-------
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
-------
CO
X
u
m
x
o
a.
oc
O
o >-
i <
O O
s
I
CO
o
10
ui
DC
3
O
tr
u.
O
z
o
-------
o
z
o
o
S
i
1H InstTHM
reatmen
t-
i
D THMFP
rH+iH TormTHM
B
^__t
aj i
E '
1
1
1
S -
C
*»'
B
ffi
e
1
-------
O
z
O
O
5
I
£
UJ
BC
1.0 --
0.5
M
.-» Q;
f*3?' T»!
i s -I I:
if i iJ
taste-
-------
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
^
<6
2
8.
3
»
3-
a>
-o
-^
a
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
»•
1'
§
S
*
1
o
s
Location
Jefferson Parish, LA
Jefferson Parish, LA
Jefferson Parish, LA
Jefferson Parish, LA
Jefferson Parish, LA
Jefferson Parish, LA
Jefferson Parish, LA
Type of GAC
Fihnnrb© 400
Filtratorb® 400
WVG 12x40
WVG 12i40
Fittrasorb® 400
WVG 12x40
Filtnturb® 400
Type of
system*
FS/SB
PC/PA
FS/PA
PC/PA
PC/PA
PC/PA
PC/PA
EBCT,
mm
23,0
23,0
24.0
33,0
35.0
44.0
46.0
Approximate
percent
initial
THMFP
removal
73
81
90
58
81
56
88
Approximate
time to
Heady-state
condrt»ru,t
weeks
24
21
20
24
21
11
17
Percent
THMFP
removal at
steady-stale
conditions
32
34
32
28
45
61
69
Influent
THMFP at
steady-stall
conditions,
MB/I
317
365
265
149
365
137
253
Sample storage
conditions
Time, Temperature,
days
5
5
5
5
5
5
5
°C§§
30
30
30
30
30
30
30
pH
10
to
10
10
10
10
10
Reference
14
14
14
14
14
14
14
•SR ~ u»d rtfltCMMt; fS - tM Kite; PA - pett-Blur idiortit. PC » pilot cghnn.
tPucMUlf at THWFP kth| imnrf k m Iwjn «. 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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
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I
3"
£
§"
Co
D
S
E
x
d
Z
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O
LU
o
K
<
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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
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8
100
z>
a
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ui
cc
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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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
a
8»
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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
-------
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 vslume divided by Hew ratel
/TOC * Total Organic Cufcon
252 Treatment Techniques for Controlling Trihalomethanes in Drinking Water
-------
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
-------
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
-------
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
-------
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).
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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
-------
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.,
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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
-------
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
-------
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,
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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.,
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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
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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
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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
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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
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131. Foster, D.M., Emerson, M.A., Buck, C.E., Walsh, D.S., and Sproul, O.J.,
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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
Combined Chlorine (Monochloramine) as a Primary Disinfectant of Drinking
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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
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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
-------
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
-------
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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