EPA/600/D~ 87/ 0 33
January 1987

COMPARISON OF SOME FILTRATION PROCESSES APPROPRIATE
FOR GIARDIA CYST REMOVAL

by

Gary S, Logsdon
Drinking Water Research Divisian
Water Engineering Research Laboratory
U.S. En\;ronmental Protection A^»ncy
CIr cinnati , Ohio 45268

WATER KNT. NEERINC RESEARCH LABORATORY
OFFICE 01' RESEARCH ANT) DEVELOPMENT

U , S . ENV: IIONMENTAL PROTECTION AC IxCY
¦ 1NC1NNATI, OH 45268


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(lPA 6co/Q-V7

TECHNICAL REPORT DATA

(Ph ase read Inslruclumi un Ihe h vem be/ure cumplclingj

1. REPORT NO. 2

EPA/600/D-87/033

'¦"wrTW&A has

4. TITLE AND SUBTITLE

Comparison of Some Filtration Processes Appropriate
for Giardia Cyst Removal

5 REPORT DATE

January 1987

6. PERFORMING ORGANIZATION CODE

7. AUTHOR(S)

Gary S. Logsdon

B PERFORMING ORGANIZATION REPOR1 NO

9 PERFORMING ORGANIZATION NAME AND ADDRESS

Chief, Microbiological Treatment Br.,
Drinking Water Research Div., WERL, USEPA
26 W St Clair St
Cincinnati OH 45268

10 PROGRAM ELEMENT NO

11 CONTRACT/GRANT NO

12 SPONSORING AGENCY NAME AND ADDRESS

WATER ENGINEERING RESEARCH LABORATORY
OFFICE OF RESEARCH AND DEVELOPMENT
U.S. ENVIRONMENTAL PROTECTION AGENCY
CINCINNATI, OH 45268

13. TYPE OF REPORT AND PEHIOO COVERED

14. SPONSORING AGENCY CODE

EPA/600/14

15. SUPPLEMENTARY NOTES

cr

-o

OCi

Slow sand filtration, aiatomaceous earth (OE) filtration, and coagulation-filtration
(Including conventional treatment, direct filtration, and In-line filtration), have
been evaluated for G1ardla cyst removal at pilot plant and/or field scale. Properly
designed and operated, the above process can attain 99 percent cyst reductions, or
higher. This paper discusses relative advantages and disadvantages of the proceses,
and factors that may result 1n success or failure of treatment. Slow sand filtration
1s the least complicated process from the operator's perspective. It may be the most
appropriate for small systems 1f the raw water 1s treatable. It very effectively
removes viruses, bacteria, and cysts; but 1t is not very effective for removal of THM
precursor organic chemicals. It gives the operator the least ability to change
treatment In response to changes 1n raw water. . DE filtration 1s very effective for
cyst removal, but removal of very small particles requires use of fine grades of DE
or chemical preconditioning of OE. Process modifications can yield Iron and man-
ganese removal. THM precursor removal 1s small. Operator skills required are mostly
of a mechanical nature. Coagulation-filtration has the greatest flexibility, and can
remove 30 to 50% of THM precursor; also turbidity, microorganisms, and metals that
can be precipitated before filtration. Many factors influence process performance so
a good understanding of coagulation chemistry 1s needed for most effective operation
regardless of plant size. This requires the greatest level of operator ability for
continued, dependable performance. Process variations Include conventional treatment,
direct filtration, and In-line filtration.

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NOTICE

This document has been reviewed in accordance with
U.S. Environmental Protection Agency policy and
approved for publication. Mention of trade names
or commercial products does not constitute endorse-
ment or recommendation for use.

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COMPARISON OF SOME FILTRATION PROCESSES APPROPRIATE
FOR GIARDIA CYST REMOVAL

Gary S. Logsdon*

INTRODUCTION

Waterborne giardiasis outbreaks have been occurring in the USA for the
past two decades, and continue to occur. This suggests a need for better
water treatment. Disinfection provides a barrier for waterborne transmission
of Giardia cysts. Craun (1986) reported that 19,770 cases of waterborne
giardiasis were related to deficiencies in treatment of surface water sources
by community water systems from 1965 throuyh 1984. Of these, 61% were related
to failures to adequately disinfect in systems having disinfection as the
only treatment. Another barrier is effective filtration. This paper reviews
filtration studies at pilot scale or full scale, or both, and compares per-
formance capabilities and advantages of slow sand filtration, diatomaceous
earth (DE) filtration, and coagulation-filtration. The latter category in-
cludes conventional filtration (coagulant feed and rapid mix, flocculation,
sedimentation, and filtration), direct filtration (coagulant feed and rapid
mix, flocculation, and filtration), and in-line filtration (coagulant feed
and rapid mix, followed by filtration).

All of the above filtration processes, if they are properly designed and
operated, and if they are treating a source water of suitable quality, can
reduce the concentration of Giardia cysts by 99 percent or more. Filtration
failures can occur because of improper design or operation, or because a
given process is not appropriate for the raw water being treated. Of the

* Chief, Microbiological Treatment Branch, Drinking Water Research
Oivision, Water Engineering Research Laboratory, U.S. Environmental
Protection Agency, Cincinnati, Ohio 45268


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19,770 cases of giardiasis mentioned above, 38% occurred because of failures
•in filtration. Aspects of filter plant design and operation are discussed in
subsequent sections of this paper, The relative costs of the processes are
not discussed because these would be influenced by conditions that are site
specific; thus general comparisons would be of limited usefulness.

SLOW SAND FILTRATION

Slow sand filtration studies have been supported in recent years by the
U.S. Environmental Protection Agency, the American Water Works Association
Research Foundation, and the State of Utah, among others. Some parameters
in EPA funded studies are given in Table 1. Filters have been evaluated for
ability to remove Giardia cysts, bacteria, turbidity, particles, and tri-
halomethane (THM) precursor.

Slow sand filters have been shown capable of removing 99 to 99.99 per-
cent of the raw Giardia cysts in water (Bellamy et_ aK 1985 a, 1985 b; Pyper,
1985). Using pilot filters Bel lamy ^t al_. (1985 a) found that cyst removal
did not deteriorate after filter scraping. Pyper (1985) observed that at
7.5°C to 21°C, cyst removal was 99.98% to 99,99t. At 0.5°C to 0.75°C, removal
ranged from 99.36% to 99.71%; however, at 0.5°C, cyst removal deteriorated to
93.7% when both Giardia cysts and primary unchlorinated sewage effluent were
added to the raw water simultaneously. In this situation, the loading of
organisms in the influent water may have been greater than the established
biological population of the slow sand filter could cope with.

Total r.oliform removal was found to be adversely influenced by increases
1n filtration rate from 0.04 to 0.4 m/hr (Bellamy	1985 a), by decreases

in filter bed deDth from 0.97 m to 0.48 m (Bellamy et al_., 1985 b), by in-
creases in sand size from 0.13 mm to 0.61 mm (Bellamy et_ aK, 1985 b), and by

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decreases in temperature from 17°C to 2°C (Bellamy et_ al_., 1985 b). Of these
parameters, the 0.61 mm sand size would be yreater than sizes tyoically used
and might have accentuated the adverse impact of that variable. The use of
0.61 mm sand resulted in average total collfohn removal of 96% vs. 99.4% for
0.13 mm sand. Temperature decreases from 17°C to 5°C or 2°C resulted in
deterioration in coliform removal from the 99% level to about 90% for the
colder waters. Cleasby et^ aK (1984 a) found that total coliform removal was
lower during the first two days after scraping than during the remainder of
the run. In some instances, differences in the two time periods were slight,
but 5 of 9 runs exhibited coliform removals ranging from 82% to 95% during
the first two days. Ouring the remainder of the runs, removals ranged from
97% to 100%. Cullen and Letterman (1985) in most cases did not observe any
effects of scraping (a ripening period) in total coliform data collected in a
study of seven operating slow sand filter plants in the State of New York.

Virus removal has been reported (Taylor, No Date) to be influenced by
temperature and filtration rate. At 0.20 m/hr and 11° to 12°C, removal was
99.9999% vs. 99.8% for 0.40 m/hr and 6°C. In another set of experiments,
Taylor reported 99.81 removal at 0.20 m/hr but only 91% at 0.40 m/hr.

Researchers have observed variation in the ability of slow sand filters
to reduce turbidity to the 1 Nephelometric Turbidity Unit (NTU) Maximum Con-
taminant Level (MCI) specified in the U.S. Environmental Protection Agency's
Drinking Water Regulations. Fox et al_. (1984) found that when water from a
gravel pit in southwestern Ohio was filtered at 0.12 m/hr, after an initial
ripening period had allowed the biopopulation to become established on new
sand, the I NTU MCI was always met. Raw water turbidity ranged from 0.2 to
10 NTU. Cleasby e£ aK (1984 a) reported that after the first two runs,

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typical effluent turbidity was 0.1 NTU except during the first two days after
scraping. Water for that research came from a gravel pit in central Iowa,
with turbidity ranging from <1 to 30 NTU. Pyper observed slow sand filtered
water turbidity of 0.1 NTU or less for 50% of the time, and 1.0 NTU or less
for 99% of the time in Mclndoe Falls, Vt. The source of water was Coburn
Pond, a body of open water with an open water surface area of about 4 hectares,
plus about 20 hectares of wetland. Raw water turbidity ranged from 0.4 to
4.6 NTU and color averaged 24 C.U. In contrast with these results, when
Horsetooth Reservoir was treated (Bellamy et al_. 1985 a, 1985 b), the filtered
water turbidity ranged from 3 NTU to 5 NTU, and the 1 NTU MCL was not met.
Raw water turbidity of Horsetooth Reservoir generally was 6 NTU to 8 NTU.

Slezak and Sims (1984) reported that about 15% of 27 plants surveyed produced
filtered water with an average turbidity of i.O NTU or higher, whereas tur-
bidity averaged 0.4 NTU or lower at half of the plants.

The different degrees of turbidity reduction in some cases may be
attributed to the nutrient condition of the filters. Water collected high
in the Rocky Mountains and transported to Horsetooth Reservoir would not be
expected to be high in nutrients for growth of biopopulation in filters.

Bellamy ejt aj_. (1985 b) reported adding sterile nutrient (BOO about 4 mg/L)
to one test filter, which should have increased the biopopulation in the
filter. Under parallel operation, turbidity reduction averaged 52% from this
filter vs. 15% from the filter treating unaltered Horsetooth Reservoir water.
Pavoni et^ al_. (1972) reported that exocellular polymers produced by bacteria
in an activated sludge culture were capable of flocculating Kaol1n1te sus-
pensions and promoting settling. It appears possible that the biological
population of a slow sand filter may produce exocellular polymers that enhance

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the "stickiness" of filter media and inorganic particles in the slow sand
filter, thus improving the filter's capability to remove such particles. The
surface waters tested in Iowa and Ohio contained sufficient nutrient to
support algae during the summer, and the water in Vermont would be expected
to be high in nutrients resulting from decaying vegetation in the wetlands.
Thus, we would infer that those waters had higher nutrient levels than the
Horsetooth Reservoir water.

Slow sand filters should not be expected to remove large amounts of THM
precursor unless something has been done to chemically alter the precursor
before filtration. Humic materials, although in contact with microorganisms
in nature, seem to persist in the environment. The biopopulation in the
Vermont slow sand filter removed about 1 OX of the trihalomethane formation
potential (THM FP) tnat was between 100 pg/L and 20U py/L in raw water. Fox
et^ aj_. (1984) reported TOC removal of 19* and THM FP removal of 18% when
treating southwestern Ohio gravel pit water.

In the research at Iowa State (Cleasby, 1984 b), algae were encountered
and evaluated for removal and influence on filter efficiency. Chlo'vphyl1-a
measurements were less than 5 pg/L during the winter and spring of 1981-1982,
until mid-April, increasing to nearly 60 pg/L in late April. Chlorophyl1-a
declined in May and June but appeared to peak near 140 ug/L in July. Algal
blooms occurred, and these influenced run length. Four runs ranged in length
from 10 to 22 days when mean chlorophyl1-a values were 8 to 138 pg/L. Runs
of 34 to 123 days were associated with chlorophyl1-a values of 1 to 4 pg/L.
Algae removal, as measured by chlorophyl1-a reductions, was quite high and
s.milar to removal of other particulate matter (generally approaching 99%).

Raw water quality limits for slow sand filters are stringent because

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particulate matter tends to be removed at the top of the filter and because
slow sand filters have limited capability to remove inorganic contaminants
and synthetic organic chemicals. Cleasby et^ al_. (1984 a) reported that
enumeration of algae or performing a surrogate measure of algal population
was necessary to judge the suitability of raw water for slow sand filtration.
Fox et^ al_. (1984) reported that treatment of Ohio River water (0.4-23 NTU)
resulted in progressively poorer filtered water quality over 250 days of
operation, with effluent turbidity exceeding 1 NTU during the last 20 days of
operation, and time to terminal head loss (0.4 m) decreasing from 98 days to
6 days. During the first 230 days, mean influent turbidity ranged from 2.4
to 7.6 NTU, levels that do not seem excessively high. Average raw water
turbidity was 10 NTU or lower at 90X of the operating plants surveyed by
Slezak and Sims (1984). Experience thus far suggests that the most reliable
way to determine treatability of water by slow sand filtration 1s to conduct
an extended pilot plant study.

Slow sand filters are simple to operate and maintain, when raw water
quality is appropriate and when the plants are small enough that complicated
equipment is not needed for filter scraping. Daily duties at a small in-
stallation (10,000 to 1,000,000 L/day) would include reading and recording
head loss, flow rates or totals, chlorine residual, raw and filtered water
turbidity, and adjusting flow.

Cullen and letterman (1985) studied filter scraping at seven slow sand
filtration plants in New York. Average flows ranged from 1 to 23 million
L/day. Scraping, or removal of a thin layer of sand when terminal head loss
1s reached, required an average of 5 hours per 100 m? of filter surface.
The thickness of the layer removed was typically 2 to 3 cm. The frequency

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of scraping would be determined by run length, which would be influenced by
the turbidity and algae in the raw water. After a sand filter has been
scraped a number of times, the full depth of the bed is restored in an oper-
ation called resanding. Cul len and Letterman estimated that resanding a
depth of 15 to 30 cm would require 48-59 hours of labor per 100 m^.

The advantages of slow sand filters are related mainly to the simplicity
inherent in the process. Small plants are simply to construct. Simple, man-
ually controlled valves can serve to control flow. Head loss can be measured
by a piezometer. Because changes in head loss occur slowly, recording equip-
ment is not needed. Coagulant chemicals are not used in slow sand filtration,
so operators do not need to understand coagulation chemistry. Chemical feed
pumps would not be needed for coagulant chemicals, so fewer pumps would be
used, lowering mechanical maintenance work. Operator skills do not need to
be as high as for plants using cogulation. Another advantage associated with
absence of coagulation is a minimum of waste disposal problems. Scraped sand
is essentially the only waste, and often it is washed and reused.

Many of the disadvantages of slow sand filtration are also related to
the absence of coagulation. Without pretreatment, limitations exist on
the quality of water that is suitable for slow sand filtration. These were
explained earlier. Because modifying a slow sand filter plant to treat a
difficult water might be costly, or not possible, pilot studies should be
performed to verify treatabi11ty. In addition, a study should be conducted
to establish that the raw water source 1s not likely to change or deteriorate
1n quality to such a degree that the water would become untreatable 1n the
future. This may not always be possible to ascertain, but an effort should
be made to predict what sort of human activities or development might happen

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in the foreseeable future. This would at least alert authorities to possible
need for changes in treatment if raw water quality deteriorated. Because
pretreatment is minimal or non existant at slow sand filter plants, little
capability generally exists to remove synthetic organic chemicals, trihalo-
methane precursors, and dissolved inorganic substances such as heavy metals.
In addition, very fine clays or glacial flour may not be readily removed.
Finally, slow sand filters may not be appropriate for medium to large in-
stallations in the USA, because of operating labor costs and land costs.
The trend for large systems is to automate and use mechanical equipment where
possible, but cleaning enclosed slow sand filters by mechanical means is very
difficult. Thus, they seem most appropriate for small systems located on
very high quality source waters.

DIATOMACEOUS EARTH FILTRATION
Diatomaceous earth (DE) filters have been studied for removal of a
variety of contaminants. They have been shown to attain excellent removal
of Giardia cysts over a broad range of operating conditions. Cyst removals
exceeding 99%, and often 99.91, were reported by Lange et_ aj_. (1986) for
filtration rates of 2.4 to 9.6 m/hr, for temperatures from 3.5 to 15°C, and
for four different grades of diatomaceous earth (Celite 545®, Celite 535®,
Celite 503*, and Hyflo Super-Cel*).*

Pyper (1985) reported 99.971 for one DE filter run in which Giardia
cysts were added. London et aK (1981) reported that when sufficient DE
precoat and body feed were used, removal of 9 pm radioactive beads was nearly
always 99.92 or higher. Use of a precoat of at least 1.0 kg/m^ was shown to

* Mention or use of commercial products does not constitute endorsement
by the U.S. Environmental Protection Agency.

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be appropriate for obtaining most effective removal of the 9 jjm particles.

They also reported that eleven filter runs were made with G_. muris cysts
at filtration ratet, of 2.2 to 3.5 m/hr, with Celite 535® precoat and body
feed. Cyst removal exceeded 99.0% in all runs, and exceeded 99.9% 1n five
of the runs. DeWalle et^ al_. (1984) reported on four 0E filter runs conducted
for Giardia cyst removal. Cyst removal exceeded 99% in each of the four runs.
The overall results of all research for Giardia cyst removal indicate that
DE filtration is very effective for controlling Giardia cysts. Factors
important to continued effective performance are using adequate precoat and
body feed, and keeping the septum very clean (good cleaning at the end of
each run).

Removal of total coliform bacteria by 0E filtration was studied exten-
sively at Colorado State University by Lange et^ al_. (1986). Coliform removals
were strongly influenced by the grade of diatomaceous earth used. Coarser
grades attained removals ranging from 30% to 50% for Celite 545® and from
501 to 70% with Celite 503®. The fine grades, with smaller pores, were con-
siderably more effective. Remova1 with Celite 512® was 92% to 96%, and total
coliform removal with S'jper-Cel® was 99.92% to greater than 99.98%.

Malina at aK (1971) reported that a high percentage of removal could
be attained for pcliovirus when coated DE filter aid was used or when cationic
polymer was added to the raw water. In one 12-hour filter run, diatomaceous
earth coated with 1 mg of cationic polymer per (jr-t of DE produced filtei'd
water in which no viruses were recovered from 11 samples (removal >99.15%).
One of 12 samples was positive, and In this Instance, virus removal was 99%.
In a 12-hour run in which uncoated DE was used and 0.14 mg/L of cationic
polymer was added to the raw water, no viruses were recovered from any of the

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12 samples analyzed.

Turbidity removal when treating Horsetooth Reservoir water, as reported
by Lange et^ £1_. (1986), was less than 20% for the grades of diatomaceous earth
commonly used for water treatment (Celite 545®, Celite 535®, Celite 503®, and
Hyflo Super-Cel®). Turbidity of the Horsetooth Reservoir raw water ranged
from 4.5 to 5.4 NTU. The finest grade tested, Filter-Cel®, could reduce the
turbidity by over 95%. In contrast to these results, Logsdon et al_, (1981)
reported that turbidity reductions of 56% to 78% were attained with Celite
535® when raw water turbidity ranged from 0.95 to 2.5 NTU, but little change
was observed when raw water turbidity ranged from 0.24 to 0.45 NTU. Pyper
(1985) reported an average turbidity reduction of 71%, with an effluent
quality of 0.5 NTU.

Pyper evaluated OE filtration for removal of THM precursor in Vermont.
Results showed no difference between the raw water and the filtered water,
suggesting that the THM precursor material present in Coburn Pond was dis-
solved. The water was colored (24 CU, average), and this may explain the
lack of change during filtration, because DE filtration alone does not
-emove color, a known precursor.

Because turbidity removal with the grades of diatomaceous earth commonly
used for water treatment was so low when Horsetooth Reservoir water was fil-
tered, the Colorado State university researchers investigated the nature of
the turbidity (Bellamy et_ aj_., 1984). When 5.6 NTU raw water was filtered,
turbidity was reduced 2% by a 5 jjm pore size membrane, 36% by a 1.2 pm mem-
brane, 73% by a 0.45 pm membrane, and 91% by a 0.22 pm membrane. Most of
the light scattering matter In the water (the cause of the turbidity) was
made up of particles that could pass through 1.2 pm pores, and thus fine

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enough to pass through typical potable water grades of OE.

Additional work was done at Colorado State University to improve the
capabilities of DE filtration. In order to alter the surface properties of
diatomaceous earth, aluminum hydroxide was precipitated to the surface of a
OE slurry. With 0.05 grams of alum per gram of Celite 545®, total coliform
removal was 99.86%, as compared to 30% to 50% removal for uncoated Celite
545®. For the same grade of OE, turbidity removal was 98%, for coated OE
vs. under 20% for uncoated DE (Lange et a]_., 1986). These results show that
the straining mechanism of removal can be augmented by a surface attachment
removal mechanism if 0E is given an electropositive coating.

Limits on the quality of raw water that would be appropriate for 0E
filtration are not easy to set. The process removes particulate matter by
trapping it within the filter cake. As the concentration of particulate
matter in raw water increases the load applied to the filter cake increases.
To maintain high permeability of the filter cake and good head loss character-
istics, body feed diatomaceous earth is added to the raw water. A rule of
thumb is that higher raw water particle concentrations require more body
feed, if the nature of the particles does not change. The nature of the
particles being removed is quite important though - especially the compressi-
bility. Rigid turbidity-causing particles, such as very fine sand, would not
block or blind the filter cake, but compressible particles, such as algae,
coagulation floe, precipitated iron, or biological matter could blind the
filter cake. Pilot filtration studies are advisable 1f the water in question
is not already being treated by 0E filtration. Such studies would establish
the appropriate grade of DE to use to obtain the desired effluent turbidity,
the amount of body feed to add under conditions of the test runs, and the

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ipproximatp length of filter run to expect, letterman and Logsdon (1976)
iurveyed 13 DE filtration plants and reported that filtered water turbidities
ibove 1 NTU or filter runs of 6 or fewer hours were observed at DE plants
laving maximum raw water turbidities of 20 NTU or greater (Fig. 1). This
figure shows the percentage of plants exceeding specified values for minimum,
average, and maximum raw water turbidity. Symbols shown in the legend identify
plant problems with high filtered water turbidity or short runs or both.

Operation and maintenance of diatomaceous earth filters is somewhat more
complex than for slow sand filters, but less complicated than coagulation-
filtration. Daily monitoring would include turbidity, disinfection residual,
rate of water production with adjustments if needed, filter head loss, and
rate of use of body feed. Periodic chores would include preparation of body
feed slurry and precoat slurry and maintenance checks on body feed and precoat
pumps. Also, filters would need to be backwashed periodically, but disposal
of spent filter cake should present few problems, because it is not gelatinous
and dries readily. Filter elements (septa) need to be kept very clean. The
cleanliness of the septa can be readily checked if vacuum filters or quick-
opening pressure filters are used. Because of the number of pumps, valves,
and other mechanical items in use at a DE filtration plant, operators should
possess good mechanical skills. Knowledge of coagulation chemistry would not
be needed unless the diatomaceous earth was conditioned by the alum coating
technique.

Oiatomaceous earth filtration has several Important advantages, especially
with respect to treating waters that may contain Giardia cysts. The process
has been shown in four studies to be very effective for cyst removal, and
the removal efficiency is not affected by very low temperatures. Different

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grades of diatomaceous earth can be kept on hand, giving the operator some
flexibility if the grade in use passes too many turbidity causing particles.
If necessary, the surface attachment properties of the coarse grades of
diatomaceous earth can be markedly enhanced by the alum coating procedure.
Diatomaceous earth filter plants do not require large land area, and are in
use for capacities up to 50 or 60 million L/day.

Among the disadvantages of diatomaceous earth are the need for high
quality raw water, the inability to remove dissolved substances, and the in-
ability to remove very fine particles with plain diatomaceous earth. Excessive
suspended solids (turbidity, algae) in raw water can cause short filter runs.
Bubbles may form and collapse in the filter cake if the vacuum DE filters are
used to treat cold, highly oxygenated water. If pressure DE filters are used
and operated to high head loss to obtain long runs and economical use of DE
precoat material, high energy costs may result.

COAGULATION-FILTRATION

The process train used most often in the United States for filtration
involves chemical pretreatment (coagulation, and frequently flocculation and
sedimentation) followed by deep bed granular media filtration. Most U.S.
coagulation-filtration research for Giardia cyst removal has focused on the
coagulation-filtration (in-line) or coagulation-flocculation-filtration
(direct filtration) variations of the process, because waterborne giardiasis
outbreaks tended to be observed in regions of the country that had low tur-
bidity waters which were thought to be suitable for such treatment. Research
by Logsdon et aj_. (1981), De Wal le et_ al_. (1984), and Al-Ani et_ al_. (1986)
involved coagulation with alum, or alum plus a polymer; filtration through
sand or dual media at 5 to 14 meters/hr; and temperature ranging from 3° to

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20°C. Later research (Logsdon et al_., 1985) was conducted on conventional
treatment, with alum or alum and polymer, dual media and three monomedia
types (sand, anthracite, GAC), filtration at 7 m/hr, and room temperatures
(about 25°C).

Results of the three cited direct filtration studies indicate that
Giardia cyst removal can exceed 99.0% or even 99.9% when the raw water is
coagulated properly and filtered. Results of Logsdon _et_ a_l_- (1981) and
De Walle et^ aj_. (1984) indicated that with proper pretreatment, cyst removal
exceeded 99.0% when filtered water turbidity was below 0.30 NTU. Al-Ani
et aj[. (1986) showed that cyst removal of 99% or more was likely to occur if
turbidity removal was 70% or more, when raw waters in the 0.2 to 1 NTU range
were treated. This would produce filtered waters in the 0.06 to 0.30 NTU
range.

All of the above researchers showed that dependable cyst removal results
can not be attained if a clear water (about 1 NTU) is filtered without being
properly coagulated. Use of no coagulant, or of an improper dose, resulted
in erratic cyst removal results. In addition, DeWalle al_. (1984) showed
that for alum coagulation, using the proper pH is necessary when soft, low
alkalinity water is treated. They observed effective treatment at pH 5.6 and
6.2, but at pH 6.8 with alum coagulation, cyst removal was reduced from 99%
to 95%.

The coagulation-filtration process can remove a variety of contaminants.
Robeck et aj_. (1962) showed that direct filtration could remove 90% to 99%
of viruses, while conventional treatment removals consistently were 99%.
McCormick and King (1982) stated that coHform removal by direct filtration
was practically 100% when filtered water turbidity was 0.10 NTU or less.

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Cleasby et^ al_. (1984) reported that in-line filtration removed more than 86%
of the total coliform bacteria in raw water, after the first hour of the
filter run had passed, in 10 test runs. Edzwald (1986) showed that direct
filtration could remove nonpurgeable total organic carbon (NPTOC) and organic
precursor materials that form trihalomethanes (TTHMFP, or total trihalomethane
formation potential). With cationic polymer as the primary coagulant, both
NPTOC removal and TTHMFP removal were about 40% whereas with alum as the
primary coagulant removals of NPTOC and TTHMFP were nearly 60%. With the
same waters, when conventional treatment was employed with alum as the primary
coagulant, removals of NPTOC and THMFP were about 70%. Cleasby et_ a_l_. (1984
a) reported that waters with low to moderate algal populations, water could
be treated by direct filtration. Water with few algae had a chlorophyl1-a
concentration of less than 5 /jg/L (Cleasby et aj_. 1984 b). Water with an
algal population sufficient to result in a chlorophyl1-a concentration of
130 jjg/L could not be effectively treated by direct filtration without
prechlorination.

Suggested limits on raw water quality for sources receiving complete
conventional treatment (including predisinfection, coagulation, sedimentation,
rapid granular filtration, and post disinfection) were given in the "Manual
For Evaluating Public Drinking Water Supplies" as a monthly geometric mean of
not more than 2,000 fecal coliform per 100 ml or a monthly geometric mean of
not more than 20,000 total coliform bacteria per 100 mL, color not to exceed
75 units, odor not to exceed a threshold odor number of 5, and turbidity not
to be so high as to overload the water treatment works (U.S. Environmental
Protection Agency, Water Supply Division, 1980).

Sugyested limits on raw water quality for direct filtration and 1n-l1ne

15


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filtration are much more stringent. Cleasby et^ al_. (1984 a) suggested that
average raw water turbidity should depend on whether the primary coagulant
is alum or a cationir. polymer, and on whether algal population 1s low or
moderate. Suggested values ranged from 7 NTU for moderate algae and alum
coagulation to 16 NTU for low algae and cationlc polymer coagulation. The
Direct Filtration Subcommittee of the AWWA Filtration Committee (Bishop et_
al_. 1980) reported that waters with less than 40 units of color, turbidity
below 5 NTU, iron less than 0.3 mg/l, manganese less than 0.05 mg/L, and
algae counts up to 2000 ASU/mL appeared to be "perfect candidates for direct
filtration." In a survey of 17 direct filtration plants (Letterman and
Logsdon, 1976), short filter runs (6 or fewer hours) were occasionally ob-
served when maximum raw water turbidity was 8 NTU or higher, and both short
runs and filtered water turbidity above 1 NTU were sometimes observed when
raw water turbidity was 20 NTU or higher (Fig. 2). This figure shows the
percentage of plants exceeding specified values for minimum, average, and
maximum raw water turbidity. Synobols shown 1n the legend identify plant
problems with high filtered water turbidity or short runs or both. From the
work of Edzwald (1986), 1t can be inferred that 1f the THM formation potential
of a water exceeds 0.20 mg/L, direct filtration may not be able to produce a
*ater that will meet the 0.10 mg/L MCL for trihalomethanes.

Operation and maintenance for coagulation-filtration plants can be more
demanding than that for DE plants or slow sand filter plants. Both conven-
tional plants and direct filtration plants should be monitored carefully,
because failure to obtain optimum coagulation can result in poor filter per-
formance. Although conventional plants are generally considered to have a
"margin of safety" with respect to coagulation control, because of the hours

16


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sf detention time afforded by settling basins, if coagulation control is lost
at the chemical feed and rapid mix point, and if this goes unnoticed until
the poorly coagulated water reaches the filters, plant operators could find
themselves in the dilemma of having settling basins full of water that could
not be filtered successfully.

Coagulation monitoring and control are very important, whether or not
the plant employs sedimentation. One traditional approach to control is jar
testing. For waters of perhaps 10 NTU or higher, jar testing combined with
continuous monitoring of the turbidity of the filtered water at individual
filters is an approach frequently used. If raw water quality can change
rapidly, or if the raw water turbidity is low (below 10 NTU), jar tests may
not be very effective, because of the time required for testing, or because
of the smaller differences in raw and settled water turbidities. In such in-
stances, coagulant dose control by zeta potential instrumentation, a stream-
ing current detector, or a pilot filter may be appropriate. Wagner and
Hudson (1982) suggested that filter paper filtration using Whatman No. 40
paper could give information on the treatment levels that produce acceptable
water quality. Other appropriate monitoring would include pH, head loss,
chemical feed, and raw and filtered water turbidity.

Maintenance operations would include care of chemical mixers and feeders,
perhaps flocculation basin mixers and sludge removal equipment in settling
basins. Filter backwashlng Is necessary, and backwash water and settling
basin sludge may require treatment and ultimate disposal. If sludge removal
from settling basins 1s not done mechanically, periodic manual basin cleaning
would be needed.

The level of operating skill needed at coagulation-filtration plants is

17


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substantial. In order to effectively J-nd efficiently control the coagulation-
filtration process and attain low filtered water turbidity, operators need
to understand the chemical aspects of coagulation. Large and medium sized
plants are able to hire and keep trained operators who can effectively operate
coagulation-filtration plants. On the other hand, small plants may not have
the resources to hire or train operators who have a solid understanding of
coagulation. This can lead to problems of poor treated water quality, if
operators are unable to adjust treatment when raw water quality changes.

Of the t'iree processes discussed in this paper, coagulation-filtration
has the greatest f1 • >1b1ity in the kind and concentration of contaminants
that can be removed in the process, especially when sedimentation is employed.
Conventional treatrent can handle the widest ranys in raw water quality, and
has been in use for several decades. Coagulation-filtration plants, because
they employ more treatment processes, can be designed with the most flexi-
bility in terms of the number of processes used. For example, settling might
be used for muddy water but bypassed when raw water turbidity Is low. Recent
developments, such as use of media in the 1 to 2 mm size range, beds about
2 meters in depth, and filtration rates of 25 m/hr or higher provide even
">ore treatment capability for the coagulation-f1ltration process, but until
experience with such plants is gained, the very high rates of filtration
probably should be considered only at large water utilities with well-
trained, full time operators and laboratory personnel.

In spite of the many advantages that can be listed for coagulation-
filtration, a number of drawbacks exist. The most Important potential problem
1s this: for rapid rate granular media filtration to be an effective process
for removal of particulate matter, the chemistry of the water must be manlpu-

18


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lated so that coagulation is effective. This can be done through adjustment
of pH and addition of an inorganic coagulant or polymer or both. At utilities
that serve 59,000 to 100,000 persons or more, hiring one or more scientists
to work in a water quality control laboratory can be considered feasible, as
1t 1s presently being done. At water utilities too small to employ a chemist,
operation of the coagulant-filtration process may be less than optimum.

Testing by persons who understand the process can establish the proper chem-
ical treatment under the raw water quality conditions existing during the
test period. The ability of operators to understand the implications of
changing raw water qualty and make proper adjustments could result in lower
process efficiency, though. A fundamental concept is that coagulation chemistry
is not influenced by the magnitude of the flow in a plant. Factors such as
pH, alkalinity, and temperature must be considered, regardless of the size of
the plant.

A particular concern in northern latitudes or mountainous areas where
giardiasis outbreaks may have occurred is the difficulty of effectively
coagulating and filtering cold, clear waters. When the raw water turbidity
is close to 1 NTU, some plant operators may question the value of adding a
coagulant. Others may be discouraged by the apparent difficulty in treating
a clear water at temperatures close to 0UC, and in both instances, operators
nay shut off the chemical feeders. Coagulant feed should never be Interrupted
nor shut off. Techniques are available for treating cold waters and low tur-
bidity waters. Performing jar tests with the jars In an 1ce water bath is
appropriate. Use of paper filters or small (2.5 cm) mini-filters with beds
30 cm deep, or shallower, could be used to evaluate f11terab1l1ty of clear
waters. Use of streaming current detectors as an on-Hne coagulant dose

19


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control device appears to work well in winter. Experience Indicates that
coagulation-filtration plants can produce high quality water even when
temperature and turbidity in the raw water are low. The Duluth, Minnesota
filtration plant consistently produced filtered water below 0.10 NTU and
attained 99% to 99.99% reductions of asbestos fibers even when temperatures
were in 3° to 5°C range and raw water turbidity was 1 NTU (Logsdon et. al..
1983).

CONCLUSIONS

'• Each of the three filtration processes reviewed 1s different, and no

single process is ideal in every circumstance.

2* As process complexity increases, from slow sand filtration, to DE fil-
tration, to coagulation-filtration, the skill level needed for effective

operation Increases.

As process complexity increases, producing high quality filtered water
increasingly becomes dependent on operator skill and ability.

A variety of filtration processes have been used successfully either
on a pilot plant scale or at full scale to remove Giardia cysts from

water.

5* Slow sand filtration, DE filtration, and the coagulation-filtration
(1n-l1ne or direct filtration) processes used without sedimentation
are all affected by raw water quality, with respect to both filtered
water quality and plant performance characteristics, such as filter
run length. Therefore, if use of any of these processes is contemplated
with a water source that is not presently being treated successfully
by the process, performing a pilot plant study before design and
construction of the treatment plant Is highly advisable.

20


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6. Even though Important limitations exist and must be taken Into account,
filtration technology capable of removing 99% or more of the Glardia
cysts from drinking water exists and is in use in many locations.

REFERENCES

Al-An1, M.Y., 0. W. Hendricks, G. S. Logsdon, and C. P. Hibler. 1986.

Removing Giardia Cysts from Low Turbidity Waters by Rapid Rate Filtration.
Jour. American Water Works Assoc. 78:5:66-73.

Bellamy, W. D., K. P. Lange, and D. W. Hendricks. 1984. Filtration of
Giardia Cysts and Other Substances: Volume 1. Diatomaceous Earth
Filtration. EPA-600/2-84-114, U.S. Environmental Protection Agency,
Cincinnati, Ohio, 1967.

Bellamy, W. D., 0. W. Hendricks, and G. S. Logsdon. 1985 a. Slow Sand

Filtration: Influences of Selected Process Variables. Jour. American
Water Works Assoc. 77:12:62-66.

Bellamy, W. D., G. P. Silverman, and D. W. Hendricks. 1985 b. Filtration

of Giardia Cysts and Other Substances: Volume 2. Slow Sand Filtration.
EPA 600/2-85/026, U.S. Environmental Protection Agency, Cincinnati,

Ohio.

Bishop, S., T. F. Craft, 0. R. Fisher, M. Ghosh, P.w. Prendiville, K. J.
Roberts, S. Stelmle, and J. Thompson. 1980. The Status of Direct
Filtration, Committee Report. Jour. American Water Works Assoc. 72:7:
405-411.

Cleasby, J. L., 0. J. Hllmoe, and C. J. Dlmltracopoulos. 1984 a. Slow

Sand and Direct In-line Filtration of a Surface Water. Jour. American
Water Works Assoc. 7(5:12:44-55.

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Cleasby, J. L., D. J. Hilmoe, C. Dimitracopoulos, and L. M. D1az-Bos$1o.

1984 b. Effective Filtration of Small Water Supplies. EPA-600/2-84-083,
U.S. Environmental Protection Agency, Cincinnati, Ohio.

Craun, G. F. 1986. Waterborne Giardiasis 1n the United States 1965-1984.

Lancet H_: 8505:513-514.

DeWalle, F. B., J. Engeset, and W. Lawrence. 1984. Removal of Giardia
lamb!1a Cysts by Drinking Water Treatment Plants. EPA-600/2-84-069,
U.S. Environmental Protection Agency, Cincinnati, Ohio.

Edzwald, J. K. 1986. Conventional Water Treatment and Direct Filtration:
Treatment and Removal of Total Organic Carbon and Trihalomethane Pre-
cursors, p. 199-236. _In N. M. Ram, E. J. Calabrese, and R. F. Christman
(eds.) Organic Carcinogens in Drinking Water: Detection, Treatment and
Risk Assessment, John Wiley & Sons, N.Y.

Fox, K. R., R. J. Miltner, G. S. Logsdon, D. L. Dicks, and L. F. Drolet.
1984. Pilot Plant Studies of Slow-Rate Filtration. Jour. American
Water Works Assoc. 76:2:62-68.

Lange, K. P., W. 0. Bellamy, D. W. Hendricks, and G. S. Logsdon. 1986.
Diatomacebus Earth Filtration of Giardia Cysts and Other Substances.

Jour. American Water Works Assoc. 78:1:76-84.

Letterman, R. D., and G. S. Logsdon. 1976. Survey of Direct Filtration
Practice - Preliminary Report. Presented at American Water Works
Association Annual Conference, New Orleans, Louisiana. June,

1976.

Letterman, R. D.t aid T. R. Cullen, Jr. 1985. Slow Sand Filter Maintenance:
Costs and Effects on Water Quality. EPA/600/2-85/056, u.S Environ-
mental Protection Agency, Cincinnati, Ohio.


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Logsdon, G. S., J. M. Symons, R. L. Hoye, Jr., and M. M. Aroi.irena. 1981.
Alternative Filtration Methods for Removal of Giardia Cysts and Cyst
Models. Jour. American Water Works Assoc. 73:2:111-118.

Logsdon, G. S., G. L. Evavold, J. L. Patton, and J. Watkins, Jr. 1983.

Filter Plant Design for Asbestos Fiber Removal. Jour, of Enviornmental
Engineering. 109:4:900-914.

Logsdon, G. S., V. C. Thurman, E. S. Frindt, and J. G. Stoecker. 1985.
Evaluating Sedimentation and Various Filter Media for Removal of
Giardia Cysts. Jour. American Water Works Assoc. 77:2:61-66.

Malina, J. F., Jr., B. D. Moore, and J. L. Marshall. 1972. Poliovirus

Removal by Diatomaceous Earth Filtration. Center for Research in Water
Resources, The University of Texas, Austin, Texas.

McCormick, R. F. and p. H. King. 1982. Factors That Affect Use of Direct
Filtration in Treating Surface Waters. Jour. American Water Works
Assoc. 74_: 5:234-242.

Pavoni, J. L., M. W. Tenney, and W. F. Echelberger, Jr. 1972. Bacterial

Exocellular Polymers and Biological Flocculation. Jour. Water Pollution
Control Federation 44:3:414-431.

Pyper, G. R. 1985. Slow Sand Filter and Package Treatment Plant Evaluation:
Operating Costs and Removal of Bacteria, Giardia, and Trihalomethanes.
EPA/600/2-85/052, U.S. Environmental Protection Agency, Cincinnati,

Ohio.

Robeck, G. G., N. A. Clarke, and K. A. Dostal. 1962. Effectiveness of

Water Treatment Processes in Virus Removal. Jour. American Water Works
Assoc. 54:10:1275-1290.

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Slezak, L. A., and R. C. Sims. 1984. The Application and Effectiveness of
Slow Sand Filtration in the United States. Jour. American Water Works
Assoc. 76:12:38-43.

Taylor, E. W. No Date. Forty-Fifth Report ort the Results of the Bacterio-
logical, Chemical and Biological Examination of the London Waters for
the Years 1971-1973. Metropolitan Water Board, London, England.

Wagner, E. G., and H. E. Hudson, Jr. 1982. Low-Dosage High-Rate Direct
Filtration. Jour. American Water Works Assoc. 74:5:256-261 .

Water Supply division, U.S. Environmental Protection Agency. 1980. Manual
for Evaluating Public Drinking Water Supplies. EPA-430/9-75-011.
Washington, D.C.

24


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TABLE 1. PARAMETERS IN SLOW SAND FILTER RESEARCH

Filter Design

Raw Water Quality

Reference

Sand Uniformity
Size, Coefficient
mm

Filtration Bed
Rate, Depth,
m/hr	m

Temp., Turbidity,
°C	NTU

Tota1
Coliform
per 100 mL

Other

ro
LA

0.17
0.32
0.33

2.1
1.4
2.8

0.13	1.5

to	to

0.62	1.6

0.12
0.12
0.08

0.04
to
0.40

0.76 about 25° <1 to 10
(room temp.)

0.94
1.07

0.48
to
0.97

10 to 10,000
2° to 28° <1 to >30 40 to 10,000
0° to 25° 0.2 to 59 1 to 8,700

2U to 17° 2.7 to 11

0 to 209,000 50 to 5,075 Giardia
cysts/L spiked

Fox et al.
1984

Cleasby et
al. 1984 b

0.2 to 143 mg/m3
chlorophyl1-a

(2.1 to 26)xl06 Giardia Pyper
cyst spiked [35 to 425 1985
cyst/L if diluted over
filter uniformly]

Bel 1 amy
et al.
1985a,
1985b


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1000

BOO

600

500

400

300

200

100

80

60

50

40

30

20

10

8

6

5

4

3

2

1

8

.6

.5

.4

.3

.2

.1

0 Maximum turbidity of
¦ filtered woter>l TU

Vf This plant had short filter runs
(6 hr. or less) caused by turbidity

X This plonf ho<
runt and ah
turbidity »xi

99

95

J-Ar

JL

4.

•0 50 30

% EXCEEDING

: l

Influence of raw water turbidity on diatomaceous earth
plant performance

26


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Maximum turbidity of filtered water
exceeded 1 TU	$(

This plant had short filter runs
(6 hr. or less) caused by turbidity
V this plant had short filter
runs and also filtered water
turbidity exceeded 1 TU

X

X

X

99 93 SO	JO	30	5	I

% EXCEEDING

Influence of raw water turbidity on granular media
plant performance

FIGURE 2

27


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