  Treatment Techniques for Controlling  Trihalomethanes in Drinking Water

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treatment barriers  that  must be  maintained continuously ,in a  high state of
effectiveness. Continuous monitoring for a disinfectant residual is recommended for
these modified treatment systems, and these measurements should be supported by
daily turbidity  and bacteriologic measurements to assure  proof of disinfection
effectiveness.
  In systems using GAC adsorbers, the bacteriologic quality of finished water
during warm-water periods should  be determined (every 4 to 6 hours) whenever a
sudden turbidity change occurs in the GAC adsorber effluent to ensure that high
densities of  bacteria in GAC adsorber effluents do not penetrate the disinfection
barrier. Ideally, an automated, programmable sampling  device  that  includes
provision  to perform the rapid (?-hr) fecal coliform measurement  or an ATP
measurement would be desirable to maintain a closer vigil for early evidence of
bacterial penetration of the treatment barrier.
  Long-term bacteriologic effects of treatment  modifications will most  likely be
observed first in the slow-flow and dead-end sections of the distribution network.
These locations are also the sites where new waterborne organisms passing through
treatment frequently establish their initial habitats in the accumulated sediments.
When  treatment  modifications  are proposed,  gathering baseline  data at these
locations over a 6-month period and continuing this monitoring for at least 1 year
following  in-plant  modifications  would be desirable.  In  monitoring in-plant
treatment changes for trihalomethane control, slow-flow and dead-end sections in
the distribution system should be monitored weekly during warm-weather periods
(when  temperatures are above 12°C [54°F]) for both total coliforms and standard
plate count. Sampling of dead-end sections should be done on a weekly basis;
rotating site  locations to include all major dead ends in the network during the warm
season. Reliance on sample collections made from the main flow in the distribution
system is misleading because of high disinfectant residuals. These samples may give
no immediate indication of subtle changes beginning to occur at more remote sites in
the  network that relate  to  ineffective disinfectant residuals and  intermittent
penetration  of the treatment barrier.
                              Section IX. Maintaining Bacteriologic Quality  227

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                               SECTION X
                         TREATMENT COSTS
Background
   Treatment costs are concerned with analyzing the unit process costs associated
with  the various technologies  that could  be most efficiently used to meet  the
trihalomethane  MCLJ using each of three possible approaches.  Not every unit
process is equally efficient in accomplishing the goals of meeting the MCL: Some are
much more efficient in removing trihalomethanes after formation, some remove
trihalomethane  precursors most efficiently, and  several alternative disinfectants
other than free chlorine are available.
   This section is designed to assist the utility manager, the consultant, the Primacy
Agency, and others in achieving economical, feasible strategies for meeting the THM
Regulation.* To combine process efficacy  and cost in  selecting appropriate unit
processes, use this section along with others in this book; the presentation is su«h
that processes can be selected  on comparative costs for equivalent performance
basis.
   An attempt has been made to identify variables such as reactivation frequency and
chemical dose, and the sensitivity of alternative strategies to these design criteria
variables has been taken into account. The  figures presented herein can be used in
conjunction with pilot testing to evaluate costs  for a wide range of alternatives.
Although the costs are based on 37,800 m'/day  and 378,000 m /day (10 and  100
mgd) for the most part, Figure 119 can be used to estimate economies of scale that
might result from size differentials. Twenty years, rather than the normal 30 to 40
years, was selected as the amortization period forthe unit processes considered. This
was done to be conservative and to reflect the use of new or relatively untried
technology and to provide a reasonable basis for comparison among processes. Cost
calculations in Section XI will compare performance and cost considerations.
   The  unit costs are based on point  estimates  and  should  be considered  as
preliminary or  planning estimates only. For more complete and  detailed cost
analysis, including sensitivity analysis,  see the  references  cited in  Section XII.
Additional data  are being collected concerning the cost and performance of the unit
processes discussed in this section. Realistically, cost data developed in this analysis
should be considered accurate in a relative sense. In  a site-specific  situation,
particular circumstances may influence the amount or cost of an input factor (labor
hours or S/labor  hour,  for example) required to produce a given water quality
output.
   This section deals with costs for the technology most closely associated with each
of the three control approaches  discussed  previously. Treatment  techniques
discussed for the first approach (removal of trihalomethanes) are diffused-air and
tower-aeration and special adsorption resins. Methods discussed for the second
approach (removal of trihalomethane precursors) include clarification, coagulation-
sedimentation-filtration, direct filtration and precipitative softening, P AC and GAC
adsorption, ion exchange resins, the combination of ozone and ultra-violet radiation
(Oif UV), and the combination of ozone and GAC adsorption. Discussion of the
third approach (alternative disinfectants) involves cost comparisons of chlorination,
ozonation, chlorine-ammonia, and chlorine dioxide treatment. Many of the cost
data  used  in this section were  derived  from a study prepared for USEPA by
Culp/Wesner/Culp Consulting Engineers.184

228  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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   120 -
                                                                    . 25
                                                                     20
                                                                        O
                                                                        o
                                                                        z

                                                                        <
        O      20     40      6O      80     100     120    14O      160
                       TREATMENT PLANT CAPACITY, mgd

        I	1	1	1	1	h-	1	1	1
        0      76     151      227     302     378     454    529      605
                  TREATMENT PLANT CAPACITY, thousands mVday


            Figure 119.  Total treatment unit costs vs. plant capacity.
General Considerations

  For each unit process and combination thereof, the assumptions made for the cost
analysis will be given, followed by a graphic presentation of the influence of key
variables on the total treatment cost—i.e., amortized capital costs plus  operation
and maintenance (O&M) costs.'8* Finally, specific cost figures for one given set of
assumptions will be presented.
  The choice of a set of assumptions is not intended to reflect performance levels
between processes but only to reflect costs within typical design levels. Pilot studies
should be done to provide comparative performance information. Table 86 contains
the cost assumptions used in each of the calculations.
 TABLE 86. COST ASSUMPTIONS USED THROUGHOUT SECTION X
Item
Level
Energy
labor
Producers Price index (1980)
Engineering News Record Index (1980)
Interest rate
Amortization rate
$0.04/kWh
$10,00/hr
243.8
325.0
8 percent
20 yr
                                             Section X, Treatment Costs  229

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 Economies of Scale

   One of the  general  issues that relates to cost estimating for water supply
 technology is that of economies of scale. As the size of the facility decreases the unit
 cost of the facility tends to increase.  Figure 119, the unit  costs for conventional
 treatment, direct filtration, and precipitative softening illustrate this effect. This
 figure is based on a specific set of assumptions that will be discussed more completely
 in the Subsection Removal of Trihalomethane Precursors, below. The "scale effect"
 is, however, one that will apply to all technologies over the size ranges discussed. For
 example, in  Figure  119, the cost of conventional treatment at 37,800 m'/day (10
 mgd)  is approximately  8c/mJ (30c/1000 gal); at 18,900 ms/day (5 mgd), 10e/m3
 (36e/ 1000 gal); and at 3,780 m /day (1 mgd),  !ic/mj (42c/ 1000 gal). These same
 percentage changes  in cost with facility size can be applied to all of the technologies
 discussed in the following section as an approximate technique for estimating scale
 economies.

 Cost Analysis Results

 Removal of Trihalomethanes—
   Diffused-Air Aeration—Diffused-air aeration involves passing air through the
 process  flow stream. For  this analysis,  this is assumed to take place in open,
 reinforced concrete basins with  direct-drive centrifugal compressors and porous
 diffusors placed at  close intervals  over the entire basin flpw for air introduction.
 Process energy requirements  include the operation of the air compressors  365
 days/year,  24  hours/day.   Maintenance  materials  include  lubricants  and
 replacement components for air compressors and air diffusion equipment. Estimates
 were developed from a  review of costs associated with activated sludge aeration
 facilities. Labor requirements include  maintenance of air compressors, air piping,
 valving  and diffusors,   and  aeration basins. Table 87 contains some of the  key
 assumptions used in calculating the costs associated with diffused-air aeration.
   The effectiveness  of using aeration as a technique for stripping trihalomethanes
 depends heavily on the air/water ratios used (see Section V!, Subsection Diffused-
 Air Aeration).  In turn, the cost of diffused-air aeration also depends on the air/ water
 ratio.  With the use of ihe design assumptions in Table 87, total treatment costs were
 calculated (Figure  120) for diffused-air aeration systems  with air/water ratios
 ranging from 1:1 to  30:1, and capacities of 37,800 and 378,000 m'/day (10 and  100
 mgd).*  The systems were assumed to be  operating  at 70-percent  capacity. A
 breakdown of costs (O&M, capital, and total) for the same systems operating at
 70-percent capacity  with a 20:1 air/water ratio is shown in Table 88.

         TABLE 87. DIFFUSED-AIR AERATION ASSUMPTIONS

 Item	Assumption	
 Basin depth             3.3m (10 ft)
 Air supply              1.52 smVm2 (5 scf/ft2)
   Aeration Towers—Stripping of trihalomethanes from water can be accomplished
 in aeration towers similar to those used for oxidation of iron and manganese (see
 Section VI, Subsection Tower Aeration). As with diffused-air aeration, the degree of
 removal of a specific organic compound by this technique depends on the Henry's
* t hcte caruottes jrc u>ed throughout this section lo reflect thcdi!lcrcncc> between small and Urge treatment plantv A .17.800-
 m1 d*) lIG-fngd) treatment plant operating at 70-percent capacity would serve a population of 75.000  the si/c covered hy
 the firs! ph*»c of the Tfihalcimethane Regulation. Cost* for .tfflalier treatment plant* are currently bcifi£ collected and will he
 4%Mtfafitc bdwfc Ntnembcr 29. 19BJ. uhen the -iecond phase of Ine Trihalomcthttne Regulation' hecome* mandatory.


23O   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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a
8»

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    TABLE 88. CAPITAL AND O&M COSTS FOR A DIFFUSED-AIR
AERATION SYSTEM OPERATING AT 70-PERCENT CAPACITY WITH A
                       20:1 AIR/WATER RATIO

                     	System treatment capacity	
                      37.800 mVday (10 mgd)  378,000 mVday (100 mgd)
Item
O&M cost
Capital cost
Total treatment cost
0/ifV>
2.0
1.8
3.8
0/1 000 gal
8.2
7.1
15.3
6/m3
1.1
1.8
2.9
C/1000gal
4.5
7.3
11.8
law constant of the compound, the air/water ratio, water temperature, and many
other factors.
  Estimated construction costs are for rectangular aeration towers with polyvinyl
chloride (PVC) packing media. For towers smaller than 178 mj (6,400 ft'), units are
shipped assembled and  have fiber-glass skins supported by a galvanized metal
framework.  Towers  of greater volume are field-erected  from  factory-formed
components and are similar in design and construction to industrial cooling towers.
The exterior skin of corrugated asbestos-cement panels is attached to a structural
steel framework. Towers are supported on reinforced concrete basins. The basin
collects tank underflow and serves as a sump for the pump.
  The cost estimate presented here includes the tower supply  pumps and tower
underflow pumps. These aeration towers have electrically driven, induced-draft fans
with fan stacks and drift eliminators. Process electrical energy requirements are for
operation of  the  induced-draft  fan, assuming  a  24-hour/day, 365-day/year
operation. In some  instances where  pumping energy may  also be required,  it  is
estimated separately as part of the  unit operation cost; but pumping head will vary
from application to application. Units are assumed notio be housed, eliminating the
need for building-related energy. Some localities may have to consider protecting the
unit(s) from inclement weather, which would incur an additional  cost. Table 89
contains the assumptions used in calculating tower aeration costs.

            TABLE 89. AERATION TOWER ASSUMPTIONS

Item	Assumption	
Towar height         6.1m {20 ft)
Pumping             9.1 m (3O ft) total dynamic head
Air supply            15.92 smVm2 (52.25 scf/ft2) of tower surface area
  As with diffused-air aeration, the effectiveness of tower aeration depends heavily
on  the assumed air/water ratio.  Total treatment costs are calculated for tower
aeration systems with air/water ratios ranging from l:l to 800:1 (Figure I2I). A
breakdown of costs (O&M, capital,  and  total) for these systems operating at an
average 70-percent capacity for an air/water ratio of 500:1 is given in Table 90.
Some tradeoffs are  possible—for example,  increasing the  tower depth  versus
increasing the air/water ratio to achieve increased removal  of volatile organics.
These options are explored as follows.
  Based on the assumptions used in this analysis, several mechanisms are available
for removing volatile organics. One  option for  a  given tower depth would be to
increase the surface area of the tower, thereby increasing the amount of air induced
into the water stream. Another option would be to fix the surface area of the tower

232  Treatment Techniques tor Controlling Trihalomethanes in Drinking  Water

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                  200
                           400      600     800

                          AIR/WATER RATIO (V/V)
1000
                                                            1200
         Figure 121.  Total treatment costs for tower aeration systems,
                     37,800- and 378,000-mVday (10- and 100-mgd)
                     capacities.
 TABLE 90, CAPITAL AND O&M COSTS FOR A TOWER AERATION
  SYSTEM OPERATING AT 70-PERCENT CAPACITY WITH A 50O:1
                         AIR/WATER RATIO
System treatment capacity
37.800 mVday (1 0 mgd) 378,000 mVday (1 00 mgd!
Item
O&M cost
Capital cost
Total treatment cost
C/m3
1.8
4.3
6.1
C/ 1000 gal
7.3
17.2
24.5
C/m3
1.6
2.S
4.1
0/1 000 gal
6.5
10.3
16.8
(thereby fixing the amount of induced air and thus fixing the air/ water ratio) and to
increase tower depth. These trade-offs are illustrated in  Figure  122. Table 91
contains some typical total treatment costs  for these options.
  Table 91 and  Figure 122 can provide some insight into the important trade-offs
involved in using tower aeration to remove trihalomcthanes. For example, assume
an initial design choice of a 6,6-m (20-ft) tower with an air/water ratio of 100:1. If an
identical target water quality could be achieved by using a 3.3-m (10-ft) tower with an
air/water ratio of 300:1, the cost would be slightly higher—1.6/m'{6.2/1000 gal) as
opposed to 1.3e/m'(4.9/1000 gal).

  Synthetic Adsorption  Resins—Granular synthetic resins can be used for  the
adsorption of trihalomethanes (see Section VI, Subsection Synthetic Resins). Data
presented  in this subsection are for a special resin called Ambersorb® XE-340. Cost
equations  were derived from preliminary cost data provided by the company  (F.
Slejko, Rohm & Haas Co.,  personal communication, 1980). For this analysis,  the

                                             Section X. Treatment Costs  233

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234  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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TABLE 91, TOTAL TREATMENT COSTS OF ALTERNATIVE DESIGNS
    FOR A 37,800-m3/day (10-mgd) TOWER AERATION SYSTEM
Tower
depth
m
3.3
6,6
9.9
13.2
ft
10
20
30
40
C/m*
0.3
1.3
1.7
1.9
100:1
C/1000 gal
3.3
4.9
6.0
7.2
Air/ water ratio

C/m3
1.6
2.4
3.2
4.1
300:1
C/1000 gal
6.2
9.1
12.0
15.5

C/m3
2.2
3.3
4.8
6.2
500:1
0/1OOOgal
8.5
12.5
18.2
23.6
information has been based on 1977 costs updated to 1980 with the Construction
Cost Index and the Producers Price Index (see Table 86), The data in Table 92 show
the assumptions used in developing the Ambersorb® XE-340 costs. To calculate
empty bed contact times (EBCT), specific design configurations were assumed for
the two system sizes (Table 92).

          TABLE 92.  AMBERSORB® XE-340 ASSUMPTIONS


Item	Assumptions	
Resin loss per regeneration            5 percent
Steam cost per regeneration           $674.28/m3(S18.73/ft3) per reactivation
Solvent cost par regeneration          $32,40/m3 ($0.90/ft3) per reactivation
Quality control                       59,000/yr
Resin cost                           $19.25/m3 («8.75/lb)
Resin density                        605 kg/m3 (37 Ib/ft3)
37,800-mVday (10-mgd) system      6 Contactors at 8 m3 (289 ftj)/contactor
378,000-mVday (1OO-mgd) system    20 Contactorsat 24m3(862ft:l)/contactor
   The interrelation of EBCT,  time  between regeneration,  and total costs for
treatment with Ambersorb® XE-340 for the two system sizes is shown in Figures 123
and 124. Table 93 presents O&M, capital, and total treatment costs  for the two
system sizes with an EBCT of 4 minutes, a regeneration frequency of once every 3
months, and an average operating capacity of 70 percent. Note that costs for disposal
of the condensate are not included.

Removal of Trihalomethane Precursors—
   Clarification—One technique for reducing the formation of trihalomethanes in
water is to lower the concentration of trihalomethane precursors. Treatment
techniques such  as coagulation-sedimentation-filtration (conventional treatment),
direct filtration,  and precipitative softening may be employed  in this manner (see
Section VII, Subsection Clarification). Table 94 lists the unit processes assumed in
each of these treatment trains, and Table 95 contains some of the assumptions used
in generating the costs for them.'*6 Total treatment cost curves are shown in Figure
119 for all these types of treatment plants, calculated for capacities from 3,780 to
567,000 m3/d (1-I50 mgd). Tables 96, 97, and 98 contain O&M, capital, and total
treatment costs for the two system sizes operating at an average 70-percent capacity.
Note that free chlorination is included in these costs.
   The costs listed in Tables 96, 97, and 98 would apply if a new treatment plant were
constructed and  operated. In many locations, however, clarification plants already
exist. As discussed in Section VII, Subsection Clarification, improving clarification
and moving the point of chlorination from the source water to later in the treatment

                   .               , .        Section X. Treatment Costs  23S

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       120
                                                                30
                   2      4      6      8      10     12

                      TIME BETWEEN REGENERATIONS, mo
         Flguro 123.  Total treatment unit costs vs.  regeneration fre-
                      quency for a 37,800-mVday (1 0-mgd) Ambersorb®
                      XE-340 system at various EBCT's.
       O
       o
           120
        a  100
                     2     4     6     8     10    12    14

                     TIME BETWEEN REGENERATIONS, mo

         Figure 124. Total treatment  unit costs  vs. regeneration fre-
                     quency for a 378,000-mVday (100-mgd) Amber-
                     sorb® XE-340 system at various EBCT's.
236  Treatment Techniques for Controlling Trihatomethanes in Drinking Water

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      TABLE 93, CAPITAL AND O&M COSTS FOR TREATMENT
                    WITH AMBERSORB®XE-340*

                    	System treatment capacity	
                     37.800 mVday (10 mgd)  378.000 m3/day (100 itifld)
Item
O&M cost
Capital cost
Total treatment cost
C/m3
2.8
6.2
9.0
0/1 000 gal
11.1
24.7
35.8
C/m3
2.8
5.5
8.3
0/1 000 gal
11.1
22.1
33.2
•Three-month regeneration frequency, 4-minute EBCT. Average operating capacity is 70 percent.
   TABLE 94. UNIT PROCESSES ASSUMED IN EACH TREATMENT
                                TRAIN
Direct filtration
Alum feed
Polymer feed
Chlorine feed*
Rapid mix
Conventional treatment
Alum feed
Polymer feed
Chlorine feed*
Rapid mix
Precipitative softening
Lime faed system
Chlorine feed*
Rapid mix
Upflow solids contact
Flocculation
Gravity filtration
Hydraulic surface wash
Backwash pumping
Clearwell storage
Wash water surge basins
Flocculation
Sedimentation
Gravity filtration
Hydraulic surface wash
Backwash pumping
Clearwell storage
Wash water surge basin
  clarifier
Recarbonation basin
CO, source
Gravity filtration
Hydraulic surface wash
Backwash pumping
Clearwell storage
Wash water surge basin
Sludge handling
Lime recalcination
'Chlorine included in these unit processes.
      TABLE 95. CLARIFICATION TREATMENT ASSUMPTIONS
Item
Alum
Polymer
Chlorine
Lime
Natural gas
Diesel fuel
Dose
15 mg/L, 25 mg/L
0.2 mg/L
2 mg/L
300 mg/L
—
—
Assumed cost
$0.08/kg ($70.00/ton)
S4.40/kg ($2.00/lb)
$0,33/kg (S300.00/ton)
$0.07/kg <«65.00/ton)
$0.01 4/sm3 ($0.001 3/scf)
$0,17/L($0.65/gal)
                                           Section X, Treatment Costs 237

-------
  TABLE 96. CAPITAL AND O&M COSTS FOR DIRECT FILTRATION"
System treatment capacity
37,800 mVday (10 mgd) 378,000 mVday C100 mgd)
Itam
O&M cost
Capital cost
Total treatment cost
C/m1
2.5
3.9
6.4
C/1000 gal
9.6
14.9
24.5
C/m3
0.9
1.7
2.6
C/1000 gal
3.5
6.4
9.9
"Chemical dote; Alum, 15 mg/U polymer. 0.2 mg/U chlorine, 2 mg/L, Average operating capacity is
 70 percent.
    TABLE 97. CAPITAL AND O&M COSTS FOR CONVENTIONAL
                             TREATMENT*


                     	System treatment capacity	
                      37,800 mVday (10 mgd)  378.000 mVday (100 mgd)
 	Item	C/m3     C/1000 gal      C/m3     C/1000 gal
O&M cost                 2.8         10.8          1.1           4.2
Capital cost               4.9         18.6          2.2           8.2
Total treatment cost        7.7         29.4          3.3         12.4

•Cnemicat dosa: Alym, 25 mg/L* polymer, 0.2 mg/L; chlorine. 2 mg/1. Average operating capacity is 70
 p*rc*nt.


     TABLE 98. CAPITAL AND O&M COSTS FOR PRECIPITATIVE
                              SOFTENING*

                     	System treatment capacity	
                      37.800 mVday (10 mgd)  378.000 mVday (100 mgd)
I torn	C/m3     C/1000 gal      C/m3     C/1000 gal
O&M cost                 4.8         18.5          3.3         12.5
Capital cost               6.6         25.0          2.5           9.6
Total treatment cost       11.4         43.4          5.8         22.2

*Ch*m!cal doia: Urn*. 300 mg/L; chlorine, 2 mg/L, Average operating capacity is 70 percent.
 train will, in many cases, improve trihalomethane precursor removal. This step is a
 potentially  inexpensive approach to trihalomethane control.  Because changing
 coagulant dose or type (or both) and moving the chlorination point involves little or
 no capital expenditure, treatment costs  for these techniques would be very low.
 Furthermore, applying  the chlorine at a point  in the treatment train where the
 disinfectant demand is lower than in the source water may permit lower doses to be
 used to achieve the same  residual, thereby actually reducing overall treatment
 cost.12""
   Figures 125, 126, and  127 show the sensitivity of cost tochanges in coagulant dose
 for clarification and in  lime for  precipitative softening, for 37,800- and 378,000-
 m*/day (10- and 100-mgd)  plants at 70-percent capacity.

 238  Treatment Techniques for Controlling Trihaiomethanes in Drinking Water

-------
    6
n



<*  5


CO

B  4


Z
=5  3
P  2
              30
           _  25
           a
           01
           O
           o
           O  20
           8  15
           O
              10
                          1       I
               37,800 mj/day (10 mfld!
                          378,000 mVday (100 mgd)
                          10     2O      30      40      50

                                    ALUM DOSE, mg/L
                                                                60     70
        Figure 125.  Total treatment unit costs of clarification by direct
                     filtration vs. alum dose.
   is
   OT
  co
  O  20
  CJ
      10
  O
      I        I        I
37,800 mVday (10 mgd!
                                       378,000 mVday (1 00 tngdj
                                                                    10
                                                                       e
                                                                       o
                                                                       CO
                                                                       O
          0       10     20      30      40     50      60      70

                            ALUM DOSE, mg/L


        Figure 126.  Total  treatment unit costs of clarification by con-
                     ventional treatment vs. alum dose.
                                             Section X. Treatment Costs  239

-------
                                                                  15
                                                                      E
                                                                 • 10  o
                                                                      O
                                                                      O
                                                                  51
            0      100     200    300    400    500    600     700

                             LIME DOSE, mg/L.

         Figure 127.  Total treatment unit costs of clarification by precipi-
                      tative softening vs. lime dose.

  Granular Activated Carbon Adsorption—As discussed in Section VII, Subsection
Granular  Activated Carbon,  GAC adsorption is  effective for trihalomethane
precursor removal.  For  this  analysis,  two types of  GAC systems  will be
considered.'"'"'One system uses activated carbon in separate contactors after sand
filters (hereafter called  "post-filter adsorbers"), and the other  uses  GAC as a
replacement  for the  media  in existing  filter  beds  (hereafter  called "sand
replacement"). Both systems will be considered with onsite thermal reactivation. The
need to consider the cost  of separate GAC  contactors is eliminated if  GAC is
assumed to replace  sand in existing filters.
  For purposes of the sand replacement analysis, a water treatment plant is assumed
to consist of an integral number of 3,780-m3/day (l-mgd) filters. Design parameters
assumed for  the sand  replacement  systems  are listed in Table 99,  and design
assumptions for post-filter adsorption systems are presented in Table 100. Note that
for  sand replacement systems, a GAC loss  of 10  percent/reactivation  cycle is
assumed, but a GAC loss of only 6 percent/reactivation cycle is assumed for post-
filter adsorbers.  These two assumptions are intended to reflect differences in the
operation of the two systems. Sand replacement systems are labor intensive and
increase  the  possibility of GAC loss  because the  activated carbon  is  changed
manually and frequently backwashed. In post-filtration systems, fewer possibilities
exist for handling losses, because the activated carbon is assumed to  be changed
hydraulically and is seldom backwashed between reactivation cycles.
  Figures 128 through 131 present total treatment cost curves for both 37,800-m3/
day and 378,000-m /day (10- and  100-mgd) sand  replacement and post-filter
adsorption systems. Table 101 (page 244)  contains  O&M,  capital, and total
treatment costs for  both systems operating at an average 70-percent capacity.

  Powdered Activated Carbon Adsorption—PAC has been suggested for removal
of trihalomethane precursors (see Section VII, Subsection Adsorption), and PAC
costs have been developed for such an application. The PAC systems were sized for
240  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
   TABLE 99, DESIGN PARAMETERS ASSUMED FOR GAC SAND
                       REPLACEMENT SYSTEMS


Item	Assumption	
Activated carbon cost              $1,54/kg ($0.70/lb)
Activated carbon loss
  per reactivation cycle             10 percent
Fuel cost                          0.17C/million joules ($1.80/million BTU)
Volume per filter                   24 m3 (856 ft3)
Loss in adsorptive capacity          0 percent
Hearth loading                     354 kg/day/m2 (70 Ib/day/ft2}
TABLE 100. DESIGN PARAMETERS ASSUMED FOR GAC POST-FILTER
                              ADSORBERS

Item	Assumption	
Activated carbon cost               $1,54/kg ($0.70/lb)
Activated carbon loss
  per reactivation cycle              6 percent
Fuel cost                          O. WC/million joules ($1.80/million BTU)
Hearth loading                      354 kg/day/m2 (70 Ib/day/ft2)
Adsorber configuration:
  37,800-m3/day (10-mgd) plant:
    No. of adsorbers                8
    Diameter of adsorber            3.7m (12 ft)
    Vol./adsorber                   41 m3 (1,470 ft3)
  378,000-mVday (100-mgd) plant:
    No. of adsorbers                28
    Diameter of adsorber            6.1 m (20 ft)
    Vol. /adsorber                   122 m3 (4,396 fta)
Loss in adsorptive capacity per
  reactivation cycle                 0 percent
 feeding an 11-percent slurry by weight. The ! l-percent slurry is assumed to be stored
 and continuously mixed in uncovered concrete tanks that are placed below ground
 level, except for the top foot or so. For feed capacities of less than 320 kg/hr (700
 lb/ hr), 8 days of storage in two equal-size basins are included. For greater feed rates,
 2 days of storage in a single basin are included. Mixers were sized based on a G value
 of 600/sec"1. Storage,/mixing basins include equipment for  PAC feed from bags in
 smaller installations and  from trucks or railroad cars in larger installations.
   Energy requirements are based on the  rated horsepower of a pump motor for
 continuous mixing of the 11-percent carbon slurry at a G value of 6QO/sec"', PAC
 requirements were estimated for various configurations. Labor requirements for the
 mixing/storage  basin  are  30  min/day  per  basin  for inspection and routine
 maintenance, and  16 hr/year per basin for cleaning and gearbox oil change. Slurry
 pumps require 1 workhour/day per pump. Figure 132 (page 244) shows the total
 costs for PAC treatment  at  PAC concentration ranges of 5  to 45 mg/ L and for five
 different system capacities. Table 102 (page 245) contains O&M, capital, and total
 treatment c5sts for 37,800- and 378,000 m'/day (10- and  100-mgd) systems feeding
 25 mg/L PAC and operating at an average 70-percent capacity.

                                              Section X. Treatment Costs 241

-------
                        24       6       8      10

                          TIME BETWEEN REACTIVATIONS, mo
                                                               12
                                                                       14
         Figure 128.  Total  treatment unit  costs vs.  reactivation  fre-
                     quency for a 37,800-mVday (10-mgd) GAC sand
                     replacement system at various EBCT's.
                        2       4       6       8      10      12

                           TIME BETWEEN REACTIVATIONS, mo
t4
         Figure 129.  Total treatment unit costs vs. reactivation fre-
                     quency for a 378,000-mJ/day(100-mgd) GAC sand
                     replacement system at various EBCT's.
242  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
              35
              30-
 E
 \
 o
 O
 O
           o  20 •
           in
           O
           o
              IS-
              10-
              0'.
                 02      4       6       8      10      12

                          TIME BETWEEN REACTIVATIONS, mo



         Figure 130.  Total treatment  unit costs  vs. reactivation fre-

                     quency for a 37,800-mVday (10-mgd) GAC post-

                     filter adsorber at various EBCT's,
                                                                      14
E
\
o


CO
O
u
12





10




 8
              25
              20
       °. 15
           8
           t 10
           z
                  02"      4-68      10      12


                            TIME BETWEEN REACTIVATIONS, mo


         Figure 131.  Total  treatment unit-costs vs. reactivation fre-

                     quency for a 378,000-mVday (100-mgd) QAC post-

                     filter adsorber at various EBCT's.
                                                                   14
                                             Section X. Treatment Costs  243

-------
  TABLE  101. CAPITAL AND O&M COSTS FOR GAC ADSORPTION
                                       System treatment capacity
Itam
37.800 mVday (10 mgd) 378.000 mVday (100 mod)
              C/100Qial     C/m3      C/IOOOgal
S«nd replacement system:*
O&M cost
Capital cost
Total treatment cost
Post-filter adsorbent
O&M cost
Capital cost
Total treatment cost

0,8
1.3
2.1§

0,8
2,1
2.9§

3.1
5.0
8.1§

3.0
8.1
11. 1§

0.7
0.6
1,3§

0.6
1.2
1.8§

2.6
2.1
4.7§

2.5
4.7
7.2§
*Nine,mir*ute 1BCT.  3-month reactivation frequency, 10-pareent loss/ reactivation. Average operating
 capacity !i 70 parcent.
fElQhieen'fnlnute EBCT, 6-month reactivation frequency, 6-percent loss/ reactivation. Average operating
 capacity it 70 percent,
{The reader is reminded that these costs were calculated using a reactivation furnace hearth loading of 3S4
 kg/d/m1 170 Ib/d /ft1).'" Previous report* Hfed • value of 202 kg/d/m1 (40 Ib/d/ft').'" Using thia lower velue
 I elsea these costs 18 percent for both of the 37.80 0 -mV d (10- m gd) systems, 11 percent for the 378,000-mVd
 (100.rnfld| send replacement system and 4 percent for the 378.000-mVd (lOO-mgd) pott-filter adsorber
 system.
          Figure 132.  Total treatment unit costs for  PAC treatment vs.
                       PAC dosB~for different plant capacities.
   Ozone Plus Granular Activated Carbon Adsorption—As shown earlier in this
section under Granular Activated Carbon Adsorption, reactivation frequency has
an important impact on the cost of GAC operation. GAC in combination with
another unit process that helps lengthen the time between reactivations might result
in a less expensive system.
   Costs for a hypothetical system in which ozone is combined with a 378,OQO-m3/day
(lOO-mgd) post-filter adsorber are shown in Figure 133. If the system is operating ini-
tially at point "Pi" without ozone (2 months between reactivations), then the addi-
tion of 2 mg/ L ozone would have to increase the time between reactivations lo "Pa"

244  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
  TABLE 102. CAPITAL AND O&M COSTS FOR PAC TREATMENT'
                                   System treatment capacity
Item
O&M cost
Capital cost
Total treatment cost
C/mJ
1.7
0.2
1.9
C/IOOOgal
6.9
0.7
7.6
C/rn3
1.6
0.1
1.7
C/ 1000 gal
6.4
0.2
6.6
*PAC doss is 25 mg/L. Assumed cost for PAC is S0.66/kg (S600/ton|. Average operating capacity Is 70
 percent.
         Figure 133.
   246        8       10       12

     TIME BETWEEN REACTIVATIONS, mo

Total treatment unit costs for ozone plus GAC treat-
ment vs. reactivation frequency for various ozone
doses.18"
(2.8 months) to break even on total treatment cost. The data in Table 103 show the
increase in time between reactivations needed to break even on total treatment cost
for various ozone dosages. These data were calculated for a system operating at a
reactivation frequency of once every 2 months without ozone.

  Ozone plus  Ultra-violet Radiation—The combination of o/one and ultra-violet
radiation (Oj/UV) is a  new treatment  technology. Results  of a recent research
project  are  presented  in  this subsection,  and no  attempt has been made to
extrapolate the available costs beyond  these results.40 This study found that  the
process  was effective in  the removal  of  trihalomethanes  and trihalomethane
precursors (see Section  VI, Subsection Ozone/Ultra-Violet Radiation and Section
VII, Subsection Ozone/Ultra-Violet Radiation). Representative costs developed by
an engineering consultant working on the project are presented  in Table 104.

  Anton Exchange—Anion exchange has proven effective for removing most of the
organic  trihalomethane  precursors  and  thereby preventing the  formation of
trihalomethanes, (see Section VII, Subsection Ion Exchange).  To calculate costs for

                                              Section X. Treatment Costs  24S

-------
  TABLE 103. REACTIVATION FREQUENCY REQUIRED TO OFFSET
                      COST OF ADDING OZONE


          Ozone dosage.                     Break-even point,*
 	mg/L	months	
                0                                  2
                2                                  2.8
                4                                  3.7
                6                                  5

•Total treatment cott.


   TABLE 104. RANGE OF O3/UV COSTS FOR TRIHALOMETHANE
                      PRECURSOR  REMOVAL40
System treatment capacity
37.800 mVday (10 mgd) 378.000 mVday (100 mgd)
Item
Ozone from O3:
O&M cost
Capital cost
Total treatment cost
Ozone from air:
O&M cost
Capital cost
Total treatment cost
C/m3
1.4
0.3
1.7
1.5
0.5
2.0
- 2
- 0
- 2
- 2
- 1
- 3
.0
.5
.5
.4
.1
.5
C/1000
5.4
1.2
6.6
6.1
2.0
8.1
- 7.
- 2.
-9.
- 9.
- 4.
- 13
gal
8
1
9
4
4
.8
C/m3
1.3
0.3
1.6
1.5
0.5
2.0
-2.0
- 0.5
-2.5
- 2.1
- 1.0
- 3.1
C/1000 gal
5
1
6
5
1
7.
.2 -
.1 -
.3 -
.8 -
.9 -
7-
7.9
2.0
9.9
8.4
3.9
12.3
this type of treatment, two configurations were assumed: I) a 37,800-m3/day (10-
mgd) plant svith one 4l-mJ (I470-ft3) contactor and 2) a 378,000-m3/day (100-mgd)
plant with ten 4l-m'1(l470-ft3)contactors. Assumptions used in developing the anion
exchange costs are presented in Table 105. The interrelation of EBCT, regeneration
frequency, and total treatment cost for the two system sizes is illustrated in Figures
I34 and I35. O&M, capital, and total treatment costs for the two system sizes are
presented in Table  106.

          TABLE 105. ANION EXCHANGE ASSUMPTIONS

Item	Assumption	
Resin loss per regeneration         5 percent
Quality control                    $9,000/yr
Resin cost                        $6.480/m3 ($180/ft3)
Resin density                      736 kg/m3 (45  Ib/ft3)
Regeneration cone. (NaOH)         4 percent
Regenerate quantity               65  kg NaOH/m3 (4 Ib/ft3)
Sodium hydroxide cost             $0.22/kg ($200/ton)
Regeneration requirement          6,800 L/m3  (50 gal/ft3)
10 mgd                          1 contactor at 41 m3 (1.470 ft3)
                                  per contactor
100 mgd                         10  contactors at 41 m3 (1,470 ft3)
                                  per contactor
 246  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
   SO
8
O  40
Z
3  20
                                                                      15
                                                                      10
                    1.2             3             4

                     TIME BETWEEN REGENERATIONS, mo

         Figure 134. Total treatment  unit costs  vs. regeneration fre-
                     quency for a 37,800-mVday (1O-mgd) anion ex-
                     change system at various EBCT's.
                                                                         o
                                                                         u
                                                                         <
                                                                         o
                    1234

                      TIME BETWEEN REGENERATIONS, mo

         Figure 135.  Total treatment  unit costs vs. regeneration fre-
                      quency for a 378,000-mVday (100-mgd) anion ex-
                      change system at various EBCT's.
                                             Section X. Treatment Costs  247

-------
  TABLE 106. CAPITAL AND O&M COSTS FOR ANION EXCHANGE'
System treatment capacity
37,800 mVday {10 mgd} 378,000 mVday (100 mgd)
Item
O&M cost
Capital cost
Total treatment cost
e/m3
6.7
0.6
7.3
C/1000gaI
26.8
2.5
29.3
C/m3
6.7
0.6
7.3
q/ 1000 gal
26.8
2.4
29.2
*R*B*nerat3on frequency, 2 weeks; EBCT, 4 minutes; loss/regeneration, 5 percent; average operating capacity,
 70 perc«nt,

Alternative  Disinfectants—
   Chlorine—The design variables unique to the cost computations for chlorination
are shown in Table !07.IVO
   Total  treatment costs  for chlorination versus chlorine dosage  are depicted  in
Figures  136 and  137 for various sizes of plants with and without contact basins,
O&M, capital, and total treatment costs for 37,800- and 378,000-m'/day (IO- and
100-mgd) plants are listed in Table  I08.

              TABLE  107. CHLORINATION ASSUMPTIONS
Item
                                    Assumption
Cost of chlorine
Chlorine dose
Contact time (when used)
                                    $0.33/kg (S300/tonJ
                                    2 mg/L
                                    20 minutes
   O)  4
»   3
H*
to
O
a
                                        378,000 mVday (100 mgd)
                        37.800 mVday (10 mgd)
              18.900 mVdayCSmgd)
                                                                   1,25
                                                                   1.00
                                                                   0,75
                                                                0.50
                                                                      3

                                                                      2
                                                                      o
                                                                0.25  •-
          01       234       5
                          CHLORINE DOSE, mg/L

          Figure 136.  Total  treatment  unit  costs for  chlorination vs.
                      chlorine dose for different plant capacities without
                      contact basins.
248  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
   (D
   01
   O
   8  4  4-
   CO   3
   O
   O
   O
                        3.780 mVday (1 mgd)
                                           378.000 mVday (100 mgd!
              37,800 mVday (10 mgd)

18.900 mVefay (5 mgd)
                                         567.000 mVday (150 mgd)
                                                                    1.50
                                                                    1.25
                                                       1.00
                                                                    0.75
                                                                         O
                                                       0.50  <
                                                            O


                                                       0.25
          0    "   1        2        3       4       5       6      7
                          CHLORINE DOSE, mg/L

          Figure 137.  Total  treatment  unit costs  for  chlorination vs.
                       chlorine dose for different plant capacities with
                       contact basins.
   TABLE 108. CAPITAL AND O&M COSTS FOR CHLORIIMATiON*
System treatment capacity
Item
Chlorination
w/o contact basin:
O&M cost
Capital cost
Total treatment cost
Chlorination
with contact basin:
O&M cost
Capital cost
Total treatment cost
37,800 m3
C/m3
0.2
0.1
0.3
0.2
0.2
0.4
/day (10 mgd}
C/100Ogal
0.6
0.2
0.8
0.6
0.6
1.2
378,000 mVday (100 mgd}
0/m3 0/1 000 gal
0.1
0.1
0.1
0.2
0.3
0.1
0.4
0.3
0.4
0.7
•Chlorine dosa, 2 mg/L; operating at 70 percent of capacity on the average.


   Chlorine Dioxide—The cost assumptions unique to chlorine dioxide are listed in
 Table 109.
   To achieve equivalent disinfection results, the chlorine dioxide dose is assumed to
 be half that for chlorine; thus 1 mg/L of chlorine dioxide was assumed to achieve
 disinfection results equivalent to those achieved by 2 mg/ L of chlorine. The data in
 Figures 138 and  139 show the total treatment costs for chlorine dioxide for various
                                               Section X. Treatment Costs  249

-------
          TABLE 109. CHLORINE DIOXIDE ASSUMPTIONS
Item
Assumption
Chlorine
Sodium chlorite (NaCIO,)
Chlorine dioxide dote
Contact time (when used)
90,33/fcg (9300/ton)
$2.20/kg (82,000/ton)
1 mg/L
2O minutes
    14
     12 •
   & 10
  CO
  O
  u
                                                                 3.50
                                                                 3.00
                      2       3      4     i      6
                      CHLORINE DIOXIDE DOSE, mg/L

          Figure 138.  Total treatment unit costs for chlorine dioxide vs.
                      chlorine dioxide dose for different plant capacities
                      without contact basins.

 sizes of systems with and without contact basins. O&M, capital, and total treatment
 costs for chlorine dioxide for 37,800- and 378,000-m3/day (10- and lOO-mgd) plants
 operating at an average 70-percent capacity appear in Table ! 10.

   Ozonation—The cost of ozonation for various dosages and sizes of systems is
 shown in Figure 140. The data in Table 111 show O&M, capital, and total treatment
 costs for an ozone dose of 1 mg/L (assumed to be equivalent in disinfecting capacity
 to 2 mg/L of chlorine) for 37,800- and 378,000-rnJ/day (10- and  lOO-mgd) systems
 operating at an average 70-percent capacity,

   Chlorine-Ammonia  Treatment (Combined  Chlorine)—Combining ammonia
 with chlorine to form chloramines has been variously called the chloramine process,
 chloramination, and combined residual chlorination. The design assumptions for
 combined residual  chlorination are shown in Table 112.                ; .   .
 250  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
     16
     14
     12
  8
  2'io
  CO  „
  O  8
  O
      4 -
                                      37,800 mVday (10 mgdl
                           378,000 mVday (100 mgd)

                      567,000 mVday (ISO mgd( •   '
                                                                     4.00
                                                                     3.60
                                                                     1.80 jS
                                                                         O
                                                                     1.00
0.50
         0       1       2        3        4       56       7
                     CHLORINE DIOXIDE DOSE, mg/L


         Figure 139.   Total treatment unit costs for chlorine dioxide vs.
                       chlorine dioxide dose for different plant capacities
                       with contact basins.
     TABLE 110. CAPITAL AND O&M COSTS FOR CHLORINE DIOXIDE'
System treatment capacity
37,800 mVday {10 mgd) 378,000 mVday (1 00 mgd)
Item
Chlorine dioxide without
contact chamber:
O&M cost
Capital cost
Total .treatment cost
Chlorine dioxide
with contact chamber:
O&M cost
, Capital cost
Total treatment cost
• 
-------
                                                               4,00
                                                               3.EO
                                      18,900 mVday (S mgd)


                          37,800 rnVdaynOmgd)
           O      1      2      3       4       5
                           OZONE DOSE, mg/L

          Figure 140,  Total treatment unit costs for ozonation vs. ozone
                      dose for different plant capacities.

        TABLE 111. CAPITAL AND  O&M  COSTS FOR OZONE*
System treatment capacity
37,800 mVday {10 mgd) 378,000 mVday (100 mgd)
Item
O&M cost
Capital cost
Total treatment cost
0/m3
0.2
0,4
0.6
C/1000gaI
0.7
1.6
2,2
C/m3
0.1
0.3
0.4

-------
  Total treatment costs of combined residual chlorination for various chloramine
dosages and sizes of plants with and without contact basins areshown in Figures 141
and 142. O&M. capital, and total treatment costs for 37,800- and 378,QOO-rrr'/day
(10- and 100-mgd) plants appear in Table 113.
    10.5
                                                                    1.25
                                                                    1.50
                                                  E
                                                  x
                                                  o

                                                  to*
                                                  o
                                                  o
                                                                    0.75
          Figure 141.
  2 ,      3       4       5        6       7
 .CHLORAMINE DOSE, mg/L

Total treatment  unit costs  of chlorine-ammonia
treatment vs. chloramine  dose for different plant
capacities without contact basins.
 Discussion—
  The cost analyses in this section have shown the impact of several variables on the
 amortized capital and O&M costs for the unit processes that might be used for the
 control of trihalomethane concentrations in drinking water. Because the different
 unit processes have different objectives and different efficiencies in achieving these
 objectives, treatment costs can only be compared on the basis of equal performance.
 For example, to compare tower aeration with the use of PAC adsorption for a given
 percentage of trihalomethane removal.  Figure 25 would be used to estimate the
 air/water ratio needed, and Figure 29 would be used to estimate the PAC dosage
 needed. Then Figures 121 and 132 would be used to obtain the treatment cost for thai
 air/water ratio and PAC dosage, respectively. Thus, by combining these cost figures
 with the discussions on effectiveness presented in Sections V1-VII1, water utility
 personnel,  design engineers, and others  should be able to assess the relative costs
 associated with a given unit process.
  Water treatment processes  as typically employed exhibit  highly  variable
 efficiencies. Within the above limitations, a summary of total unit treatment costs has
                                              Section X, Treatment Costs  253

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    10.5
     9.0-
  ra
  <*> 7.5-
"  6.0-
t~

O
O

z  4'5 '
3


t  3.0-
     1.5
     3,780 mVday (1 mgd)





                         18,900 m'/day (5 mgd)


              37,800 mVday (10 m8
-------
been prepared (Table 114, Section XI) for each of the unit processes using a set of
conditions for the key variables that will produce equal effectiveness. The choice of
unit process would depend largely on the degree of the trihalomethane problem at a
particular utility. Process effectiveness varies greatly with the key variable assumed.
                                               Sect/on X. Treatment Costs  2SS

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                               SECTION XI
         SUMMARY OF TREATMENT CONSIDERATIONS

  Three approaches have been investigated for trihalomethane control: removal of
trihalomethanes, removal of trihalomethane precursors, and the use of disinfectants
other than free chlorine. Of these, the use of alternative disinfectants appears to be
the most effective and the least costly. Chlorine dioxide, ozone, and chloramines
produce no  significant  concentrations  of  trihalomethanes   when  used  as
disinfectants. Theoretically, any utility with any trihalomethane precursor concen-
tration  could  reduce  its  instantaneous  trihalomethane  (InstTHM)
concentration to almost zero by the use of one of these three disinfectant alternatives
to free chlorine. Furthermore, the cost of any of these unit processes, calculated
either with or without contact chambers, is very low (Tables 110, 111, and 113).
  The major disadvantage of this approach to trihalomethane control is that it does
not  remove  trihalomethane  precursors. Although no trihalomethanes  will  be
produced as disinfection byproducts, other byproducts will still be produced as the
oxidants (disinfectants) react with organic matter in the water.  Further, some of
these byproducts will be halogenated if chlorine dioxide or chloramines are used as
the disinfectant alternative.  Additionally, each of  the disinfectants has  inherent
disadvantages. For example, ozone does not produce a residual for the distribution
system, chloramine is a weaker disinfectant than free chlorine and may itself have
some unique toxicologic properties,l68'169 and chlorine dioxide produces chlorite and
chlorate as inorganic byproducts, anionic species whose health effects are currently
unknown."'1*4  Because  of  the  cost  advantages,  a  water  utility  requiring
trihalomethane control probably would consider the use of alternative disinfectants
as the first approach to meeting the Trihalomethane  Regulation,3 but utility
managers and their consultants should also consider the above disadvantages of this
approach.
  Alternatively, nine approaches to  the control of trihalomethanes by removal of
trihalomethanes and  trihalomethane precursors were studied: oxidation, aeration,
adsorption,  clarification, ion exchange, biodegradation,  pH adjustment, source
control, and intense mixing during disinfection. Within these nine approaches, 19
different techniques wereexamined. Several of these techniques were not extensively
tested  for this purpose: oxidation  by ozone plus  ultraviolet radiation  and  by
hydrogen peroxide, adsorption by Ambersorb® XE-340, ion exchange by strong-
and  weak-base resins, biodegradation,  and intense mixing during disinfection.
Although some of these techniques were effective, they will not be discussed further
because design considerations are less  amenable for immediate application.
  One of the remaining 12 techniques to be compared for treatment effectiveness
and  relative cost is source  control.  Source control is,  however, a  nontreatment
process and cannot be compared on an equal basis with the other unit processes.
Obtaining the best quality source water is of paramount importance and should be a
goal of all water utility managers and consulting engineers. Examination of the
source  for  possible  improvement  with respect  to  trihalomethane precursor
concentration is always important in the analysis of any water utility's practices.

Summary of Treatment Effectiveness and Costs*

  Table 114 compares the performance and costs of the remaining 11 unit processes:
oxidation by ozone,  chlorine dioxide, and potassium permanganate;  aeration by
  Alf coils >fc rounded to two vigmjlcan! figures,
256  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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diffused air and with aeration towers; adsorption by powdered activated carbon and
granular   activated  carbon;   clarification   by  coagulation-settling-filtration,
precipitative softening, and direct  filtration; and the lowering of pH. This table
summarizes the behavior of these unit processes with respect  to several common
areas: the effect on trihalomethane  precursor concentrations, the effect on trihalo-
methane  concentrations,  the  formation  of  other byproducts,  the effect  on
disinfection, and representative estimated costs.
   For this table, the representative estimated costs were calculated for a single
treatment plant size, 378,000 m3/d (100 mgd),at three levels of treatment success and
were based on the cost of chemical dosages and of other operating parameters that
achieved specified levels of treatment. These data were collected at specific utilities
studied and reported in Sections VI-X. These data  should be used for comparison
purposes  of costs for equal treatment and should not be considered universally
applicable.  Absolute effectiveness  of unit processes and  costs  will vary among
locations. This summary table draws together the most important features of all of
the processes listed for control of trihalomethanes  by removal of trihalomethanes
and trihalomethane precursors and  should allow the comparison of these processes
on an approximately equal basis.

Examples of Treatment  Options
   To assist water utility managers, consulting engineers, and others in assessing
treatment options, some treatment possibilities for the following four systems* will
be discussed:
   1) a 37,800-m'V d (10-mgd) ground water system  with chlorination only, having an
average InstTHM concentration in the distribution system! of 0.20  mg/L;
   2) a similar-sized groundwater utilityt with chlorination only, having an average
InstTHM concentration in the distribution system of 0.12 mg/L;
   3) a 378,000-m'/d (100-mgd) utility treating surface water with conventional
treatment, having an average InstTHM concentration in the distribution system of
0.20 mg/ L; and
  4) a 378,000-m'!/d (100-mgd) utility treating surface water with conventional
treatment having an average InstTHM concentration in the distribution system of
0.12 mg/L.
   For the purposes  i{ these examples, the alternative of using a disinfectant other
than free chlorine will not be discussed because that application is relatively straight-
forward. The reader is reminded, however, of the previously cited disadvantages to
this approach.
   The  discussion   of these  examples  will  focus  on  trihalomethane  and
trihalomethane precursor removal options in an attempt to show how water utility
managers, consulting engineers, and others can determine treatment effectiveness
and estimate treatment  costs as a first step to selecting the most reasonable options
for pilot study at the actual location. Of course, many other treatment options are
possible and should be considered  in  any actual case, but these  examples should
provide helpful guidance as to the proper approach. As noted in Table 114, each
process has disadvantages, and,  although they are not always mentioned  in the
following examples, they must not  be overlooked.

   1 A) 37,800-m^/d (10-mgd) Groundwater Utility 2 xMCL—0. IS mg/ L Imi THM
       in Finished Water:
   For the first example, the smaller utility treating gound water by chlorination only.
with a relatively high  InstTHM concentration (0.20 mg/L)  in the distribution
system, an approximate 50  percent lowering of the trihalomethane concentration in
•The first three examples wilt be discussed for two different cases: {A! where a large percentage of the possible trihalomeihatic
 production has occurred rspidK at the treatment plant, and (B) where a large amount of the possible trihalomethane
 production occurs in the distribution s\stcm after the water has Iclt the plant. .
'Kir the purposes «!' these examples, these gmunduater \vMems are assumed to have all the flow collected in one location,


                          Section XI. Summary of  Treatment Considerations 257

-------
    TABLE 114. SUMMARY OF SALIENT FEATURES  OF PRACTICAL AND EFFECTIVE
      PROCESSES FOR CONTROLLING TRIHALOMETHANES IN DRINKING WATER
Tr»itment
                          Precursor
                                              Trihalomethanos
                       Othar Byproducts
Oiont           Good lo very good destruction
Oxidation        is technically feasible. Hie
                apparent concentration may
                increase at low dosas. High
                doses and long contact times
                are required for good  destruc-
                tion, and complete destruction
                is difficult.
No effect by ozone,
some incidental
gas stripping.
Some are formed, but they
will not contain chlorine,
unless free chlorination
or chlorine  dioxide is
employed. Bromine-con-
taining THM may not be
formed on later chlorination.
Chlorini
Dioxide
Oxidation
Potassium
Pirminganate
Oxidation
Lowuing
PH
Good destruction is technically Mo effect.
feasible, but complete destruc-
tion was not achieved.
Fair destruction is technically No effect.
feasible, but complete destruc-
tion was not achieved.
Fair decline of TermTHM con- No effect.
centration is technically feasible.
Affects the rate of reaction be-
Some are formed by the
process and some will
contain halogen.
Some are formed by the
process and some will
contain halogen, if free
chlorine or chlorine dioxide
is used.
None formed by the process,
but some formed during
final disinfection.
                tween free chlorine and pre-
                cursor, thereby lowering
                resulting THM concentration.
Diffinad-
Alr
Airition






Tow«r
Aeration






No effect and THM will form Good to very good
if free chlorine is used. removal is techni-
cally feasible, but
bromine-containing
THMs are harder to
remove than chloro-
form. High air to
water ratios are
difficult to achieve.
No effect and THM will form Good to very good
if free chlorine is used, removal is feasible.
but bromine-con-
taining THMs are
harder to remove.
High air to water
ratios can be
achieved.
None are known to be
formed by the process but
some are still formed during
disinfection. Byproducts
will contain halogen if free
chlorine or chlorine dioxide
is used.


None known to be formed by
the process, but some are
still formed during disinfec-
tion. Byproducts will con-
tain halogen if free chlorine
or chlorine dioxide is used.


Continued
258  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
 TABLE tU. (Continued)
                         Representative estimated cost" for
                   378.000 m'/d (100 mfld) in C/m3 (t/1000gal)
     Disinfection    26% removal   50% removal  80% removal    Reforenca       Remarks
Excellent, but no
residual is created.
Organisms may re-
grow in the distri-
bution system.
                      Caddo Lake water. TX, Precursor Removal
.2 mg/L
0,48 (1.8)*
20 mg/L
2.1 (7.9)*
50 mg/L
4.0 (IS)*
         —with contact chambers-
Fig. 75
Fig. 140
Slightly belter at
high pH.

Good and provides
a residual. Slightly
more effective at
higher pH.


Poor; a disinfec-
tant must be used.




Free chlorine is
more effective at
lower pH.




A disinfectant is
required.







A disinfectant is
required.









Ohio River water, precursor removal
Not 8 mg/L Not
determined 3.2 (12)* achieved

w/o contact
chambers
Ohio River water, precursor removal
10 mg/L for Not Not
10 hours achieved achieved
2.6 (10)"
w/o contact
chamber
Daytona Beach. Ft precursor removal
0.3 pH unit Not Not
19%f achieved achieved
Equiv. of
2 mg/L
HjSQ,
0.03 (0.12)*
Cincinnati, OH, tap water, THM removal
A/W"=2:1 A/W=8:1 A/W=20:1
0.48 (1.8)* 1.3 (4.9)* 3.7 (14)*






North Miami Beach, FL, THM removal
Not A/W=4:1 A/W=32:1
determined. 0.56 (2.1)* 0.78 (2.9)*










Fig. 78 Residual oxidant
Fig. 138 should be limited to
0.5 mg/L because
of health effect


Table 41 Pink water with
overdose, Better
at high pH.



Table 45 May cause some
corrosion
problems.




Table 9 Influent air can be
Fig. 120 cleaned. Possible air
pollution problems.
Removes regulated
contaminant. Some
removal of SOCs®
and T&0# com-
pounds.

Table 12 Difficult to clean air.
Fig. 121 may entrain par-
ticulates. Possible
air pollution prob-
lems. Removes regu-
lated contaminant.
May have to protect
from freezing. Some
removal of SOCs@
and T&OS com-
pounds.
                                Section XI, Summary of Treatment Considerations  259

-------
TABLE 114. (Continued)
Tmlmint
                            Precursor
                                                  Trihalom ethanes
                         Other Byproducts
3owdtrnd Good to vary good removal is
ictivattd feasible. Removal is influenced
Utibon by influent concentration and
Usorpo'on the loading is proportional to
the influent concentration.
Good to vary good
removal is feasible.
Bromine-containing
THMs are better ad-
sorbed than chloro-
form. Removal is in-
fluenced by influent
concentration and
the loading is pro-
portional to the in-
fluent concentration.
None are farmed by the
process. Some removal of
those coming to the process
and less reformation as
related to TOC removal.
Will contain halogen if
chlorine or chlorine dioxide
is used.
Graitylir          Good to very good removal
Activated         technically feasible. Removal
Carbon           is nearly complete when ad-
Adsorption        sorbent is fresh, then break-
                  through toward exhaustion
                  begins. Complete exhaustion
                  generally does not occur,
                  however. Loading is propor-
                  tional to influent concentra-
                  tion and desorption may occur
                  when the influent concen-
                  tration declines.
Good to very good    None formed by the process
removal is techni-    and  some can be removed.
cally feasible. Re-    Because of good TOC re-
moval is nearly com-  moval, fewer are formed
plete when adsor-    during disinfection.
bent is fresh but
then breakthrough
to exhaustion occurs.
Bromine-containing
THMs adsorbed
better than chloro-
form. Loading is pro-
portional to influent
concentration and
desorption will occur
if the influent concen-
tration  drops.	
Continued

260   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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TABLE 114. (Continued)
Representative estimated east* for
378,000 m'/d (100 mgd) in C/m] (C/1000 gal)
Disinfection

Removes chlorine,
so must post-dis-
infect. Some reduc-
tion in disinfectant
demand





20% removal 50% removal
Louisville, K¥, tap water.
10mg/L 50 mg/L
0.74(2.8)* 3,4(13)*


80% removal
THM 'removal
150 mg/L
10.3 (39J*


Reference

Table 16
Figure 132


Ohio River water, precursor removal
9.5 mg/L 43 mg/L
Starting Starting
at at
1 ^mol/L 1 pmol/L
0.89(2.6)* 2.9(11}*
222 mg/L
Starting
at
1 jurnol/L
15 (57)'
Fig. 82
Fig. 132



Remarks

Some removal of
SQCs@ and T&OS
compounds. No
desorption with
decreasing concen-
tration because PAC
only used once.
Sludge disposal a
problem.

Buntington, WV, THM removal
Chlorine removed,
so post-disinfec-
tion required. Dis-_
infectant demand
is lower than when
TDC is removed.



7 min. 7 min.
EBCT§ EBCT§
7 wks 4 wks
react. react.
Sand Sand
replacem. replacem.
1.8(6.0)* 2.4(9.0)*


7 min.
EBCT§
2 wks
react.
Sand
replacem.
4,2 (16)*


Table 21
Ref. 18
Fig. 129






SOC@ & T&0# com-
pounds also removed.
Requires reactivation
or replacement. Com-
plete removal does
not last long. Passible
corrosion problems
if effluent TOC# con-
centration near zero.
Huntington, WV, precursor removal







7 min. 7 min.
EBCT§ EBCT§
5.5 wks 3 wks
react. react.
Sand Sand
replacam. replacem.
1.9(7.1)* 2.9(11)*
7 min.
EBCT§
1 wk
react.
Sand
replacem.
7.4 (28)*
Table 42
Ref. 18
Fig. 129











                          Section XI. Summary of Treatment Considerations  261

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TABLE 114. (Continued)
Iriitmtnt
Cltrificition
Br
Coagulation,
Sidimtntition,
Filtration



Precursor
Good removal is feasible. If
reaction with free chlorine is
fast, delaying chlorination to
, after clarification will permit
more removal. More removal
will occur at lower pH but the
reaction between free chlorine
and precursor will be slower.
TrihalomelhariBs Other Byproducts
No effect. Nona formed by the process
and some may be removed.
Because of TOO removal.
fewer are formed later
during disinfection. Some
will contain halogen if free
chlorine or chlorine dioxide
is used.
Clirificition
Br
Prtcipitttiv*
Sofa Ding
Good removal is technically
feasible. The faster reaction
rate between free chlorine and
precursor at higher pH should
result in additional benefit by
delaying chlorination.
No removal by
process. Higher pH
accelerates reac-
tion to form THMs.
None formed by the process.
Because of TOC removal,
fewer are formed during dis-
infection. Some will con-
tain halogen if free chlorine
or chlorine dioxide is used.
Clirificition
Br
Diroct
Filtration
Good removal is technically No effect.
feasible. THM concentrations
will be lower if chlorination is
delayed to after the process,
None formed by the process.
Because of TOC removal,
fewer are formed during dis-
infection. Some will con-
tain halogen if free chlorine
or chlorine dioxide is used.
 *M EOid a»* reufijlrf ia iws figmlieini figures,
 ffett.it fwctm Kittsval it thai location.
 "AAV * Air to Wilcr Ratio {Volume /Volume!
 Rt&O * TlStl and Ode»
f£BCf * Imp!? 8f d CofiiKt lime (imply 8e
-------
TABLE 114. (Continued)
Representative estimated cost* tor

Disinfection

Disinfectant
demand lower if
disinfection is
delayed.






Effectiveness of
free chlorine
reduced at higher
pH. Disinfectant
demand will be
lower if disinfec-
tion delayed.



378,000 mVd
20% removal

Wheeling,
WV
16%f
Lime =
16 mg/L
Ferric
Sulfate =
8 mg/L
4.0 (15)*

Jefferson
Parish, LA
16-25%f
lime =
60 mg/L
Cationk
polymer =
4 mg/L

5.8 (22)*
(100 mgd) in C/m3 (C/1000 gal)
50% removal 80% removal
Precursor removal
Fox Chapel, Not
PA achieved
49% f
Alum =
27 mg/L
Lime =
17 mfl/L

4.0 (1S>*
Precursor removal
Daytona Not
Beach, FL achieved
41%f
Lime =
225 mg/L
Alum =
25 mg/L
Polymer =
0.1 mj/L
5.6(21)«
Reference

Fig. 59
Ref. 18;
Table 27
Ref. 18
Fig. 126





Table 32
Ref. 14
Fig. 127







Remarks

Sludge disposal
problem. Iron salts
may be somewhat
better than alum.






Sludge disposal a
problem.








Bridgeport, CT, precursor removal
Disinfectant
demand lower if
disinfection fallows
clarification.


'AH costs are rounded let ft
Not
determined




ra significant figures.
36-54%f Not
Alum = achieved
21 mg/L
Polymer =
0.1 mj/L
2.6 (10)"

Table 35
Ref. 91
Fig. 125




Little sludge pro-
duced. May require
polymers.




 fActual percent removal at that location,
 "A/W = Aft to Water Ratio (Volume/Velum e)
 0T&Q - Tam and Odor
 @SGC = Synthetic Organic Contaminants
 §ESCT - irapty Btd Ccntic! Time (Empty Bed vdume divided fey fiow rate)
 jtTQC - Total Dfoanic Carbon
                                   Section XI, Sum/nary of Treatment Considerations  283

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the distribution system would be required so that the average concentration of
trihalomethanes in samples collected throughout the distribution system would be
less than 0,10 mg/ L, Because much of the source water precursor has been converted
into trihalomethanes prior to leaving the treatment plant in this example (i.e., the
InstTHM concentration in the finished water vtasQ.IS mgl L with an increase of 0,05
mg/ L in the distribution system),  aeration could be employed to remove these
trihalomethanes. According to Table 114, a 20:1 air to water ratio for a diffused-air
system, or a 32:1 air to water ratio for a tower aeration system, achieved 80 percent
removal of the InstTHM at one location. This would produce an expected average
InstTH M concentration of 0.03 mg/ L leaving the plant [0.15-{0.8)(0.15)] = 0.03 and
0,08 mg/ L (0.03 + 0.05) in the distribution system, less than the trihalomethane
MCL.J An estimated added cost for these two systems would be 3.7
-------
aeration towers, according to Table 114, using data from one location. The added
cost  for these two unit processes for this size treatment plant would be 1.8e/m'
(6.9c/ 1000 gal) (Figure 120) and 0,90
-------
Decisions as to which processes to study on a pilot-plant basis at a given location
should take all of these factors into account, but the least expensive treatment, ozone
oxidation, would be the first choice.

   4) 37S,000-mi/(J  (JOO-mgd)  Surface   Water  Utility—THM  Concentration
     UxMCL:
   For the fourth example, a 378,QQO-m3/d (100-tngd) utility having a conventional
treatment plant, using a surface water source and producing an average InstTHM
concentration of 0.12 mg/ L in the distribution system, a decline in trihalomethane
precursor concent rat ion of only about 20 percent would be needed to bring the utility
into compliance. Under these circumstances,  techniques  producing a modest
removal   of  trihalomethane   precursor—improving  clarification,  moving  the
chlorination point,  adjusting  pH,  or adding some oxidant—should result in an
acceptable average  InstTHM concentration  in  the distribution  system at a very
modest cost (see Table 114).
  These examples show how water utility personnel, design engineers, and  Primacy
Agencies might compare options  when attempting to control the trihalomethane
concentration at a given location. With diligent  disinfection as the final treatment
step and proper surveillance of the distribution system, any of these processes can be
used for trihalomethane control with the knowledge that water with an acceptable
bacteriologic  quality  will  reach  the consumer's tap. Of course,  many  other
combinations of source water qualities, existing treatment processes, and treatment
options  can   occur.  This research  report  provides information  concerning
cost-effective treatment processes that can be considered by water utility personnel
design engineers, and Primacy Agencies to successfully control the concentration of
trihalomethanes in the Nation's drinking water while maintaining high bacteriologic
water quality at the consumer's tap.
266   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

-------
                             SECTION XII
 •.   •     ,           '       REFERENCES*
  I. Rook, J.J., "Formation of Haloforms During Chlorination of Natural Water,"
    Water Treatment and Examination, 23, 234-243 (Part 2, 1974).

  2. Bellar, T.A.,  Lichtenberg,  J.J.,  and  Kroner, R.C., "The Occurence of
    Qrganohalides  in Chlorinated Drinking  Water," JA WWA, 66, 703-706
    (December. 1974),

  3. Federal Register, 44, No. 231, 68624-68707 (November 29, 1979); 45, No, 49,
    15542-15547 (March 11, 1980).

  4. "Manual of Treatment Techniques for Meeting the Interim Primary Drinking
    Water Regulations," EPA-600/8-77-005, USEPA, Cincinnati, OH (May 1977,
    Revised April  1978), NT1S Accession No. PB  2680294

  5. "Trihalomethane Implementation  Guidance,"  USEPA, Washington, DC, In
    press.

  6. "Industrial  Pollution  of the Lower  Mississippi   River  in  Louisiana,"
    Surveillance and Analysis Division, USEPA,  Region VI, Dallas, TX (April
    1972), Mimeo,  146 pp.

  7. Symons, J.M.,  Bellar,  T.A.,  Carswell,  J.K.,  DeMarco, J., Kropp, K.L.,
    Robeck, G.C., Seeger, D.R., Slocum, C.J., Smith, B.L., and Stevens, A.A.,
    "National  Organics Reconnaissance Survey  for Halogenated  Organics,"
    JA WWA, 67, 634-647 (November 1975).

  8. Region V Joint Federal/State Survey of Organics and Inorganics in Selected
    Water Supplies, USEPA, Chicago, 1L (June 1975), Unpublished.

  9. Federal Register, 41, No. 136, 28991-28998 (July 14,  1976).

 10. Federal Register, 43, No. 28, 5756-5780 (February 9, 1978).

 11, Federal Register, 43, No. 130, 29135-29150 (July 6, 1978).

 12. Pfaender,  F.K., Jonas,  R.B., Stevens, A.A.,  Moore, L., and Mass, J.R.,
    "Evaluation of Direct Aqueous Injection Method for Chloroform Analysis,"
    Environmental Science and Technology, 12, 438-441 (April 1978).
 13. Dressman, R.C., Stevens, A.A.,  Fair,  J., and Smith, B., "Comparison of
    Methods  for   Determination of  Trihalomethanes   in  Drinking  Water,"
    JA WWA, 71, 392-396 (July 1979).

 14, Final Report,  USEPA-DWRD Project CR-804571  "Fixed Bed Granular
    Activated Carbon Treatment  for  Organic Removal," Jefferson  Parish, LA
    (1976-1980), In press.
 15. Stevens, A.A., Slocum, C.J., Seeger, D.R., and Robeck, G.G.,"Chlorination
    of Organics in  Drinking Water," JA WWA, 68, 615-620 (November 1976).
•Unpublished reports and sponsored project information available from Director. Drinking Water Research Division. Mu-
 nicipal Environmental Research Laboratory. USEPA. 26 W. Si. Clair St.. Cincinnati. OH 45268,
*NT!S National Technical Information Service. Springfield. VA 22161.


                                                Section XII. References  267

-------
16. Stevens, A.A., "Formation  of Non-Polar Organo-Chloro Compounds as
    Byproducts  of  Chlorination," In: Proceedings -  Oxidation Techniques in
    Drinking Water Treatment, September 11-13, 1978, Karlsruhe, F.R.G., EPA-
    570/9-79020, USEPA, Washington, DC (1979) pp.  145-160, NT1S Accession
    No. PB3013I3/AS.

17. Stevens,  A.A.,  and  Symons, J.M.,  "Formation  and  Measurement  of
    Trihalomethanes in Drinking Water," In: Proceedings - Control of Organic
    Chemical Contaminants in Drinking Water, 1978,1979, USEPA, Washington,
    DC, In press.

18. Ohio River Valley Water Sanitation Commission, "Water Treatment Process
    Modifications for Trihaiomethane Control and Organic Substances in the
    Ohio River," EPA-600/2-80-028, USEPA, Cincinnati,  OH (March 1980),
    NTIS Accession No. PB 81-301222.

19. Bunn, W.W., Haas, B.B., Deane, E.R., and Kleopfer, R.D., "Formation of
    Trihalomethanes by Chlorination  of Surface Water," Environmental Letters,
    70,205(1975).

20, Lange, A.A., and Kawezynski, E., "Controlling Organies-The Contra Costa
    County Water District Experience,"./^ WWA, 70, 653-659 (November 1978).

21. Rook, J.J., "Chlorination Reactions of  Fulvic Acids in  Natural Waters,"
    Environmental Science and Technology, II, 478-482 (May 1978).

22. Christman, R.F., "Chlorination of Aquatic Humic Acids," EPA 600/2-81-016,
    Final Report for USEPA-DWRD Project - R-804430, USEPA, Cincinnati,
    OH (1981), NTIS Accession No. PB 81-161952.

23. Kajino,  M.,  and  Yagi,  M., "Formation  of  Trihalomethanes During
    Chlorination and Determination of Halogenated Hydrocarbons in Drinking
    Water," In: Hydrocarbons and Haiogenated Hydrocarbons in the Aquatic
    Environment, Afghan, B.K., and Mackay, D., Eds., Plenum Publishing Corp.
    (1980), p. 491.

24. Trussell, R.R.,  and  Umphres, M.D., "The Formation of Trihalomethanes,"
    JAWWA, 70, 604-612 (November 1978).

25. Trussell, R.R., "Factors Influencing the Formation of Trihalomethanes," In:
    Organics in  Domestic Water Supplies,  Proceedings, California - Nevada
    Section Forum, American Water Works Association, Palo Alto,  CA (April 12,
    1978).

26. Rook, J.J., "Haloforms in Drinking Water," JA WWA, 68,  168-172 (March
    1976).

27. Kavanaugh,  M.C.,  Trussell, A.R.,  Cromer,  J., and Trussell, R.R.,  "An
    Empirical Kinetic Model of Trihaiomethane Formation: Applications to Meet
    the Proposed THM Standard," JA WWA, 72, 578-582 (October 1980).

28. Nicholson, A.A., Meresz, O., and Lemyk,  B., "Determination of Free and
    Total Potential Haloforms in Drinking  Water," Analytical Chemistry, 49,
    814-819 (May 1977).

29. Stevens, A.A.,  and Symons, J.M., "Measurement of Trihaiomethane and
    Precursor Concentration  Changes Occurring During Water Treatment and
    Distribution," JA WWA, 69, 546-554 (October 1977).

268  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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30.  Final Report on USEPA-DWRD  Project CR805433, "Feasibility Study of
    Granular Activated Carbon Adsorption on On-Site Reactivation," Cincinnati,
    OH (1977-1981), In press.

31.  Wood,  P.R.,  Gervers, J.A.,  Waddell, D.H., and Kaplan,  L., "Removing
    Potential Organic Carcinogens and Precursors from Drinking Water," EPA
    600/2-80-130a, Final Report for USEPA-DWRD Project R804521, USEPA,
    Cincinnati, OH (1980), NTIS  Accession No.  PB 81-107146.

32.  Love, O.T., Jr., Carswell, J.K., Stevens, A.A., Sorg, T.J., Logsdon, G.S., and
    Symons, J.M., Appendix IV "Preliminary Results of Pilot Plants to Remove
    Water Contaminants," In: Preliminary Assessment of Suspected Carcinogens
    in  Drinking  Water  -  Interim  Report  to Congress, USEPA  Report,
    Washington, DC, (June 1975), Unpublished.

33.  Love, O.T., Jr., Carswell, J. K., Stevens, A.A., and Symons, J. M., "Treatment
    of  Drinking  Water for Prevention and  Removal of  Halogenated Organic
    Compounds  (An  EPA Progress  Report),"  Presented at the  95th Annual
    Conference of the American Water Works  Association, June 8-15,  1975,
    Minneapolis, MM.

34.  Love, O.T., Jr., Carswell, J.K., Stevens, A.A., and Symons, J.M., "Pilot Plant
    Studies and  Measurement  of Organics,"  Presented at Third Water Quality
    Technology Conference, American Water  Works Association, December 8-9,
    1975, Atlanta, GA.

35.  Symons, J.M., "Interim Treatment  Guide  for the Control of Chloroform and
    Other Trihalomethanes," USEPA, Cincinnati, OH, 48 pp.  + 4 Appendices
    (June 1976),  Unpublished.

36.  Symons,  J.M.,  "Utilization  of Various Treatment  Unit  Processes  and
    Treatment Modifications  for Trihalomethane Control," In: Proceedings -
    Control of Organic Chemical Contaminants in Drinking  Water, 1978,  1979,
    USEPA, Washington,  DC, In press.

37.  Basic Manual of Application and Laboratory Ozonalion Techniques, p. 21,
    The Welsbach Corporation, 3340 Stokley Street, Philadelphia, PA.

38.  Palin, AT., "Methods  for the Determination  in Water of Free and Combined
    Available Chlorine,  Chlorine  Dioxide and Chlorite,  Bromine, Iodine and
    Ozone Using Diethyl-/?-phenylene Diamine (DPD)," J. Inst.  Water Engr., 21,
    537 (August  1967).

39.  Miltner, R., "The Effect of Chlorine Dioxide on Trihalomethanes in Drinking
    Water," M.S. Thesis, University of Cincinnati, Cincinnati, OH (August 1976).

40.  Glaze, W.H., Peyton, G.R., Huang, F.Y., Burleson, J.L.Jones, P.C., Prengle,
    H.W., Nail, A.E., and Joshi, D.S., "Oxidation of Water Supply Refractory
    Species by Ozone with Ultra-Violet Radiation," EPA 600/2-80-110,  Final
    Report for USEPA-DWRD  Project  R-804640, USEPA, Cincinnati, OH,
    (1980),  NTIS Accession No. PB 81-107104.

41.  "Innovative  and  Alternative  Technology  Assessment  Manual (Draft),"
    EPA430/9-78-009, USEPA, Cincinnati, OH (1978). NTIS Accession No. PB
    81103277.

42.  Dilling, W.L., Tefertilier, N.B., and Kallos,  G.J., "Evaporation Rates and
    Reactivities  of  Methylene Chloride, Chloroform,  1,1,1-Trichloroethane,

                                               Section XII. References 269

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    Trichloroethylene, Tetrachloroethylene and Other Chlorinated Compounds in
    Dilute  Solutions," Environmental  Science  and  Technology,  9,  833-838
    (September 1975).

43, McCarty, P.L., "Organics in Water - An Engineering Challenge," Jour. Env,
    Engr. Div., ASCE, 106, 1-17 (February  1980).

44. Neely, W.B., Blau, G.E., and Alfrey, T., Jr., "Mathematical Models Predict
    Concentration - Time Profiles Resulting from Chemical Spills in a River,"
    Environmental Science and  Technology, 10, 72—76 (January 1976).

45. Singley, J,E., Ervin, A.L., and Williamson,  D.F., "Aeration (Plus Resins)
    Doing  Job  Removing  TOC," Water  and Sewage Works,  126,  100-102
    (September 1979).

46. Kavanaugh, M.C, and  Trussell, R.R., "Design of Air Stripping Towers to
    Remove Volatile Contaminants from Drinking Water," JA WWA, 72,684-692
    (December 1980).

47. Weil, J.B., "Aeration and Powdered Activated Carbon Adsorption for the
    Removal of Trihalomethanes from Drinking Water," Master of Engineering
    Thesis, University of Louisville, Louisville, K.Y (December 1979).

48. Houcl, N.,  Pearson, F.H., and Selleck, R.E., "Air Stripping of Chloroform
    from Water," Jour. Env. Eng. Div.,  ASCE, 105, 777-781 (August 1979).

49. Wood,  P.R., Curtis, F.W., Jr., Harween, R.F., and Lang, R.F., "Removal of
    Organics from Water by Aeration," Presented at the 101st Annual Conference
    of the American Water Works Association, June 7-11, 1981, St. Louis, MO.

50. SingSey, J.E., Ervin, A.L., Mangone,  M.A.,  Allan, J.M., and Land,  H.H,,
    "Trace  Organics  Removal  by Air Stripping," American  Water Works
    Association  Research  Foundation,  Denver,  CO (May 1980)  120 pp. +•
    Appendix.

51. Dobbs, R.A., and Cohen, J.M., "Carbon Adsorption Isotherms for  Toxic
    Organics," EPA-600/8-80-023, USEPA, Cincinnati, OH (April 1980),322pp.,
    NTIS Accession No. PB 80-197320.

52. Hoehn,  R.C.,  Randall, C.W.,  Groode,  R.P.,  and Shaffer,  P.T.B.,
    "Chlorination and Water Treatment  for Minimizing Trihalomethanes in
    Drinking Water," In: Water  Chlorination: Environmental Impact and Health
    Effects, Vol II, Jolley, R.L., Gorchev, H., and Hamilton, H.D., Jr., Eds,, Ann
    Arbor Science Publishers, Inc., Ann Arbor, MI (1978) p. 519-535.

53. McGuire, M.J., Suffet, I.H., and Radziul, J.V., "Assessment of Unit Processes
    for  the  Removal  of Trace Organic Compounds from Drinking  Water,"
    JAWWA,  70, 565-572 (October 1978).

54. Singley, J.E., Beaudet, B.A., and  Ervin, A.L., "Use of Powdered Activated
    Carbon  for Removal  of Specific Organic Compounds," In: Proceedings
    A WWA Seminar - Controlling Organics in  Drinking Water, 1979 Annual
    Conference, San Francisco,  CA,  June  24, 1979, American  Water Works
    Association, Denver, CO (1979), 15  pp.

55. Cams,  K.E., and  Stinson,  K..B.,  "Trihalomethane Experiences, East Bay
    Municipal  Utility District," JA WWA, 70, 637-644 (November 1978).


270  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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56.  Feige, M.A., Click, E.M., Munch, J.W., Munch,  D.J., Naschang, R.L., and
    Brass, H.J., "Potential Contaminants Introduced into Water Supplies by the
    Use of Coagulant Aids," In:  Water CMorinaiion: Environmental Impact and
    Health Effects, Vol. Ill, Jolley, R.L., Brungs, W.A. and Cumming, R.B., Eds,,
    Ann Arbor Science Publishers, Inc. Ann Arbor, Ml (1980) p. 789-802.

57.  Lukchis, G.M., "Adsorption Systems, Part  I, Design by Mass-Transfer-Zone
    Concept," Chemical Engineering, 80,  111 (June II, 1973).

58.  Yohe, T.L.,  and Suffet,  I.H., "Specific Removals by Granular Activated
    Carbon Pilot Contactors," In: Proceedings - 1979 Annual Conference ofihe
    American Water Works Association, San Francisco, CA., June 24-29,  1979, p.
 .   553-577, American Water Works Association, Denver, CO  (1979).

59.  Wood, P.R., and DeMarco, J., "Effectiveness of Various Adsorbents in
    Removing Organic Compounds from Water - Part 1, Removing Purgeable
    Halogenated Organics," In: Activated Carbon  Adsorption of Organics from
    the Aqueous Phase, Vol. II, McGuire, M.J., and Suffet, I.H.,  Eds., Ann Arbor
    Science Publishers, Inc., Ann Arbor,  Ml (1980) p. 85-114.

60.  Brodtmann,  N.V., Jr., and DeMarco, J., "Critical Study  of  Large-Scale
    Granular Activated   Carbon Filter  Units for the Removal  of  Organic
    Substances  from Drinking  Water," In: Activated Carbon Adsorption of
    Organics from the Aqueous  Phase, Vol. II, McGuire, M.J., and Suffet, I.H.,
    Eds., Ann Arbor Science Publishers, Inc., Ann Arbor, Ml (1980) p. 179-222.

61.  DeMarco,  J., and Brodtmann, N.V., Jr., "Prediction of Full  Scale Plant
    Performance from Pilot Columns," In: Proceedings-Symposium on Practical
    Application of Adsorption Techniques in Drinking Water Treatment, Reston,
    VA, April 30-May 2,  1979, USEPA, Washington, DC, In press.

62.  Miller, R., "Treatment of Ohio River Water," In: Proceedings-Symposium on
    Practical Application  of  Adsorption  Techniques  in  Drinking  Water
    Treatment, Reston, VA, April 30-May 2, 1979, USEPA, Washington, DC, In
    press.

63.  Final  Report on  USEPA-DWRD  Project CR804902, "Use  of Chlorine
    Dioxide and Granular Activated Carbon for Organic Removal," Evansville, IN
    (1976-1981), In press.

64.  O'Connor, J.T., Badorek, D., and Thiem,  L., "Removal of Trace Organics
    from Drinking  Water Using Activated Carbon and Polymeric Adsorbents,"
    Vol. 2, Final Report,  USEPA-DWRD Grant No.  R-804433, Cincinnati, OH
    (1980),  Available from  American Water Works  Association  Research
    Foundation, Denver,  CO.

65, Final  Report on USEPA-DWRD Project 68-03-2496 "Effect of Reactivation
    on the  Performance of Granular  Activated Carbon," Little  Falls, NJ
    (1976-1980), In press.

66.  Blanck,  C.A., "Trihalomethane Reduction in Operating Water Treatment
    Plants," JA WWA, 71, 525-528 (September 1979).

67.  DeMarco, J., and Wood, P., "Design Data for Organic Removal by Carbon
    Beds," In: Proceedings -National Conference on Environmental Engineering.
    American Society of Civil Engineers, Kansas City, MO, July  10-12,  1978,
    American Society of Civil Engineers, New  York, NY (1979).


                                               Section XII. References 271

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68. Hutchins,  R.A.,  "New Method  Simplifies  Design  of Activated  Carbon
    System," Chemical Engineering, 80,  133-138 (August 1973).

69. Ruggiero, D.D., and Ausubel, R., "Removal of Organic Contaminants from
    Drinking Water Supply at Glen Cove, N.Y. - Phase 1," EPA-600/2-80-I98,
    USEPA, Cincinnati,  OH (1980), NTIS Accession No. PB 81-115040.

70. Dressman,  R.C.,  Najar, B.A., and Redzikowski, R., "The Analysis of
    Organohalides (OX) in Water as a Group Parameter,"  In: Proceedings —
    Seventh Water Quality Technology Conference, Philadelphia, PA, December
    9-12, 1979, p. 69-92, American Water Works Association, Denver, CO(1980).

71. Bull, R.J., "Health Effects of Alternate Disinfectants and Their Reaction
    Products," JAWWA, 72, 299-303 (May 1980).

72. Committee  Report,  "Organic Removal by  Coagulation:  A  Review  and
    Research Needs," JA WWA, 71, 588-603 (October 1979).

73. Hall,  E.S., and  Packham,   R.F.,  "Coagulation of Organic Color with
    Hydrolyzing Coagulants," JA  WWA, 57, 1149-1166 (September 1976).

74. Narkis, N., and Rebhun, M., "Stoichoimetric Relationships Between Humic
    and Fulvic Acids and Flocculants," JA WWA, 69, 325-328 (June 1977).

75, Edzwald, J.K., Haft, J.D., and Boak, J.W.,  "Polymer Coagulation of Humic
    Acid Waters," Jour. Env. Eng. Div., ASCE, 103, 989-1000 (December 1977).

76. Inhoffer, W.R., "Use of Granular Activated Carbon at Passaic Valley Water
    Commission," In: Proceedings - Third Water Quality Technology Conference,
    Atlanta, GA,  December 8-9, 1975, American Water Works Association,
    Denver, CO (1976).

77. Kavanaugh,  M.C.,  "Modified Coagulation  for  Improved Removal  of
    Trihalomethane Precursors,"./,'! WWA,  70,  613-620 (November 1978).

78. Semmens,  M.J.,  and  Field,  T.K., "Coagulation: Experiences in Organic
    Removal," JA WWA, 72, 476-483 (August 1980).

79. Babcock, D.B., and Singer, P.C., "Chlorination and Coagulation of Humic
    and Fulvic Acids," JA WWA,  71, 149-152 (March 1979).

80. Cohen, R.S., Hwang, C.J., and Krasner, S.W., "Controlling Organics: The
    Metropolitan Water District of Southern California Experience," JA WWA,
    70, 647-652 (November 1978).

81. DiFilippo, J.D., Copeland, L.G., and Peil, K.M., "Evaluation of Powdered
    Activated Carbon for the Removal of Trace Organics at New Orleans, LA,"
    EPA 600/2-81-027,  Final Report on  USEPA-DWRD  Project R804404,
    USEPA, Cincinnati,  OH (1981), NTIS Accession No. PB 81-161853.


82. Bolton, C. M., "Cincinnati Research in Organics.'V^ WWA, 69,405-406, (July
    1977).

83. Kinman, R.N., and Rickabaugh, J., "Study  of In-Plant  Modifications  for
    Removal of Trace Organics from Cincinnati Drinking Water," University of
    Cincinnati, Cincinnati, OH (July 30, 1976).

272  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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84,  Young, J.S., and  Singer, P.C.,  "Chloroform Formation  in  Public Water
    Supplies: A Case Study," JA WWA, 71, 87-95 (February 1979).

85,  Singley, J.E., Beaudet, B.A., Brodeur, T.P., Thurrott, J.T,, and Fisher, M.E.,
    "Minimizing Trihalomethane Formation in a Softening Plant," Final Report,
    EPA Contract No. CA6992948-A, USEPA-DWRD, Cincinnati, OH (1976),
    Unpublished.

86.  Brodeur, T.P., Singley, J.E., Beaudet, B.A., Thurrott, J.T., and Frey, E.,"The
    Reduction  of Trihalomethane Precursor Compounds  by the Addition  of
    Coagulants and Polymers," Final Report USEPA-DWRD Contract CI770901
    Cincinnati, OH (1977), Unpublished.

87.  Wood,  P.R., and  DeMarco, J., "Effectiveness of Various Adsorbents  in
    Removing  Organic Compounds  from Water  -  Part II - Removing Total
    Organic Carbon and Trihalomethane Precursor Substances," In: Activated
    Carbon Adsorption of Organics from the Aqueous Phase, Vol. II, McGuire,
    M.J., and Suffet, I.H., Eds., Ann Arbor Science Publishers, Inc., Ann Arbor,
    MI (1980)  p. 115-136.

88.  Edzwald,   J.K., "A Preliminary  Feasibility  Study of the  Removal  of
    Trihalomethane Precursors by Direct Filtration," USEPA-DWRD, Cincin-
    nati,  OH (February 1979), Unpublished.

89.  Snoeyink,  V.L.,  McCreary,  J.J.,  and  Murin, C.J.,  "Activated  Carbon
    Adsorption of Trace Organic Compounds,"  EPA-600/2-77-223,  USEPA-
    DWRD, Cincinnati, OH (1977), NTIS Accession No. PB 279253/AS.

90.  McBride, D.G., "Controlling Organics: The Los Angeles Department of Water
    and Power Experience," JA WWA,  70, 644-646 (November 1978).

91.  Bryant, E.A., and  Yapijakis, C.,  "Ozonation-Diatotnite Filtration  Removes
    Color and  Turbidity,"  Water and Sewage  Works, 124, Part  I,  96-101
    (September 1977),  Part 2, 94-98 (October 1977).

92,  Barnett, R.H., and Trussell,  A.R., "Controlling  Organics: The Casitas
    Municipal  Water District Experience," JAWWA, 70,  660-664  (November
    1978).

93.  Hoehn, R.C., Barnes, D.B., Thompson, B.C., Randall,  C.W., Gizzard, T.J.,
    and Shaffter,  P.T.B., "Algae as Sources of  Trihalomethane  Precursors,"
    JA WWA,  72, 344-350 (June 1980).

94.  Briley,  K.F.,  Williams,  R.F.,  Longley, K.E., and Sorber,  C.A., "The
    Trihalomethane Production from Algal Precursors," In:  Water Chlorination:
    Environmental Impact and Health  Effects,  Vol. Ill, Jolley, R.L.,  Brungs,
    W.A., and Gumming, R.B., Eds., Ann Arbor Science Publishers, Inc., Ann
    Arbor,  MI (1980) p. 117-130,

95.  Riley, T.L., Mancy, K. H., and Boettner, E.A., "The Effect of Preozonation on
    Chloroform Production in the Chlorine  Disinfection  Process," In: Water
    Chlorination: Environmental Impact and Health Effects, Vol. H", Jolley, R.L.,
    Gorchev, H., and Hamilton, H.D., Jr., Eds., Ann Arbor Science Publishers,
    Inc.,  Ann Arbor, MI (1978) p. 593-603.

96,  Granstrom, M.L., and Lee, G.F., "Generation and Use of Chlorine Dioxide in
    Water Treatment," JA WWA, 50, 1453-1466 (November 1958).


                                              Section  XII, References  273

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 97.  Singer, P.C., Borchardt, J.H., and Colthurst, J.M., "The Effects of Potassium
     Permanganate  Pretreatment  on Trihalomethane  Formation in  Drinking
     Water," JA WWA, 72, 573-578 (October 1980).

 98.  Fung, M.C.,  "Reduction of Haloforms in Drinking Water Supplies," Report
     No. 69, Water  Technology Section,  Pollution Control  Branch,  Ontario
     Ministry of the Environment, Rexdale, Ontario, Canada (September 1978) 59
     pp.

 99.  Burton, B.D., and Siria,  J.W., "Hydrogen Peroxide  as  a  Treatment for
     Disinfection and Reduction of Trihalomethane Formation in Potable Waters,"
     Louisville Water Company, Louisville, KY (March 1978) 39 pp.

100.  Lykins, B.W., Jr.,  and DeMarco, J., "An Overview of the  Use of Powdered
     Activated  Carbon for Removal of Trace  Organics in Drinking  Water,"
     USEPA, Cincinnati,  Ohio, In press.

101.  Zogorski,  J.S.,  Allgeiver, G.D.,  and Mullins, R.L., Jr., "Removal  of
     Chloroform from Drinking Water," Research Report No. 111, University of
     Kentucky Water Resources Research Institute, Lexington,  KY (June 1978).

102.  Benedek,  A.,  "Simultaneous   Biodegradation  and   Activated  Carbon
     Adsorption - A Mechanistic Look,"  In:  Activated Carbon  Adsorption of
     Organics from the Aqueous Phase, Vol. 11, McGuire, M.J., and Suffet, I.H.,
     Eds., Ann  Arbor Science Publishers, Inc., Ann Arbor, Ml (1980) p. 273-321.

103.  USEPA-DWRD Project CR 805371 "Reactivation of Granular Activated
     Carbon Beds to Remove Organics," Manchester, NH (1977-1982).

104.  Symons, J.M., Carswell, J.K., DeMarco, J., and Love, O.T., Jr., "Removal of
     Organic Contaminants from Drinking  Water Using Techniques Other Than
     Granular Activated Carbon Alone - A Progress Report," In: Proceedings -
     Symposium on Practical Application of Adsorption Techniques in Drinking
     Water Treatment, Reston,  VA, April 30-May 2, 1979, USEPA, Washington,
     DC, In press.

105.  Frisch, N.W., and  Kunin, R., "Organic Fouling of Anion-Exchange  Resins,"
     JAWWA, 52, 875-887 (July I960).

106.  Rook, J.J., and Evans, S., "Removal of Trihalomethane  Precursors from
     Surface Waters Using Weak Base Resins,'V/l WWA, 71, 520-524 (September
     1979).

107.  Rice, R.G., "Biological  Activated  Carbon," In: Proceedings - Control of
     Organic Chemical Contaminants in Drinking Water,  1978,  1979, USEPA,
     Washington,  DC, In  press.

108.  Sontheimer,  H., Heilker, E., Jekel, M., Nolle, H., and Vollmer,  F.H., "The
     Muhlheim  Process,"  JA WWA, 70, 393-396 (July 1978).

109.  Eberhardt, M.,  Madsen,  S., and  Sontheimer, H.,  "Untersuchungen  zur
     Verwendung  biologish arbeitender AJctivkohlefilter bei der Trinkwasserauf-
     bereitung"  Engler-Bunte-lnstitut der Universitat Karlsruhe, Heft 7, Karlsruhe,
     F.R.G. (1974) 86 pp.

110.  USEPA-DWRD Project  CR806256 "Treatment of Water for Removal of
     Organics with Ozone and Granular Activated Carbon," Philadelphia, PA
     (1978-1982).

274  Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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III.  USEPA-DWRD Project CR806I57 "Removal of Trihalomethane Precursor
     Using Ozone Combined with Granular Activated Carbon," Shreveport, LA
     (1978-1981).

112.  USEPA-DWRD Project CR806890 "Removal of Organic Substances Which
     Are Potential Carcinogens Either Originally Present  in Ground Water or
     Generated  During the Purification Process," Miami, FL (1978-1981).

113.  "Oxidation Techniques in  Drinking Water Treatment," September 11-13,
     1978, Karlsruhe, F.R.G., EPA-570/9-79-020, USEPA, Washington, DC(1979)
     765 pp., NTIS Accession No. PB 301313/AS.

114.  Rudek, R,, "Untersuchungen zum Einfluss von  Naturlichen Organischen
     Wassennhaltsstoffen auf die Vorgange bei der Korrosion in Trinkwasserin-
     staliationen."  In:  Untersuchungen zum  Einfluss naturlichen  organischen
     Wasserinhaltsstoffe auf die Ausbildung und Korrosionsschutzwirkung  von
     Deckschichten in Trinkwasserinstallaiionen, Teil 111, Dissertation Rudek, Heft
     14 der Veroffentlichungen des  Bereichs und Lehrstuhls  fur Wasserchemie,
     Engler-Bunte-lnstitut des Universitat Karlsruhe. Zusammengestellt von Prof.
     Dr. H. Sontheirher und Dr. R.  Rudek, Karlsruhe (1980).

115,-Symons, J.M., Carswell, J.K., Clark, R.M., Dorsey, P., Geldreich, E.E.,
     Heffernan, W.P., Hoff, J.C., Love, O.T., Jr., McCabe, L.J., and Stevens, A.A.,
     "Ozone, Chlorine  Dioxide and  Chloramines as Alternatives to Chlorine for
     Disinfection of'Drinking Water -State of the Art," USEPA, Cincinnati, OH,
     84 pp. (November 1977), Unpublished. Summary in: Water Chlorination,
     'Environmental'Impact and Health Effects, Vo! II, Jolley, R.L., Gorchev, H.,
     and Hamilton, D.H., Jr., Eds., Ann Arbor Science Publishers, Inc., Ann Arbor,
     Ml (1978)  p. 555-560.

116.  Scarpino,  P.V., Cronier, S.,  Zink, M.L., Brigano, F.A.O., and  Hoff, J.C.,
     "Effect of Particulates on Disinfection of Enteroviruses and Coliform Bacteria
     in  Water  by Chlorine  Dioxide,"  In: Proceedings -  Fifth Water  Quality
     technology Conference, Kansas City,  MO, December 4-7, 1977, Paper 2B-3,
     11 pp., American Water Works Association, Denver, CO (1978),

117.  Esposito, M.P., "The Inactivation of Viruses in Water by Dichloramine,''M.S,
     Thesis, University  of Cincinnati, Cincinnati, OH (1944).

118.  Walsh,  D.S., Buck,  C.E., and  Sproul, O.J., "Ozone  Inactivation  of Floe
     Associated Viruses and Bacteria," Jour. Env, Eng. Div., ASCE, 106, 711-726
     (August 1980).

119.  Engelbrecht,  R.S.,  Weber,   M.J,,   Salter, B.B.,  and  Schmidt,  C.A.,
     "Comparative Inactivation of Viruses by Chlorine," Applied and Environment
     tal Microbiology, 40, 249-256 (1980).

120.  White, G.C., "Handbook  of Chlorination," Van Nostrand Reinhold,  New
     York, NY (1972) 744pp.

121.  Benarde, M.A., Israel, B.M,,'Olivieri, V.O.,and Granstrom, M.L.," Efficiency
     of Chlorine Dioxide as a Bactericide," Applied Microbiology,' 13, 776-780
     (1965)1                 '                            _

122.  Scarpino, P.V., Berg, G., Chang,  S.L., Dahling,  D., and  Lucas, M.L., "A
     Comparative Study of the Inactivation of Virus in Water by Chlorine," Water
     Research, 7, 959-965 (1972).


                                                Section XII. References  275

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123.  Sharp,  D.G., Young, D.C., Floyd, R., and Johnson, J.D., "Effect of Ionic
     Environment on the Inactivation of Poliovirus in Water by Chlorine," Applied
     and Environmental Microbiology, 39, 530-534 (1980).

124.  Jensen, H., Thomas, K.., and Sharp, D.G., "Inactivation of Coxsackie B3 and
     B5 Viruses in Water by Chlorine," Applied and Environmental Microbiology,
     40,633-640(1980).

125.  Sharp,  D.G., and Leong, J., "Inactivation of Poliovirus I (Brunhilde) Single
     Particles by Chlorine in Water," Applied and Environmental Microbiology,
     40,381-385(1980).

126.  Heather,  R.C.,  "The Bactericidal Effect of Ammonia-Chlorine Treatment,
     Residual Chloramine and Free Residual Chlorine," Journal of the Institute of
     Water Engineers, 3, 507-514 (1949).

127.  Houghton, G.U., "Experiments as to the Effects of pHand Organic Content in
     the Arnmonia-Chlorine Treatment of Water, "Journal of the Institute of Water
     Engineers, 4, 434^44 (1950).

128.  Selleck, R.E.,  Saunier,  B.M.,  and  Collins,  H.F.,  "Kinetics of  Bacterial
     Deactivation with Chlorine," Jour. Env. Engr. Div.,  ASCE, 104, 1197-1212
     (December 1978).

129.  Hoff, J.C., "The Relationship of Turbidity to Disinfection of Potable Water,"
     In: Evaluation of the Microbiology Standards for Drinking Water, Hendricks,
     C.H., Ed., EPA-570/9-78-002, Washington, D.C. (1978), NTIS Accession No.
     PB 297119.

130.  Hijkal,  T.W.,  Wellings, P.M.,  LaRock, P.A., and Lewis, A.L., "Survival of
     Poliovirus Within  Organic  Solids  During  Chlorination," Applied and
     Environmental Microbiology, 38, 114-118 (1979).

131.  Foster,  D.M., Emerson,  M.A.,  Buck, C.E., Walsh, D.S., and Sproul, O.J.,
     "Ozone Inactivation  of  Cell- and Fecal-Associated Virus and Bacteria,"
     Journal of the Water Pollution Control Federation, 52, 2174-2184 (August
     1980).

132.  Tuepker, J.L., "Sampling and Analysis of Chloro-Organics in the Distribution
     System," In: Proceedings- Fourth Water Quality Technology Conference, San
     Diego,  CA,  December 6-7,  1976,  Paper 3A-4, American  Water  Works
     Association,~Denvcr, CO (1977).

133.  Duke, D.T., Siria, J.W., Burton, B.D., and Amundsen, D.W., Jr., "Control of
     Trihalomethanes in Drinking Water," JA WWA, 72, 470-476 (August 1980).

134.  Water Quality Research News,  No. 3, American Water Works  Association
     Research  Foundation, American Water Works Association, Denver, CO
     (December 1979).

135.  Hubbs, S.A., Guers,  M., and Siria, J., "Plant-Scale Examination and Control
     of a ClOi-Chloramination Process at the  Louisville Water Company," In:
     Water  Chlorination:  Environmental  Impact and Health  Effects,  Vol. Ill,
     Jolley, R.L.,  Brungs, W.A., and Gumming, R.B., Eds., Ann Arbor Science
     Publishers, Inc., Ann Arbor, MI (1980) p. 769-776.

136.  Brodtmann, N.V., Jr., Koffskey, W.E., and DeMarco, J., "Studies of the Use of
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275  Treatment Techniques for Controlling  Trihalomethanes in Drinking Water

-------
    Water," In:  Water Chlorination: Environmental impact and Health Effects,
    Vol. Ill, Jolley, R.L., Brungs, W.A., and Cummings, R.B., Eds.. Ann Arbor
    Science Publishers, Inc., Ann Arbor, Mi (1980) p. 777-788.

137. Norman.T.S., Harms, L.L.,and Looyenga, R.W.,"The UseofChloraminesto
    Prevent Trihalomethane Formation," JA WWA, 72,  176-180 (March 1980).

138. Williams,  R.F., Moore, B.E., Longley, K.E., and Sorber, C.A., "Reduction of
    Trihalomethane Production with Optimal Disinfection Through Alternative
    Disinfection Systems," In: Chemistry in  Water Reuse, Vol. 1., Cooper, W.C.,
    Ed., Ann  Arbor Science Publishers^ Inc., Ann Arbor, M! (1981) p. 477-500.

139. Siemak, R.C., Trussell, R.R., Trussell, A.R., and Umphres, M.D., "How to
    Reduce Trihalomethanes in  Drinking Water," Civil Engineering, 49, 49-50
    (February 1979).

140, Sontheimer, H., "Effectiveness of Granular  Activated Carbon for Organics
    Removal," In:  Proceedings  - 1978 Annual Conference, American Water
    Works Association, Atlantic City, N J.June 25-30, 1978, Paper 10-1, American
    Water Works Association, Denver, CO  (1979).

141. Miller, W.G., Rice, R.G., Robson, C.M., Scullin, R.L., Kfihn, W., and Wolf,
    H.,  "An  Assessment  of Ozone and Chlorine  Dioxide Technologies for
    Treatment of  Municipal  Water  Supplies," EPA 600/2-78-147,  USEPA,
    Cincinnati, OH (August 1978) 571 pp., NTIS Accession No. PB 285972/AS.

142. Augenstein, H.W., "Use of Chlorine Dioxide to Disinfect Water Supplies,"
    JAWWA, 66, 716-717 (December 1974).

143. Kuhn, W., and Sontheimer, H., "Treatment: Improvement or Deterioration of
    Water Quality," Presented at: Water Supply and Health, Noordwijkerhout,
    The Netherlands,  August 27-29, 1980.

144. Rickabaugh, J., and Kinman, R.N., "Trihalomethane Formation from Iodine
    and Chlorine Disinfection of Ohio  River Water," In:  Water  Chlorination:
    Environmental  Impact and Health Effects, Vol. II, Jolley, R.L., Gorchev, H.,
    and Hamilton,  R.D., Jr., Eds., Ann Arbor Science Publishers, Inc.,  Ann
    Arbor, Ml (1978) p. 583-591.

145. USEPA  Interoffice Memo,  "Use of Iodine for  Disinfection  of  Drinking
    Water," USEPA,  Washington, DC (February 20, 1973).

146. "Health  Effects of Drinking Water  Disinfectants  and  Disinfectant  By-
    Products," April 21-24, 1981, Cincinnati, OH, USEPA, Cincinnati, OH, In
    press.  '

147. Stieglitz,  L,, Roth,  W.,  Kuhn,  W.,  and  Leger,  W.,  "The  Behavior of
    Organohalides  in  the Treatment of Drinking Water," Vom Wasser,47, 347
    (1976).

148. Coleman, W.E.,  Lingg, R.D.,  Melton,  R.G., and  Kopfler,  F.C.,  "The
    Occurrence of Volatile Organics in Five Drinking Water Supplies Using Gas
    Chromatography/Mass  Spectrometry,"  In:  Identification and Analysis of
    Organic Pollutants in Water, Ann Arbor Science Publishers,  Inc., Ann Arbor,
    MI (1976) p. 305.

149. Trehy, M.L., an'd  Bieber, T.I,, "Effects of Commonly Used Water Treatment
    Processes on the Formation of THMs and DHANs," In: Proceedings - 1980

                                                Section XII.  References   277

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     Annual Conference American  Water Works Association, Atlanta, GA, June
     15-20, 1980, p. 125-138, American  Water Works Association, Denver, CO
     (1980).

150.  Suffet,   I.H.,  Brenner,  L,,  and  Silver,  B,, "Identification  of  1,1,1-
     Trichloroacetone  (1,1,1-Trichloropropanone)  in Two Drinking  Waters: A
     Known  Precursor  in  Haloform Reaction,"  Environmental  Science  and
     Technology, 10, 1273-1275 (December 1976).

151.  Seeger,  D.R.,  Slocum,  C.J.,  and  Stevens,  A.A.,  "G.C/MS Analysis of
     Purgeable  Contaminants in Source and Finished  Drinking Water," In:
     Proceedings — 26th Annual Conference  on Mass Spectrometry  and Allied
     Topics, St. Louis, MO, May 28-June 2 1978.

152.  Brass, H.J., Feige, M.A.,  Halloran, T., Mello, J.W., Munch, D., and Thomas,
     R.F., "The National Organic Monitoring Survey: Sampling and Analysis for
     Purgeable Organic Compounds," In: Drinking Water Quality Enhancement
     Through Source Protection, Ann Arbor Science Publishers Inc., Ann Arbor,
     Ml (1977), p. 393.

153.  Burtschell,  R.H.,  Rosen,  A.A., Middleton,  P.M., and  Ettinger,  M.B.,
     "Chlorine Derivatives of Phenol  Causing Taste and Odor," JA WWA, 51,
     205-214  (February 1959).

154.  Morris, J.C., "Formation of Halogenated Organlcs by Chlorination of Water
     Supplies,"   EPA-600/1-75-002,  USEPA,  Washington,  DC (1975),  NT1S
     Accession No. PB 24151 I/AS.

155.  Gordon, G.. Kieffer, R.G., and Rosenblatt, D.H., "The Chemistry of Chlorine
     Dioxide," In: Progress in  Inorganic Chemistry, IS, Lippard, S.J., Ed., Wiley —
     Interscience, New York, NY (1972) p. 201.

156.  Black, A.P., and Christman, R.F., "Chemical Characteristics of Fulvic Acids,"
     JA WWA, 55, 897-912 (July 1963).

157.  Stevens.  A. A., Seeger, D.R., and Slocum, C.J., "Products of Chlorine Dioxide
     Treatment of Organic Materials in Water," In: Proceedings- Ozone I Chlorine
     Dioxide  Oxidation Products of Organic Materials, Rice, R.G., and Cotruvo,
     J.A., Eds., Cincinnati, OH, November 17-19, 1976, Ozone Press International,
     Cleveland, OH (1978) p.  383-395.

158.  Christman,  R.F., and Ghassemi, M., "Chemical Nature of Organic  Color in
     Water," JA WWA, 58, 723-741 (June 1966).

159,  Dcnce,  C.W., Gupta,  M.K., and Sarkanen,  R.V.,  "Studies on Oxidative
     Delignification Mechanisms, Part 11. Reactions of Vanillyl Alcohol with
     Chlorine Dioxide and Sodium Chlorite," Tappi, 45, 29 (1962).

160.  Dcnce, C.W., and Sarkanen, K.V., "A Proposed Mechanism for the Acidic
     Chlorination of Softwood Lignin," Tappi, 43,  87 (1960).

161.  Glabisz, U.,"The Reactions of Chlorine Dioxide with Components of Phenolic
     Wastewaters - Summary,"  Monograph 44, Polytechnic University, Szczecin,
     Poland (1968).
278   Treatment Techniques for Controlling Trihalomethanes in Drinking Water

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162.  Miltner, R.J., "Measurement of Chlorine Dioxide and Related Products," In:
     Proceedings— Fourth Water Quality Technology Conference, San Diego,CA,
     December  6-7,  1976,  Paper 2A-5,  American Water Works Association,
     Denver, CO (1977).

163.  "The Chemistry.of Disinfectants in  Water: Reactions and Products," In:
     Drinking Water and Health, National Academy of Sciences, Washington, DC
     (1980),  p. 139-249.

164.  Schalekamp, M., "Experience  in Switzerland  with  Ozone, Particularly  in
     Connection with the Neutralization  of Hygenically Undesirable Elements
     Present in Water,"In: Proceedings-1977 Annual Conference American Water
     Works  Association, Anaheim, CA, May 8-13, 1977, Paper 17-4,  American
     Water Works Association, Denver, CO (1978).

165.  Sievers, R.E., Barkley, R.M., Eiceman, G.A., Shapiro, R.H.,  Walton, H.F.,
     Kolonko, K.J.,and Field, L.R., "Environmental Trace Analysis of Organics in
     Water by Glass Capillary Column Chromatography and Ancillary Techniques
     - Products of Ozonolysis," Journal of Chromatography, 142, 745-754 (1977).

166.  Simmon, V.F., and Spanggord, R.J., "The Effects of Ozonation Reactions in
     Water," SRI  International, Final Report on  Contract No. 68-01-2894, Vol. 1,
     USEPA, Washington, DC (March 1979), 213 pp.

167.  Simmon, V.F., Spanggord, R.J., Eckford, S.L.,and McClurg, V., "The Effects
     of Reactions  of Chlorine Dioxide in Water," SRI International, Final Report
     on Contract No. 68-01-2894, Vol. II, USEPA, Washington, DC (March 1979)
     157  pp. + Appendix.

168.  Shih, K.L., and Lederberg, J., "Chloramine  Mutagenesis in Bacillus subtilis,"
     Science, 192, 1I4I-1I43 (June 11, 1976).

169.  Eaton, J.W.,  Kolpin, C.F., and Swofford, H.S., "Chlorinated Urban Water: A
     Cause of Dialysis Induced Hemolytic Anemia, "Science, 18!, 463-464 (August
     3, 1973).

170.  Cummins, B.B., and Nash, H.D., "Microbiological Implications of Alternative
     Treatment," In: Proceedings - Sixth  Water  Quality Technology Conference,
     Louisville,  KY, December 3-6, 1978, Paper 2B-1, American Water Works
     Association,  Denver, CO (1979).

171.  Parsons, F., "Removing Potential Organic Carcinogens and Precursors from
     Drinking Water,  Appendix  B,  Preliminary  Reports of Bacterial  Study on
     Drinking Water,  Miami,  Florida," USEPA, Cincinnati,  OH,  53  pp.,
     Unpublished.

172.  Parsons, F., "Bacterial Populations in Granulated Activated Carbon Beds and
     Their  Effluents,"  USEPA,  Cincinnati, OH (January  10,  1980)  45  pp.,
     Unpublished.

173.  Allen, M.J.,  Taylor, R.H., and Geldreich,  E.E., "The Impact of Excessive
     Bacterial Populations on Coliform Methodology," In: Proceedings - Fourth
     Water Quality Technology Conference, San  Diego, CA, December 6-7, 1976,
     Paper 3B-4, American Water Works  Association, Denver, CO (1977).

174.  Geldreich,  E.E.,  Nash,  H.D.,  and  Spino, D.,  "Characterizing Bacterial
     Populations in Treated Water Supplies: A Progress Report," In: Proceedings
     Fifth Water  Quality Technology Conference, Kansas City, MO,  December

                                                Section XII. References  279

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     4-7,  1977, Paper 2B-5, American Water Works Association, Denver, CO
     (1978).

175. Reasoner, D.J., and Geldreich, E.E., "A New Mechanism for the Enumeration
     and Subculture of Bacteria  from Potable  Water," American  Society for
     Microbiology, Abstracts of the Annual Meeting, N-7, ISSN 0067-2777, May
     4-8, 1979, Los Angeles, CA.

176. van der Kooij, D., "Processes During Biological Oxidation  in Filters," In:
     Proceedings—Oxidation Techniques in Drinking Water Treatment, September
     11-13,  1978, Karlsruhe, F.R.G., EPA-570/9-79-020, USEPA, Washington,
     DC, p. 689-701 (1979), NTIS Accession No. PB 301313/AS.

177. Parsons, F., "Bacterial Populations of Granular Activated Carbon Columns
     and Sand Filters Used to Treat Unchlorinated Water,"  USEPA, Cincinnati,
     OH (November 15, 1979) 99 pp., Unpublished.

178. Hubbs, S.A., Amundsen, D., and Olthius, P.,  "Use of  Chlorine Dioxide,
     Chloramines,  and   Short-Term  Free  Chlorination  as  Alternative
     Disinfectants," JAWWA, 73, 97-101 (February 1981).

179. Geldreich, E.E., Allen, M.J.,  and Taylor, R.H., "Interferences to  Coliform
     Reduction in Potable Water  Supply," In: Evaluation of the Microbiology
     Standards for Drinking Water, Hendricks,  C.W., Ed., EPA-570/9-78-002,
     USEPA, Washington, DC (1978), NTIS Accession No.  PB 297119.

180. Snead,  M.C., Olivieri, V.O., Kruse, C.W., and Kawata, K., "Benefits of
     Maintaining a Chlorine Residual in Water Supply Systems," EPA-600/2-80-
     010, Final Report  for USEPA Project R-806074, USEPA, Cincinnati, OH
     (1980), NTIS Accession No. PB 81-110892.

181. Brodeur, T.P., Singley, J.E., and Thurrott, J.C., "Effects of a Change to Free
     Chlorine Residual at Daytona Beach," In: Proceedings- Fourth Water Quality
     Technology  Conference, San Diego, CA, December 6-7,  1976, Paper 3A-5,
     American Water Works Association, Denver, CO (1977).

182. Vendryes, J.H., "Experiences with the Use of Free Residual Chlorination in the
     Water Supply of the  City  of Kingston, Jamaica," In:  Proceedings AIDIS
     Congress of Washington.  D.C., (1962).

183. Buelow,  R.W.,  and  Walton, G., "Bacteriological  Quality vs.  Residual
     Chlorine," JA WWA, 63, 28-35 (January 1971).

184. Gumerman.   R.C.,  Gulp,  R.L.,  and  Hanson, S.P.,  "Estimating Water
     Treatment Costs: Volume 2 -Cost Curves Applicable to 1 to 200 mgd Plants,"
     EPA-600/2-79-162b. USEPA, Cincinnati, OH (August 1979), NTIS Accession
     No. PB 80-139827.

185. Clark, R.M., Guttman, D.L., Crawford, J.L., and Machisko, J.A., "The Cost
     of Removing Chloroform and Other Trihalomethanes from Drinking Water,"
     E PA-600/1-77-008, USEPA, Cincinnati, OH (March 1977), NTIS Accession
     No. PB264283/AS.
186. Logsdon,  G.S., Clark, R.M.,  and Tate, C.H., "Direct Filtration Treatment
     Plants: Costs and Capabilities," JAWWA, 69, 134-147 (March 1980).

187. Harms, L.L., "Formation and Removal of Halogenated  Hydrocarbons in
     Drinking Water," Final Report on Project R008128010, Region VIII, USEPA,
     Denver, CO (January  1977) 45 pp.
250  Treatment Techniques for Control/ing Trihalomethanes in Drinking Water

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188. Clark, R.M.,and Dorsey, P., "Influence of Operating Variables on the Cost of
    Treatment by GAC Adsorption," In: Proceedings - Symposium on Practical
    Application of Adsorption Techniques in Drinking Water Treatment, Reston,
    VA, April 30 - May 2, 1979, USEPA, Washington, DC, In press.

189. Gumerman,  R.C.,  Culp,  R.L., and Clark, R.M., "The Cost of Granular
    Activated Carbon Adsorption Treatment in the \J.S."JAWWA, 77,690-696
    (November 1979).

190. Clark, R.M.,and Dorsey, P., "The Costs of Compliance: An EPA Estimate for
    Organics Control," JA WWA, 72, 450-457 (August 1980).
                                               Section XII. References  281

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                             SECTION XIII
                              APPENDIX*

  Accordingly, Part 141. Title 40 of the Code of Federal Regulations is hereby
amended as follows:
   1. By amending § 141.2 to include the following new paragraphs (p) through (t):
§ 141.2 Definitions

  (p) "Halogen" means one of the chemical elements chlorine, bromine or iodine.
  (q) "Trihalomethane" (THM) means one of the family of organic compounds,
named as derivatives of methane, wherein three of the four hydrogen atoms in
methane are each substituted by a halogen atom in the molecular structure.
  (r) "Total trihalomethanes"(TTHM) means the sum of the concentration in milli-
grams per liter of the trihalomethane compounds (trichloromethane [chloroformjj
dibromochloromethane, bromodichloromethane and tribromomethane  [bromo-
form]), rounded to two significant figures.
  (s) "Maximum Total  Trihalomethane Potential (MTP)" means the maximum
concentration of total trihalomethanes produced in a given water containing a
disinfectant residual after 7 days at a temperature of 25°C or above.
  (t) "Disinfectant" means any oxidant,  including but not limited to chlorine,
chlorine dioxide, chloramines, and ozone added to water in any part of the treatment
or distribution  process,  that is intended to kill or inactivate pathogenic micro-
organisms.
  2. By revising § 141.6 to read as follows:
§ 141.6  Effective dates.
  (a) Except as provided in paragraph (b) of this section, the regulations set forth in
this part shall take effect on June 24, 1977.
  (b) The regulations for total trihalomethanes set forth in § 141.12(c) shall take
effect 2 years after the date of promulgation of these regulations for community
water systems serving 75,000 or more individuals, and 4 years after the date of
promulgation for communities serving 10,000 to 74,999 individuals.
  3. By revising the introductory paragraph and adding a new paragraph (c) in
§ 141.12 to read as follows:
§ 141,12 Maximum contaminant levels for organic chemicals.
  The following are the  maximum contaminant levels for organic chemicals. The
maximum contaminant levels for organic chemicals in paragraphs (a) and (b) of this
section apply to all community water systems. Compliance with the maximum con-
taminant levels  in paragraphs (a) and (b) is calculated pursuant to §  141.24. The
maximum contaminant  level for total  trihalomethanes  in paragraph (c) of this
section applies only to community water systems which serve a population of 10,000
or more individuals and which add a disinfectant (oxidant) to the water in any part of
the drinking water treatment process. Compliance with the maximum contaminant
level for total trihalomethanes is calculated pursuant to § 141.30.
•from Fnlrrat KesiMrr. 41, Ho, 2)1. 28641-28642 (Nov. 29. I979)ascor«cil
-------
  (c) Total  trihalomethanes  (the sum of the  concentration of bromodichloro-
methane, dibromochloromethane, tribromomethane [bromoform] and triehloro-
methane [chloroform]) 0.10 mg/L.
  4. By revising the title, the introductory text of paragraph (a)and paragraph (b) of
§ 141.24 to read as follows:
§ 141.24 Organic  chemicals  other than total  trihalomethanes, sampling,  and
analytical requirements.
  (a) An analysis of substances for the purpose of determining compliance with
§ 141.12(a) and  § 141.12(b) shall be made  as follows:
  (b) If the result of an analysis made pursuant to paragraph (a) of this section indi-
cates that the level of any contaminant listed in § 141,24 (a) and (b) exceeds the
maximum contaminant level, the supplier of water shall report to the State within 7
days and initiate three additional analyses within one month.
.  5. By adding a new §  141,30 to read as  follows:
§ 141.30 Total trihalomethanes sampling,  analytical and other requirements.
  (a) Community water systems which serve a population of 10,000 or more indi-
viduals and  which add a disinfectant (oxidant) to the  water in any part of the
drinking water  treatment process shall analyze for total trihalomethanes in accor-
dance with  this section. For systems serving 75,000 or more  individuals, sampling
and analyses shall begin not later than 1 year after the date of promulgation of this
regulation.  For systems serving 10,000 to 74,999 individuals, sampling and analyses
shall  begin not  later than 3 years after the  date of promulgation of this regulation.
For  the purpose of this section,  the minimum  number of samples required to be
taken by the system shall be based on the number  of treatment plants used by the
system, except that multiple wells drawing  raw water from a single aquifer may, with
the State approval, be considered one treatment plant for determining the minimum
number of samples.  All samples  taken within an established frequency shall be
collected within a 24-hour period,
  (b)(l) For all community water systems utilizing surface water sources in whole or
in part, and for all community water systems utilizing only ground water sources that
have not been determined by the State to qualify for the monitoring requirements of
paragraph (c) of this section, analyses for total trihalomethanes shall be performed at
quarterly intervals on at least four water samples for each treatment plant used by the
system. At least 25 percent of the samples shall be taken at locations within the distri-
bution system reflecting the maximum residence time of the water in the system. The
remaining 75 percent shall be taken at representative locations in the distribution
system, taking into account number of persons served, different sources of water and
different treatment methods employed. The results  of all analyses per quarter shall
be arithmetically averaged and reported to the State within 30 days of the system's
receipt of such results. Results shall also be reported to EPA  until such monitoring
requirements have  been adopted by the State. All samples collected shall be used in
the computation of the average, unless the  analytical results are invalidated for tech-
nical reasons. Sampli.ng and analyses shall  be conducted in accordance with the
methods listed in paragraph (e) of this section.
  (2) Upon the written request  of a community water system, the monitoring
frequency required by paragraph (b)( 1) of this section may be reduced by the State to
a minimum of one sample analyzed for TTHMs per quarter taken at a point in the
distribution system reflecting the  maximum residence  time of  the water in the
system, upon a written determination by the State that the data from at least I year of
monitoring in accordance with paragraph (b)(l) of this section and local conditions
demonstrate that total trihalomethane concentrations will be consistently below the
maximum contaminant level.
  (3) If at any time during which the reduced monitoring frequency prescribed under
this paragraph applies, the results from any analysis exceed 0.10 mg/L of TTHMs


                                                  Section XIII. Appendix   283

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and such results are confirmed by at least one check sample taken promptly after
such results are received, or if the system makes any significant change to its source of
water or treatment program, the system  shall immediately begin monitoring in
accordance  with  the  requirements  of paragraph (b)(l) of this  section,  which
monitoring shall continue for at least I year before the frequency may be reduced
again. At the option of the State, a system's monitoring frequency may and should be
increased above the minimum in those cases where it is necessary to detect variations
of TTHM levels within the  distribution system.
  (c){ 1) Upon written request to the State, a community water system utilizing only
ground water sources may seek to have the monitoring frequency required by sub-
paragraph {I) of paragraph  (b) of this section reduced to a minimum of one sample
for maximum TTH M potential per year for each treatment plant used by the system
taken at a point in the distribution system reflecting maximum residence time of the
water in the system. The system shall submit to the State the results of at least one
sample analyzed for maximum TTH M potential for each treatment plant used by the
system taken at a point in the distribution system reflecting maximum residence time
of the  water  in  the  system. The system's monitoring  frequency may only
be reduced upon a written determination by the State that, based upon the data sub-
mitted  by the system, the system has a maximum TTH M  potential of less than 0.10
mg/L and that, based upon  an assessment  of the local conditions of the system, the
system is not likely to approach or exceed the maximum contaminant level for total
TTH Ms. The results of all analyses shall be reported to the State within 30 days of
the system's receipt of such results. Results shall also  be reported to EPA until such
monitoring requirements have been adopted by the State. All samples collected shall
be used for determining whether the  system  must  comply with the monitoring
requirements of paragraph  (b) of this section, unless the analytical results  are
invalidated for  technical  reasons. Sampling and analyses shall be conducted in
accordance with the methods listed in paragraph (e) of this section.
  (2) If at any time during which the reduced monitoring frequency prescribed under
paragraph (c)(l) of this section applies, the results from  any analysis taken  by the
system for maximum TTH M potential  are equal to or greater than 0.10 mg/  L, and
such results are confirmed by at least one check sample taken promptly after such
results  are received, the system shall immediately begin monitoring in accordance
with the  requirements of paragraph  (b) of this section and such monitoring shall
continue for at least one year before the frequency may be reduced again. In the event
of any significant change to the system's raw water or treatment program, the system
shall immediately analyze an additional sample for maximum  TTHM potential
taken at a point in the distribution system reflecting maximum residence time of the
water in the system for the purpose of determining whether the system must comply
with the monitoring requirements of paragraph (b) of this section. At the option of
the State, monitoring frequencies  may and  should be increased above the minimum
in those cases where this is necessary to detect variation of TTHM levels within the
distribution system.
  (d) Compliance with §  14l.l2(c) shall be determined based on a running annual
average of quarterly samples collected by the system as prescribed in subparagraphs
(I) or (2) of paragraph (b) of this  section. If the average of samples covering any 12
month  period exceeds the Maximum Contaminant Level, the supplier of water shall
report to the State pursuant to § 141.31 and notify the public pursuant to § 141.32.
Monitoring after public notification shall be at a frequency designated  by the State
and shall continue until a monitoring schedule as a condition to a variance, exemp-
tion or enforcement action shall become effective.
  (e) Sampling and analyses made pursuant to this section shall be conducted  by one
of the following EPA approved methods:
   (I) "The Analysis of Trihalomethanes in Drinking Waters by the Purge and Trap
Method," Method 501.1, EMSL, EPA Cincinnati, Ohio.
  (2) "The  Analysis of Trihalomethanes  in Drinking  Water by Liquid/Liquid
Extraction," Method 501.2, EMSL,  EPA  Cincinnati, Ohio.

284  Treatment Techniques  for Controlling Trihalomethanes in Drinking Water

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Samples for TTHM shall be dechlorinated upon collection to prevent further pro-
duction of Trihalomethanes, according to the procedures described in the above two
methods. Samples for maximum TTHM potential should not be dechlorinated, and
should be held for seven days at 25° C (or above), prior to analysis, according to the
procedres described in the above two methods.
  (0 Before a community water system makes any significant modifications to its
existing treatment process for the purposes of achieving compliance with § 141.12(c),
such system must submit and obtain State approval of a detailed plan setting forth its
proposed modification and those safeguards that it will implement to ensure that the
bacteriological quality  of the drinking water served  by such system will not be
adversely  affected by  such modification.  Each  system shall comply with the
provisions set forth in the State-approved plan. At a  minimum, a State approved
plan shall require the system modifying'tts disinfection  practice to:
  (1) Evaluate the water system for sanitary defects and evaluate the source water for
biological quality;
  (2) Evaluate its existing treatment practices and consider improvements that will
minimize disinfectant demand and optimize finished water quality throughout the
distribution system;  •          •      :
  (3) Provide baseline water quality survey data of the distribution system. Such
data should include the results from monitoring for  coliform and fecal coliform
bacteria, fecal  streptococci, standard plate  counts at.35°C and 20°C, phosphate,
ammonia nitrogen and total organic carbon. Virus studies should be required where
source waters are heavily contaminated with sewage effluent;
  (4) Conduct additional monitoring to assure continued maintenance of optimal
biological quality in finished water, for example, when chloramines are introduced
as  disinfectants or  when pre-chlorination is being  discontinued.  Additional
monitoring should also be required by the State for chlorate, chlorite and chlorine
dioxide when chlorine dioxide is used. Standard plate count analyses should also be
required by the State as appropriate before and after any modifications;
  (5) Consider inclusion in the plan of provisions to maintain an active disinfectant
residual throughout the  distribution  system at all  times during and after the
modification.
This paragraph (f) shall become effective  on the date  of its promulgation.
                                                   Section XIII. Appendix  285

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                                      INDEX
 adsorption:
   to remove trihalomethane precursors,
     136-148
     granular activated carbon, 138-143
     powdered activated carbon, 136-138
     synthetic resins, 143-148
   to remove trihalomethanes, 53-81
     granular activated carbon, 61-81
     powdered activated carbon, 53-61
 aeration:
   to remove trihalomethane precursors, 124
   to remove trihalomethanes, 38-53
     costs, 230-233
     diffused-air aeration, 43-45
     quiescent standing, 43
     tower aeration, 46-49
 algae, as trihalomethane precursor, 122-123
 alternative disinfectants, 160-193
   advantages, 193
   bromine chloride, 182
   byproducts other than trihalomethanes,
     182-191
   chloramincs, 164-166, 168-175
   chlorine dioxide, 175-181
   costs, 248-252
     chlorine, 248
     chloramines, 250
     chlorine dioxide, 249-250
     ozone. 250
   disadvantages, 193
   effects on water quality, 211-221
   iodine. 182
   ozone. 181-182
 anion exchange, to remove THM pre-
   cursors, 245-246

 Beaver  Falls, PA, studies. 169, 198
 Bridgeport, CT. studies, 114
 Bristol County, RI, studies, 100
 bromide concentration, effect on trihalp-
   methanc formation,  13-15
 bromine chloride, effect on trihalomethane
   formation, 182

 Chapel  Hill, NC, studies,  135
 ehloramines:
   costs. 250
   disinfection byproducts, 189-190
   effect on trihalomethane formation,
     164-166. 168-175
   effect on water quality,  211
   non-trihalomethane disinfection
     byproducts, 189-190
chlorinatlon. moving point of application,
   88-99, 105-106
chlorine:
   costs, 248
   non-trihalomethane disinfection
     byproducts, 183-185
   dose and type, effect on trihalomethane
     formation, 20-21
   free, effect on trihalomethane formation,
     26-27, 168-175
chlorine-ammonia treatment. See
   chloramines
chlorine dioxide:
   costs, 249-250
   non-trihalomethane disinfection
     byproducts, 185-189
     inorganic byproducts, 189
     organic byproducts,  185-189
   effect on trihalomethane formation,
     175-181
   effect on water quality, 212-218
   to remove trihalomethane precursors,
     128-129
   to remove trihalomethanes, 37
chlorophenols, as byproducts of chlorine
   dioxide disinfection, 187-188
Cincinnati, OH, studies, 43-44, 55, 58-59,
   81-82, 94, 98, 105-106,  195, 222-225
clarification:
   costs, 235-240
   effect on water quality,  194r195
   to remove trihalomethane precursors,
     87-121, 235-239
     coagulation-sedimentation-filtration,
       94-107   '
     direct filtration, 109-114,
     precipitative softening, 107-109
coagulation, 88-109
Contra Costa, CA, studies, 15, 43-44,
   99-100, 123-124, 174-175
costs, treatment, 229-255

Davenport, 1A, studies, 71
Daytona Beach,  FL, studies, 107-109, JS5
degradation, biologic, to remove  trihalo-
   methane precursors, 152-154
/n-dihydroxybenzoic acid, as trihalo-
   methane precursor,  19-20
direct filtration, to remove trihalo-
2fiff  Index

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   methane precursors, 109-114. See also
   clarification
disinfectants, alternative. See alternative
   disinfectants
disinfection:
   non-triha!omethane byproducts, 182-191
     from chloramines, 189-190
     from chlorine, 183-185
     from chlorine dioxide, 185-189.
     chlorophenols. 187-188
     organic, 85
     organic halogen, 85, 191
     from ozone, 190
   comparative efficiencies of alternates,
     160-167
   costs, 248-253
   effect of parliculates, 166
   instantaneous, effect on water quality,
     218-221
   kinetics, 160-162
distributed water:
  bacterial quality, 226-227
  disinfectant, stability of, 225
  impacts on quality from treatment
    changes,  221-225
Durham, NC, studies, 106-107, 135
East Bay Municipal Utilities District, CA,
   studies, 59, 113
Evansville, IN, studies, 103, 176-177,
   215-216

filtration, to remove trihalomethane
   precursors, 94-107, 109-114. See also
   clarification
formation of trihalomethanes:
   effect of bromide concentration, 13-15
   effect of bromine chloride use, 182
   effect of chloramine use, 164-166,
     168-175
   effect of chlorine dioxide use, 175-181
   effect of chlorine dose and type, 20-21
   effect of free chlorine residual, 26-27,
     168-175
   effect of iodide concentration, 13-15
   effect of iodine use,  182
   effect of ozone use, 181-182
   effect of pH, 15, 28
   effect of temperature, 12, 27-28
   effect of time, 10
   general mechanism, 10
   effect of precursors,  16-20
free chlorine, and trihalomethane
   formation, 26-27,  168-175
fulvic acid, as trihalomethane precursor,
   19-20

granular activated carbon adsorption, 61 -68
   costs, 240-244
   effects on water quality,  195-211
     bacterial populations, 202-211
    coliform and standard plate count
      organisms, 195-202
  to remove trihalomethane precursors,
     138-143
  to remove trihalomethanes, 53-81

halogen, organic, as disinfection byproduct,
  191
health effects:
  of alternative disinfection byproducts, 193
  of trihalomethanes, 2-3
humic acid, as trihalomethane precursor, 16
Huntington, WV, studies, 195-198, 202
Huron,  SD, studies, 173
hydrogen peroxide, to remove trihalo-
  methane precursors, 136

instantaneous  disinfection, effect on water
  quality, 218-221
InstTHM:
  defined, 23
  measurement,  24-25
iodide concentration, effect on trihalo-
  methane formation, 13-15
iodine, effect on  trihalomethane formation,
  182
ion exchange,  to remove  trihalomethane
  precursors,  148-151
  costs, 245-248
  strong-base  anion exchange resins,
     148-151
  weak-base anion exchange resins, 151

Jefferson Parish, LA, studies,  109, 141,
  172-173,211

Kansas  City, MO, studies, 82-84

Los Angeles, CA, studies, 114
Louisville, KY, studies, 43-44, 55, 170-172,
  181, 211, 221-222

Maximum Contaminant  Level (MCL), 1,
  24, 36, 71
measurement of TH M precursors, 25-28, 87
measurement of trihalomethanes, 6-9,23-28
  gas chromatographic techniques, 6-7
     purge and trap, 6-7
    liquid-liquid extraction, 7
Miami,  PL, studies, 47, 59, 81-83, 109, 141,
  148-149, 203
moving  point of chlorine application, 88-99,
  105-106, 194-195

New Orleans,  LA, studies, 103, 138

Orange  County,  CA, studies, 47
organic  carbon, as trihalomethane measure-
  ment, 8
organic  disinfection byproducts, 85
organic  halogen, as disinfection byproduct,
  85, 191
                                                                       Index  287

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ORSANCO studies,  12, 70, 94, 169-170,
   177. 214
oxidation:
  to remove trihalomethane precursors,
     124-136
    chlorine dioxide, 128-129
    hydrogen peroxide, 136
    ozone, 125-128, 135
    ozone plus ultra-violet radiation,
       37-38, 135, 245
    potassium permanganate, 129-135
  to remove trihalomethancs, 36-38,
ozone;
  and  bacterial populations. 202. 207-211
  costs. 250
  disinfection byproducts, 190
  effects on trihalomethane formation,
    181-182
  to remove trihalomethane  precursors,
    125-128, 135
  to remove trihalomethanes, 36-38
ozone plus ultra-violet radiation:
  costs, 245
  to remove trihalomethane precursors, 135
  to remove trihalomethanes, 37-38

paniculate;, effect on disinfection, 166
pH:
   effect on trihalomethane formation, 15,28
   influence on removal  of trihalomethane
     precursors,  155-156
Pittsburgh. PA. studies, 94,  98, 195, 135
potassium permanganate, to remove trihalo-
   methane precursors, 129-135
powdered activated carbon adsorption:
   costs. 240-244
   to remove trihalomethane precursors,
     136-138
   to remove trihalomethanes, 53-61
precursors, trihalomethane. Set trihalo-
   methane precursors

removal  of trihalomethane precursors,
   87-159
   by adsorption, 136-148. See also
    adsorption
   advantages, 156-159
   by aeration, 124
   by anion exchange, 245-246
   by biologic degradation, 152-154
   by chlorine dioxide, 128-129
   by clarification, 87-121,235-239. See also
    clarification
  control of precursors at source, 122-124
  costs, 235-247
  disadvantages, 159
  effect on water quality, 194-211
   by hydrogen peroxide, 136
   by ion exchange, 148-151. See also ion
    exchange
   lack of, 85
  by lowering pH, 155-156
  by moving point of chlorine application,
    88-89, 105-106, 194-195
  by oxidation, 124-136. See also oxidation
  by ozone, 125-128, 135
  by ozone plus granular activated carbon
    adsorption, 244-245
  by ozone plus ultra-violet radiation, 135,
    245
  by potassium permanganate, 129-135
  by sedimentation, 94-107
removal of trihalomethanes, 36-86
  by adsorption, 53-81.Sfe also adsorption
  by aeration, 38-53. See also aeration
  by chlorine dioxide. 37
  costs, 230-235
  by oxidation, 36-38
  by ozone, 36-38
  by ozone plus ultra-violet radiation, 37-38
  by synthetic adsorption resins, 81-84
resins, synthetic:
  costs. 233-237
  to remove trihalomethane precursors,
    143-148
  to remove trihalomethanes, 81-84.
  See also ion exchange
resorcinol, as trihalomethane precursor,
  19-20
Rotterdam, The Netherlands, studies, 151,
  183

salt water, influencing trihalomethane
  formation, 123-124
sedimentation, to remove trihalomethane
  precursors. 94-107. See also clarification
Shreveport, LA, studies, 155
St.  Louis County Water Company, MO,
  studies, 169
  synthetic resins. See resins, synthetic

 temperature, effect on trihalomethane
   formation,  12, 27-28
 TcrmTHM:
  defined, 23
   measurement, 25-28
 THMFP:
  defined, 23
   measurement, 25-28
 total precursor, defined, 23
 treatment costs, 229-255
 treatment techniques, examples, 29-35
  conventional treatment, 30-33
  finished water InstTHM concentration
     reduction, 33-34
  simple chlorination, 29
 trihalomethane precursors:
  algae, 122-123
  control of at source, 122-124
  plankton control, 122-123
  m-dihydroxybenzoic acid,  19-20
  effect of characteristics and concentration
233  Index

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    on trihalomethane formation,  16-20
  fulvic acid, 19-20
  • humic acid, 16
  measurement, 87
  removal. See removal of trihalomethane
    precursors
  resorcinol, 19-20
  THMFP, 23, 25-28
  total, defined, 23
trihalomcthancs:
  discovery, 2
  formation, 2, 10-22, 160, 168-182.,
    Set  also formation of trihalomethanes
  health effects, 2-3
  measurement, 6-9, 23-28. See also
    measurement of trihalomethanes
  Regulation, 3-5, 282-285
  removal. See removal of trihalomethanes
Trihalomerhane Implementation Guidance,
  1, 5
TTHM, defined, 10
turbidity, effect on disinfection, 166

ultra-violet radiation. See ozone plus ultra-
  violet radiation
USEPA studies, 27, 44, 49, 66, 88,
  103-105, 109, 124-125, 129-130, 136-137,
  139-141, 152-153, 168-169, 175-177, 181,
  185-189, 191

water distribution;
  disinfectant stability during, 225
  impacts on quality from treatment
    changes, 221-225
water quality:
  distributed water, impacts of treatment
    changes, 221-225
  effect of alternative disinfectants, 211-221
    chlorine-ammonia  treatment, 211
    .chlorine dioxide, 212-218
    instantaneous disinfection, 218-221
  effects of THM control, 194-227
    clarification,  194-195
    granular activated  carbon adsorption,
       195-211
    removal of trihalomethane precursors,
       194-211
Wheeling, WV. studies, 94,  98
 *U.S.GOViRNMiNTPIUNTINCOFHCE!l991-5»8. IS 7/ Itssm                Index  289

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